Document emxpkGw1DQyEbvb3jk13D4eRq

PPG Industries, Inc. Lake Charles, Louisiana EN3R Enforceable Commitment Volume I: General Distribution ENSR Consulting and Engineering Submitted January 1992 Revised May 1992 Document Number 5510-016-114 SL 025815 PPG Industries, Inc. Chemicals Post Office Box 1000 Lake Charles. Louisiana 70602 USA May 20, 1992 Mr. Stanley Meiburg Director, Air, Pesticides and Toxics Oivision (6T) United States Environmental Protection Agency Region 6 1445 Ross Avenue, Suite 1200 Dallas, TX 75202-2733 Re: Enforceable Commitment for PPG Industries, Inc. Lake Charles, Louisiana Complex Dear Mr. Meiburg: PPG has addressed the concerns listed in your letter dated February 28, 1992, which was in response to the Enforceable Commitment Document (ECD) filed by PPG Industries, Inc., Lake Charles, Louisiana on January 20,1992. PPG revised the ECD filed in January 1992 in response to recommendations made by Mr. Dave Beck of EPA OAGPS during a conference call made on April 7,1992 involving PPG, ENSR, LDEQ, EPA Region 6 and EPA OAQPS (RTP). PPG would like to thank Ms. Tanya Murray for sending ENSR the final copy of the Procedures for Establishing Emissions for Early Reduction Compliance Extensions. Volume I ---Synthetic Organic Chemical Manufacturing Ethvlene Oxide Sterilization, and Chromium Electroplating. (EPA-450/3-91-012a) for the calculations of the air emissions. PPG has used forms from that document in the updated ECD. PPG's reply to the concerns listed in your letter are as follows: Request #1. One of the requirements of the Early Reduction application is evidence that the base year emissions are verifiable and representative wh n compared to other years. Your Table 3*1 compares years 1985 through 1990 based on the production rate to show that the base year 1987 Is representative. Please explain the correlation between emission and production numbers especially In view of the fact that some of the emissions came from the wastewater treatment unit which was significantly improved in July of 1987 by replacing surge pond and API separator (p. J-7). SL 025816 Mr. Stanley Meiburg May 20, 1992 Page 2 Response: SL 025817 A correlation of production rates and emission rates is presented below for each source type contained in the Enforceable Commitment. Storage Tanks are used at the site to store raw materials, intermediates, and final products prior to use or transport offsite. The emissions from these units are primarily attributable to working losses, which is a function of tank turnovers. As production increases the use of raw material and products increases the number of tank turnovers and working losses. Loading and Unloading Emissions - by the same reasoning presented above, the more raw material used and final products shipped from the site the more materials which must be loaded and unloaded from barges and railcars. Consequently, these emissions are directly related to production. Wastewater Emissions Increased production increases the amount of water used at the site for cleaning and process activities. Under past practices the amount of wastewater generated at a site was directly tied to the amount of water used which was tied to production rate. Current practices have changed the water use patterns and more water is recycled, but this did not occur in the base year. Process Vents - Increasing the production rate of a unit means that more raw material are processed. Increased throughput effects all components of the unit including emissions. From this simple review, it is clear that an increase in production would lead to an increase in emissions. However, PPG did not select the peak production year as the base year, but rather opted for the only pre-control year available, 1987. The Early Reduction regulation requires PPG to provide evidence that the base year emissions are not 'Artificially or Substantially" greater than emissions in other years. The meaning of the phase "Artificially or Substantially" is given as follows: "Artificially or Substantially greater emissions means abnormally high emissions such as could be caused by equipment malfunctions, accidents, unusually high production or operating rates compared to historical rates, or other unusual circumstances." Mr. Stanley Meiburg May 20, 1992 Page 3 In response to the above requirement, PPG has used production rates to demonstrate that 1987 is not an unusually high production year tor the reasons stated above. Request # 2. For the surge pond taken out of service on June 28,1987, PPG has claimed unweighted HAP emissions of 543 tons for the first half f 1987. This figure is based on mass balance calculations provided in the application. However LDEQ files include data submitted by Mr. Andy Plauch6 of PPG in 1986 which claimed annual emissions from the surge pond of 492 tons which would prorate to 246 tons half a year. Please explain the discrepancy. Response: The surge pond emissions were first estimated in 1979 to be 356 tons/year by material balance calculations. The flow rate through the pond was 500 gpm and the inlet and outlet organic concentrations of the water were 429 ppm and 104 ppm. The surge pond emissions were estimated in 1982 to be 492 tons based on an extrapolation of 1979 analytical material balance data and an increase in the flow rate to 835 gpm. The flow rate to the pond increased from 1979 to 1982 due to the startup of the new vinyl chloride plant No. 2 and new process pads that were installed in the plant. Mr. Plauchfe reported in a letter to Mr. Gus Bodungen of the Louisiana Department of Environmental Quality (May 23, 1986) that the waste treatment unit surge pond emissions were 492 tons using the 1982 emissions as the basis for the estimate. This letter informed the LDEQ that PPG was going to eliminate the surge pond and API separator emissions. The surge pond was taken out of service on June 28, 1987 and the estimated unweighted HAP emissions of 543 tons for the first half of 1987 reported in the enforceable commitment report were based on material balance data from 1986-1988 as referenced in the enforceable commitment. The flow rate to the surge pond in 1987 was 792.5 gpm with an inlet organic concentration of 1057 ppm and an estimated outlet organic concentration of 425 ppm. The organics concentration in the water to the pond from 1979 to 1987 increased due to reducing the number of pure water streams entering the process sewers. SL 025818 Mr. Stanley Meiburg May 20, 1992 Page 4 Request # 3. For the API separator taken out of service June of 1987, PPG claimed unweighted HAP emissions of 119 tons for the first half of 1987. This figure Is also inconsistent with emissions data previously submitted to LDEQ by PPG, which claimed 30 tons per year emissions for the API separator. Please explain the discrepancy. The above noted discrepancies affect about 50% of the Waste Treatment Unit baseline emissions. Waste Treatment Unit emissions represent about 55% of the total Early Reduction Source. Response: The emissions for the API separator for 1987 were based on Dr. Shen's model as referenced in the enforceable commitment. The estimated emissions of 119.4 tons for the first 6 months of 1987 were based on an API separator outlet concentration of 1054 ppm. In the Shen model, the vapors released to the atmosphere are directly proportional to the concentration of organics in the separator. Initial PPG estimates in 1979 of the organic emissions to the air from the API separator were 107 tons/year based on solar radiation calculations. The organic concentration of the wastewater stream leaving the API separator in 1979 was 597 ppm. Mr. Plauch6 reported a 30 tons/year emission reduction in 1986 to the LDEQ based on the fact that the separator was partly covered with a wooden cover. The wooden cover was badly deteriorated and was removed prior to the shutdown of the separator in 1987. The estimated losses in 1987 are higher than the original estimate of 107 tons/year because the organics in the separator were nearly double the values in 1979. Request # 4. The submittal states that the PPG defines the source as "Activities directly associated with the production of SOCMI chemicals that occur within the contiguous property boundary, excluding all hazardous air pollutant (HAP) emissions from equipment leaks." Based on your definition of source, are all emission points of all HAPs accounted for in your submittal? Response: All emission points of all HAPs are not included in the PPG source definition. PPG defines the "source" for the Lake Charles facility as follows: Mr. Stanley Meiburg May 20, 1992 Page 5 Activities within the contiguous property boundary which will be subject to regulation under the Hazardous Organic NESHAP(HON), directly associated with the handling of raw materials, the handling, production or transport of intermediate and final products, and wastes of SOCMI chemicals, excluding all hazardous air pollutants (HAP) emissions from equipment leaks and non-SOCMI production units in operation at the facility. These activities are strictly limited to the those SOCMI chemical production units which are in operation prior to proposal of the HON. Included under this definition are all points of emissions associated with the following list of activities: Raw Materials Transport and Storage Intermediate Product Storage and Handling Final Product Storage and Handling Waste Handling The specific SOCMI production units present on-site at the time of this filing includes: Chlorine Ethyl Chloride (EC)/Hydrogen Chloride (HCI) Ethylene Dichloride (EDC) Perchloroethylene/Trichloroethylene (PER/TRI) Shipping/Loading Operations Tri-Ethane II* (Methyl Chloroform, MC) Vinyl Chloride (VCM-II) Vinylidene Chloride (VDCM) Waste Treatment Unit (WTU) Not included under this definition are activities and HAP emissions associated with: On-site Power Generation Caustics Processing Silicas Plant SL 025820 Mr. Stanley Meiburg May 20, 1992 Page 6 This definition meets the regulatory requirements outlined under Section 63.73 (a)(1) as it addresses: A portion of an entire contiguous facility under common ownership or control, Activities defined by a standard under Section 112 (d) of the Act. Request #5. In Table 2-1, Emission Point Description, where plural of "vents," "tanks," "trucks," etc. is used, please indicate the numbers of vents, tanks, trucks, etc. Additionally, in place of * where no EIQ number exists, please assign vour own identifying number. Response: Review of EIQs shown in Table 2*1 identified 17 sources that include more than one emission source that is routed through a single vent location. Table 1 shows the vents that include multiple emission sources. The number of trucks was not used to calculate emissions from vacuum trucks. The calculation was based on an estimate of the number of hours that loading of organics and contaminated water into trucks occurred because the loading operation resulted in the release of emissions. An emission factor in Ib/hr had been developed based on test data collected from the vacuum truck vent. The calculation of vacuum truck emissions is found on pages J-30 and J-31 of the EC document. Shipping and loading emissions from ships, barges, tank trucks, railcars, and drums were not calculated by unit. The emissions were calculated using the following equation: E = 5J5 x IQ'6 S P M G T SL 025821 where, G* M= P= T= s= Annual volume of liquid loaded (gal/yr) Molecular weight of the HAP (Ib/lb-mole) True vapor pressure of the HAP loaded (psia) Temperature of liquid loaded, eR or ("F + 460) Saturation Factor Mr. Stanley Meiburg May 20, 1992 Page 7 The equation used to determine an emission factor as shown above is from Volume I of Procedures for Establishing Emissions for Early Reduction Compliance Extensions (EPA-450/3-9l-0l2a). The annual volume of each HAP loaded into drums, ships, barges, railcars, and tank trucks is shown on the emissions calculation form in Section F of the Enforceable Commitment, page F-15 through F*57. The total volume loaded is also shown in the attached Table 2. Ethyl Chloride (EC) loading emissions from railcars and tank trucks were calculated separately from the other shipping and loading emissions. Detailed data on the loading procedure had been compiled by PPG and was used to calculate emissions from EC loading. The emission calculations are presented on pages F-il to F-12 of the document. In response to the second part of question 5, the asterisk used in the table was footnoted by saying all fugitive emissions from the PPG facility are reported under EIQ 349. Table 2*1 has been revised and a unique EIQ number has been assigned to all emission sources, including fugitive emissions from drums (EIQ 394), tank trucks (EIQ 393), railcars (EIQ 392), barges (EIQ 391), and ships (EIQ 390). Request # 6. The base year submittal requires that supporting basis for each emission number of each emission point include: (a) For test results submitted as the supporting basis, a description of the test protocol followed, any problems encountered during the testing, and a discussion of the validity of the method for measuring the subject emissions; and (b) For calculations based on emission factors, material balance, or engineering principles and submitted as the supporting basis, a step-by-step description of the calculations, including assumptions used, and a brief rationale for the validity of the calculation method used. SL 025822 Mr. Stanley Meiburg May 20, 1992 Page 8 We find that PPG's submittal is inadequate in this regard for several emission points. As an example, C-13, the following information is needed: (1) What is the "source1'? (2) How was the process flow obtained? (3) How was the method of concentration calculated? If not an EPA method, give a brief justification and provide supporting calculations. (4) What was the "HAP* stream concentration? "Attachment r does not provide "C". (5) What are the numbers that go in the brackets to obtain 91.153 Mg/yr of uncontrolled emissions? (6) What are the numbers that go in the brackets to obtain 5.239 Mg/yr of HAP emissions? (7) What is the basis for the numbers submitted in Attachment III? (8) To facilitate review, please substitute real names and HAP amounts instead of "See Attachment....". Please review all calculations with these comments in mind and make corrections as necessary. Response: SL 025823 PPG initiated a conference call on April 7,1992 with EPA Region 6, EPA OAQPS, the LDEQ, and ENSR, during which appropriate responses to the items in Question 6 were discussed. EPA and LDEQ concurred that a single set of calculation forms could be used for process vents that emitted multiple HAPs. The "sample* calculation form needed to be completely filled out. A separate worksheet could be used to show the results of calculations for the other HAPs emitted from the vent. Based on the recommendations of EPA and LDEQ during the call, PPG has revised the emission calculation forms as follows: Item (1) - What is the "source"?. The PPG facility is comprised of several distinct production units (e.g., ethyl chloride) and common activity units (e.g., waste treatment unit). Since the definition of source discussed in Question 4 includes only those activities subject to regulation under HON, PPG elected to define source on each process vent calculation form as the HON "subunit" in which the Mr. Stanley Meiburg May 20, 1992 Page 9 SL 025824 emission point is located. For example, EIQ 363, the PER/TRI BLM Tank No. 2, is located in PER/TRI HON subunit. M; lt$(n (2) - How was the process flow obtained? `4* For the example cited on page C-13 of the January 1992 document, the flow rate was calculated using process design specification data. In several cases, specific process knowledge and SOPs were used to calculate flow data. Item (3) How was the method of concentration calculated? If not an EPA method, give a brief justification and provide supporting calculations. For the page C-13 example, the emission rate was calculated based on the mass balance of materials. Item (4) - What was the "HAP" stream concentration? 'Attachment I* does not provide *C\ Attachment I was originally intended to show the results of emission calculations from all HAPs emitted from a process vent. The attachment, however did not always show all input data included on the sample calculation form. Attachment I has been revised for all process vents to include all the variables used in the process vent emission calculation equation. Item (5) - What are the numbers that go in the brackets to obtain 91,153 Mg/yr of uncontrolled emissions? As mentioned, a sample calculation form has been completed for a HAP emitted from that vent. The data on the sample calculation sheet shown in Attachment I can be directly input to the brackets of the equation to determine emissions. Item (6) - What are the numbers that go in the brackets to obtain 5.239 Mg/yr of HAP emissions? Please see the answer to Question 5. Mr. Stanley Meiburg May 20, 1992 Page 10 Item (7) - What is the basis for the numbers submitted in Attachment III? The use of Attachments II and III has been eliminated. The HCI and EC emissions for EIQ 304 presented on page C-13 of the January 1992 report was calculated based on mass balance. Item (8) - To facilitate review, please substitute real names and HAP amounts instead of "See Attachment....". All HAPs emitted from a process vent are listed below the source entry line or, if only a single HAP is emitted, on the HAP entry line on the process vent form. The total for the specific HAP, and the total emissions for all HAPs is included on the process vent form and in Attachment I. Request # 7. In example on B-16, where EPA Test Methods were used, please describe any problems encountered during testing. If none, state so. This applies to all instances where this was omitted. Response: On each of the process vent forms, an answer has been provided as requested. As an example, on page B-16 the answer supplied was "none identified." Request # 8. HAP emissions based on "Emergency" situations cannot be included in the base year emissions. See D-13. This applies to ail instances where "Emergency" emissions were used. Response: The "emergency" mode occurs when emissions that would normally vent to a specific location are diverted through an alternate vent. The "emergency" vent emissions occur when process conditions or equipment reach a preset action level as defined in the process safety design, and emissions are vented to a scrubber. These releases were redefined as "non-routine" releases in the revised EC document. The actions that cause "non-routine" releases do not result in operating unit shutdown. Emissions resulting in incinerator and process unit shutdowns (pumps, compressors, reactors, etc.) are not included in the base year emission calculations. These releases are reported under CERCLA and SARA release reporting requirements. Mr. Stanley Meiburg May 20, 1992 Page 11 Request # 9. The emission reductions from scrubber for EDC Process Unit (EIQ 300 and 301 Table D-2) when compared to 1987 base year data do n t tally with the 99.99% control shown in the report. Response: The values reported for 1994 are the non-routine emissions. EIQ 300 and 301 have three scenarios (non-routine, startup and shutdown) and in 1987 had a scrubber for emission control. These vents are to be incinerated in 1994 at an efficiency of 99.99%. However, only the startup and shutdown scenarios will be incinerated leaving the non-routine emissions to be vented through the scrubber. In general, when a vent having the three scenarios of non-routine, startup and shutdown is to be incinerated, only its startup and shutdown scenarios will be incinerated. The non-routine emissions will not be incinerated. In addition to EIQ 300 and 301, EIQ 302C is controlled in this manner. Therefore, the 1994 emissions reported for EIQ 302C also reflect the non-routine emissions from that vent. Detailed calculations are included as an attachment to this letter. Request #10. The emission reductions from Higher Efficiency Scrubber for Chlorine Manufacturing Unit (EIQ 101 Table B-2) when compared to 1987 base year data do not tally with the 99.99% control shown in the report. Response: The reported emissions are correct, however, the control efficiencies shown on Tables B-1 and B-2 are reported incorrectly. The controlled chlorine emissions in 1987 were the following: Uncontrolled emissions equaled 4.652 Mg/yr (see page B-17). The control efficiency in 1994 will be 99.9%. The emissions in 1994 will therefore be: 4.652 x (1 - 0.999) = 0.005 Mg/yr Request #11. For all the HAPS listed, please include CAS numbers. Response: Table 3 lists all the CAS numbers for each of the HAPs reported in the Enforceable Commitment document. SL 025826 Mr. Stanley Meiburg May 20, 1992 Page 12 Request #12. For LDEQ to verify permitted emissions for the 1987 base year, please submit a list of permits issued, their numbers, date of issuance and a new to old EIQ number cross reference. Response: A list of permits and a new to old EIQ reference are shown in Table 4. PPG looks forward to participating in EPA's Early Reduction Program. Should there be any further questions, please feel free to contact me at (318) 491-4823. Very truly yours, Dave Angell Works Director Environmental Assurance DA/mm:5510-016-114/5510L016.002 Attachments cc: Chris Roberie, Acting Division Administrator Air Quality Compliance Division Louisiana Dept, of Environmental Quality, Baton Rouge David Beck, OAQPS Emissions Standards Division (MD-13) Research Triangle Park, NC SL 025827 EIQ No. 310 312 313 315 324 Unit TE-II EDC EDC TE-II TE-II 325 PER/TRI 327 PER/TRI 328 PER/TRI 330 PER/TRI 331 PER/TRI SL 025828 TABLE 1 EIQ DESCRIPTIONS Vent Description DCE Tank Vents LP-EDC Process Tanks No. 1 North Dock EDC Tank EDC Crude and Storage MC Process Storage MC Dock Storage Per Dock Storage Per Process Storage Tri Dock Storage Tri Process Storage Tank Description No. 1 DCE Storage Tank No. 2 DCE Storage Tank EDC Bottom Storage Tank No. 2 EDC Bottom Storage Tank No. 4 No. 1 Dock EDC Tank No. 2 Dock EDC Tank No. 1 OHC Product Tank No. 2 OHC Product Tank No. 1 OHC Crude Storage Tank No. 2 OHC Crude Storage Tank No. 1 DOL/SBL Tank No. 2 DOL/SBL Tank DOL/DOX SBL Tank S-1 Tank S-2 Tank S-3 Tank S-4 Tank No. 1 Day Tank No. 2 Day Tank No. 3 Day Tank No. 4 NRE Tank No. 1 Triethane Dock Storage Tank No. 2 Triethane Dock Storage Tank No. 3 Triethane Dock Storage Tank No. 1 Per Dock Tank No. 2 Per Dock Tank No. 3 Per Dock Tank DG 3 Per 232 Batch Tank DG 4 Per 232 Batch Tank No. 1 DG Per Stab. Tank No. 2 DG Per Stab. Tank Per 232 Shipping Tank No. 1 Per Stab. Tank No. 2 Per Stab. Tank TRI-Dock Storage Tank No. 1 TRI-Dock Storage Tank No. 2 TRI-Dock Storage Tank No. 3 No. 1 HP Stab. Tank No. 2 HP Stab. Tank No. 1 TRI Stab. Tank No. 2 TRI Stab. Tank A-1 EIQ No. 333 338 344A 348B 360 369 375 Unit WTU EC WTU WTU PER/TRI Chlorine WTU TABLE 1 (Cont'd) EIQ DESCRIPTIONS Vent Description Tank Description i Per/Tri Feed Tanks Area Bottoms Tank No. 1 Area Bottoms Tank No. 2 HCI Tails Tower Scrubber No. 1 HCI Add Tank No. 2 HCI Add Tank Weak No. 1 HCI Acid Tank Weak No. 2 HCI Acid Tank | Bottoms Plant Tank Bottoms Plant Feed Tank No. 1 Bottoms Plant Product Tank No. 1 Bottoms Plant Product Tank No. 2 Bottoms Plant Product Tank No. 3 Sludge Box Incinerator Tanks Scrubber WTU Surge Tank No. 1 WTU Surge Tank No. 2 WTU Settling Tank No. 1 WTU Settling Tank No. 2 Per/Tri Still Line Tank No. 1 Still Line Feed Tank No. 2 Still Line Feed Tank No. 1 Aux Line Feed Tank No. 2 Aux Line Feed Tank No. 3 Aux Line Feed Tank No. 4 Aux Line Feed Tank No. 5 Aux Line Feed Tank No. 6 Aux Line Feed Tank No. 7 Aux Line Feed Tank No. 8 Aux Line Feed Tank No. 9 Aux Line Feed Tank No. 10 Aux Line Feed Tank Heavies Still Feed Tank No. 1 Per/Tri Bottoms Tank No. 2 Per/Tri Bottoms Tank TCE Storage Tank Per/Tri Bottoms Tank No. 1 Per/Tri Bottoms Tank No. 2 Dowtherm 'A' Make-up Tank Dowtherm Recyde H20 Recovery No. 1 HCI Add Storage Tank No. 1 HCI Storage Tank Scrubber No. 2 HCI Storage Tank HCI Add Formate Destruction HCI Add Tank (Sodium Formate Destruction) Combination of Sewers HCI Acid Tank Weak HCI Acid Tank SL 25829 A-2 SL 025830 Name Chloroethane (Ethyl Chloride) 1,2-Dlchloroethane Methylene Chloride Perchloroethylene Trichioroethylene Methyl Chloroform EC EDC MeCI2 PER TRI MC TABLE 2 CHEMICAL PRODUCTION RATES Drums gal/yr 0.0 2677.0 1629.0 10556.0 58763.0 237734.7 Annual Volume Loaded Tank Truck gal/yr Tank Cars gal/yr Barges gal/yr 1434393.0 5452482.0 0.0 706883.0 187686.0 12219254.0 145810.0 0.0 0.0 618706.0 2117044.0 2125293.0 796673.0 1683653.0 583519.0 1872179.9 3520965.6 2897367.7 Ships gal/yr 0.0 1777361.0 0.0 1994353.0 1326619.0 6297957.2 A-3 TABLE 3 LIST OF HAP CHEMICALS CAS No. 56-23-5 67-66-3 67-72-1 71-55-6 74-67-3 75-00-3 75-01-4 75-09-2 75-34-3 75-35-4 79-00-5 79-01-6 79-34-5 79-46-9 87-68-3 92-52-4 106-46-7 106-88-7 107-06-2 108-88-3 108-90-7 118-74-1 123-91-1 127-18-4 7439-97-6 7647-01-0 7782-50-5 SL 025ft*n HAPs Carbon Tetrachloride Chloroform Hexachloroethane Methyl Chloroform Methyl Chloride Ethyl Chloride (Chloroethane) Vinyl Chloride Methylene Chloride 1,1-Dichloroethane Vinylidine Chloride 1,1,2-Trichloroethane Trichlorethylene 1.1,2,2-Tetrachloroethane 2-Nitropropane Hexachlorobutadiene Biphenyl 1,4-Dichlorobenzene 1,2 Epoxy Butane (Butylene Oxide) Ethylene Dichloride (1,2 Dichloroethane) Toluene Chlorobenzene Hexachiorobenzene 1,4 Dioxane Perchloroethylene Mercury Hydrogen Chloride Chlorine Acronym CCI4 CHCI3 HEXA MC MECI EC VC MECI2 DCE VDC TCE TRI SYM NTE HCBD BIPHEN 1,4 DICH BLM EDC TOL C6H5Q HCB DOX PER Hg HCI CI2 TABLE 4 LIST OF EXISTING AIR QUALITY PERMITS AND EIQ CROSS-REFERENCE NUMBERS New EIQ 100 101 102 103 105 106 107 109 128 130 300 301 302 302A 302C 302D 303 304 305 306 307A 307B 308 309 310 311A Old EIQ 56 57 58 89 7-73 3-80 4-80 2-80 -- -- 20 22 -- 24 -- -- 26 36 4-74 3-76 3-78A 3-78B 33 1-86 2-74 68 Permit No. Permit Date G.f. G.f. G.f. G.f. 290 1430T 1430T 1430T None None 2105 2105 2105 923T 923T None G.f. ! G.f. -- -- -- -- 2/74 9/80 9/80 9/80 -- Exemption 11/91 12/91 12/91 12/91 4/78, consolidated into EIQ 302, Permit No. 2105, 12/91 4/78, consolidated into EIQ 302, Permit No. 2105, 12/91 consolidated into EIQ 302, Permit No. 2105, 12/91 -- 442 4/75, revised 7/78 698 2/77 897 2/78 897 2/78 923T 4/78 1929 5/86 j 442 j 4/75. revised under 1 1154T. 5/79 G.f. 1 SL 025832 TABLE 4 (Cont'd) UST OF EXISTING AIR QUALITY PERMITS AND EIQ CROSS-REFERENCE NUMBERS New EIQ 311B 312 313 314 315 316 317 318 319 320 321 322 323 324 Old EIQ -- 69 70 1-74 2-76 72-1 72-6 72-7 72-8 72-9 72-10 72-11 72-12 3-74 325 5-74 326 327 328 329 330 331 332 333 334 335 336 337 SL 025833 108 74 75 109 76 77 80 81 110 87 2-82 32 Permit No. None 1305T G.f. 1305T 698 G.f. G.f. G.f. G.f. G.f. G.f. G.f. G.f. 442 442 G.f. G.f. G.f. G.f. G.f. G.f. G.f. G.f. G.f. G.f. 1658T G.f. Permit Date -- , 12/79, revised 11/80 I 12/79, revised 11/80 | 2/77 -- -- -- ... -- -- -- 4/75, revised 7/78, j revised 4/79, revised in permit 1154T 5/79 | ------------------------------ 1 4/75. revised 7/78, revised in permit ---------1--1-5--4--T-5-/-7--9---------[ -- ' 1 ! -------------- ----------------1 -------------------------------1 -- --i _ -- \ -- -- 12/81 1 | TABLE 4 (Cont'd) UST OF EXISTING AIR QUALITY PERMITS AND EIQ CROSS-REFERENCE NUMBERS New EIQ 338 339 340 341 342 343 344A 344B 345 346 347 348A 3488 353 355 356 357 358 359 360 361 362 363 365 369 370 371 373 374 375 Old EIQ 38 78 90 11-78 79 1-80 83 83 1-75 1-77 1-78 3-83 -- -- -- -- -- -- -- -- -- ** -- ** -- -- -t Permit No. G.f. G.f. G.f. None assigned G.f. 1476T G.f. 2040 2040 2040 897 2040 G.f. G.f. None None None None None None None None None None None None None None None None Permit Date -- -- -- 2/79 -- 11/80 -- 12/90 12/90 12/90 2/78 12/90 1 ' -- -- -- _-- -- -- -- -- ... ... ... _ TABLE 4 (Cont'd) LIST OF EXISTING AIR QUALITY PERMITS AND EIQ CROSS-REFERENCE NUMBERS New EIQ 376 377 380 381 382 383 384 385 386 387 388 389 390 391 392 393 394 G.f. - Grandfatfwr pwrmM ttotus. Old EIQ -- -- -- -- -- -- -- -- -- -- -- -- -- -- -- -- Permit No. None None None None None None None None None None None None None None None None None Permit Dat -- -- -- -- -- -- -- j 1 -- -- ... -- -- -- SL 025835 RESPONSE TO QUESTION 9 SL 025836 RESPONSE TO QUESTION 9 As explained in the response to Question 9, the reported emissions for EIQ 300 and 301 in 1994 when compared to 1987 base year date do not tally with the 99.99%. Control shown in the report, because the non-routine emissions will not be incinerated in 1994. Detailed calculations are as follows: SL 025837 Emission EIQ 300,1987; EC 0.015 EDC 0.068 HCI 0.147 EIQ 300,1994; EC EDC HCI 0.015 0.058 0.147 Non-Routine Percent Control Controlled Emission Emission Stsrt-Up Psrcsnt Control Controlled Emission 5.0 0.01425 0.002 5.0 0.0019 5.0 0.0551 0.087 5.0 0.0826 99.0 0.00147 0.003 99.0 0.000 0.071 0.0845 EIQ 300, TOTAL EMISSIONS (1987) = 0.1785 Mg/yr 5.0 0.01425 0.002 99.99 0.00 5.0 0.0551 0.087 99.99 0.00 99.0 0.00147 0.003 99.0 0.00 0.071 0.00 EIQ 300, TOTAL EMISSIONS (1994) = 0.071 Mg/yr Emission 0.00 0.024 0.00 0.00 0.024 0.00 Shut-Down Percent Control Controlled Emission 5.0 0.00 5.0 0.023 99.0 0.00 0.023 99.99 99.99 99.0 0.00 0.00 0.00 0.00 RESPONSE TO QUESTION B (CONTD) Emission EIQ 301,1967; EC EDC HO 0.157 0.487 0.236 EIQ 301,1994; EC EDC HCI 0.157 0.487 0.236 Non-Routine Psrcsnt Control Controlled Emission Emission Stsrt-Up Percent Control Controlled Emission 5.0 0.149 0.014 5.0 0.0133 5.0 0.4626 0.562 5.0 0.534 99.0 0.00236 0.021 99.0 0.0002 0.614 0.5495 EIQ 301, TOTAL EMISSIONS (1967) = 2.273 Mg/yr 5.0 0.149 0.014 99.99 0.0 5.0 0.4626 0.562 99.99 0.0001 99.0 0.00236 0.021 99.0 0.0 0.614 0.0001 EIQ 301, TOTAL EMISSIONS (1994) = 0.614 Mg/yr Emission 0.0 1.17 0.0 0.0 1.17 0.0 Shut-Down Percent Control Controlled Emission 5.0 0.0 5.0 1.111 99.0 0.0 1.111 99.99 99.99 99.0 0.0 0.0 0.0 0.0 a in PPG Industries, Inc. Lake Charles, Louisiana Enforceable Commitment Volume I: General Distribution ENSR Consulting and Engineering Submitted January 1992 Revised May 1992 Document Number 5510-016-114 CONTENTS CERTIFICATE OF ENFORCEABLE COMMITMENT ........................................................... 1 1.0 INTRODUCTION ...............................................................................................................1-1 1.1 Overview ................................................................................................................... 1-1 1.2 Report Organization ................................................................................................. 1-3 2.0 SOURCE DEFINITION ..................................................................................................... 2-1 2.1 Process Unit Description.......................................................................................... 2-4 2.2 Hazardous Air Pollutant (HAP) Emission Sources..................................................2-6 3.0 BASE-YEAR SELECTION................................................................................................. 3-1 4.0 EARLY REDUCTION DEMONSTRATION ...................................................................... 4-1 4.1 Emissions Summary................................................................................................. 4-1 4.2 Emission Reduction Strategy................................................................................... 4-3 5.0 GLOSSARY OF ABBREVIATIONS ............................................................................. 5-1 APPENDICES A FACILITY DESCRIPTION....................................................................................... A-1 B CHLORINE PROCESS UNIT ..................................................................................B-1 B.1 Process Description.....................................................................................B-1 B.2 1987 Base-Year Emissions......................................................................... B-1 B.3 Emissions Reduction Strategy.................................................................. B-1 B.4 Post-Reduction Emissions......................................................................... B-6 B-A CHLORINE PROCESS UNIT STORAGE TANK CALCULATIONS .....................B-8 B-B CHLORINE PROCESS UNITPROCESS VENT CALCULATIONS ................... B-14 C ETHYL CHLORIDE PROCESS UNIT (EC) AND HYDROGEN CHLORIDE PROCESS UNIT (HCL) C.1 Process Description.................................................................................... C-l C.2 1987 Base-Year Emissions......................................................................... C-5 C.3 Emissions Reduction Strategy .................................................................. C-5 5510R016.01 ny 25840 i Final 05/27/92 CONTENTS (Cont'd) EN3I APPENDICES (Cont'd) C.4 Post-Reduction Emissions......................................................................... C-5 C-A EC PROCESS UNIT STORAGE TANK CALCULATIONS..................................... C-9 C-B EC PROCESS UNIT PROCESS VENT CALCULATIONS................................... C-15 D ETHYLENE DICHLORIDE PROCESS UNIT (EDC) D.1 Process Description.....................................................................................D-l D.2 1987 Base-Year Emissions......................................................................... D-4 D.3 Emissions Reduction Strategy ...................................................................D-4 D.4 Post-Reduction Emissions......................................................................... D-7 D-A ETHYLENE DICHLORIDE PROCESS UNIT STORAGE TANK CALCULATION D-9 D-B EDC PROCESS UNIT PROCESS VENT CALCULATIONS ........................... D-15 E PERCHLOROETHYLENE/TRICHLOROETHYLENE PROCESS UNIT (PER/TRI) E.1 Process Description.....................................................................................E-1 E.2 1987 Base-Year Emissions..........................................................................E-4 E.3 Emissions Reduction Strategy...................................................................E-4 E.4 Post-Reduction Emissions......................................................................... E-4 E-A PERCHLOROETHYLENE/TRICHLOROETHYLENE PROCESS UNIT STORAGE TANK CALCULATIONS ...................................................................................... E-8 E-B PER/TRI PROCESS UNIT PROCESS VENT CALCULATION .......................E-22 F SHIPPING AND LOADING PROCESS UNIT (S/L) F.1 Process Description..................................................................................... F-1 F.2 Base-Year Emissions...................................................................................F*1 F.3 Emissions Reduction Strategy...................................................................F-1 F.4 Post-Reduction Emissions..........................................................................F-4 F-A SHIPPING AND LOADING UNIT PROCESS VENT CALCULATIONS................ F-6 F-B SHIPPING AND LOADING UNIT FUGITIVE EMISSIONSCALCULATIONS . . F-14 5510H016.01 SL 025841 ii Final 05/27/92 CONTENTS (Cont'd) ENSR APPENDICES (Cont'd) G TRI-ETHANE* II PROCESS UNIT (TE-II) G.1 Process Description....................................................................................G-1 G.2 1987 Base-Year Emissions.........................................................................G-7 G.3 Emissions Reduction Strategy ..............................................................G-11 G.4 Post-Reduction Emissions.....................................................................G-11 G-A TRI-ETHANE* II PROCESS UNIT STORAGE TANKCALCULATIONS..........G-14 G-B TRI-ETHANE* II PROCESS UNIT PROCESS VENTCALCULATIONS..........G-26 H VINYL CHLORIDE PROCESS UNIT (VCM-II) H.1 Process Description....................................................................................H-l H.2 1987 Base-Year Emissions.........................................................................H-5 H.3 Emissions Reduction Strategy ..................................................................H-5 H.4 Post-Reduction Emissions............................................................... H-5 H-A VINYL CHLORIDE UNIT PROCESS VENT CALCULATIONS............................ H-9 I VINYUDENE CHLORIDE MONOMER PROCESS UNIT (VDCM) I.1 Process Description.................................................................................. 1-1 1.1.1 VDCM Section........................................................................... l-i 1.1.2 Transdichloroethylene Section ................................................ 1-4 1.2 1987 Emissions........................................................................................ 1-4 1.3 Emissions Reduction Strategy ............................................................... 1-4 1.4 Post-Reduction Emissions...................................................................... 1-8 l-A VINYUDENE CHLORIDE MONOMER PROCESS UNIT (VDCM) STORAGE TANK CALCULATIONS .................................................................................... 1-10 l-B VCDM PROCESS UNIT PROCESS VENT CALCULATIONS.......................... 1-16 J WASTE TREATMENT UNIT (WTU) J.1 Process Description.................................................................................... J-1 J.1.1 Bottoms Recovery Section..........................................................J-1 J.1.2 Waste Treatment Section ............................................................J-7 J.1.3 Chloropivaloyl Chloride (CPC) Section....................................... J-8 J.1.4 Base-Year Wastewater Treatment Fugitive Emissions............ J-9 J.1.4.1 Surge Pond Description................................................ J-9 J.1.4.2 Surge Pond Emission Calculations..............................J-9 5510noi6.01 SL 025842 jjj Final 05/27/92 CONTENTS (Cont'd) ENSR APPENDICES (Cont'd) J.1.4.3 Surge Pond Emissions Summary........................... J-19 J. 1.4.4 API Separator Air Emissions ..................................J-19 J. 1.4.5 North Classifier Air Emissions ................................ J-24 J. 1.4.6 Lift StationAir Emissions.............................................J-30 J.1.4.7 Vacuum Truck Air Emissions.....................................J-27 J.2 1987 Base-Year Emissions........................................................................ J-31 J.3 Emissions Reduction Strategy ................................................................. J-31 J.4 Post-Reduction Emissions........................................................................ J-35 J-A HAPS INLET CONCENTRATIONS ..................................................................... J-37 J-B HAPS OUTLET CONCENTRATIONS .................................................................J-46 J-C AVERAGE FLOW RATE TO THE SURGE POND...............................................J-51 J-D SLUDGE ANALYSIS ............................................................................................J-53 J-E ASPEN PLUS MODEL RUN RESULTS.............................................................. J-55 J-F JUSTIFICATION OF HAP CONCENTRATION IN WATER PHASE DUE TO SLUDGES IN POND ...........................................................................................j-57 J-G DR. THOMAS SHEN'S PAPER................... J-59 J-H TEMPERATURES AND WIND SPEEDS FOR LAKE CHARLES FOR 1987 . . J-64 J-l WASTE TREATMENT UNIT STORAGE TANK CALCULATIONS ......................J-66 J-J WASTE TREATMENT UNIT PROCESS VENT CALCULATIONS ......................J-82 5510R016.01 SL 025843 IV Final 05/27/92 LIST OF TABLES 2- 1 Emission Point Descriptions........................................................................................... 2-8 3- 1 Production Rate ............................................................................................................. 3-2 4- 1 Early Reductions Emission Summary........................................................................... 4-2 4-2 Strategy to Achieve Emissions Reductions.................................................................. 4-4 4-3 Vapor Pressure of Pollutants .......................................................................................4-10 A-1 Common Hydrocarbon Compounds Found in Plant B................................................A-3 B-1 1987 Base-Year Emissions Chlorine Manufacturing...................................................B-4 B-2 Emissions Reductions Strategy and Post-Reduction Emissions - Chlorine Manufacturing................................................................................................................ B-5 B-3 HAP Emissions Summary - Chlorine Process Unit....................................................... B-7 C-1 1987 Base-Year Emissions Ethyl Chloride Process Unit (EC)/Hydrogen Chloride Process Unit (HCI)............................................................ C-6 C-2 Emissions Reductions Strategy and Post-Reduction Emissions - Ethyl Chloride Process Unit (EC)/Hydrogen Chloride Process Unit (HCI).......................................C-7 C-3 HAP Emissions Summary - Ethyl Chloride Process Unit (EC)/Hydrogen Chloride Process Unit (HCI) ..........................................................................................C-8 D-1 1987 Base-Year Emissions - Ethylene Dichloride Process Unit (EDC)....................... D-5 D-2 Emissions Reductions Strategy and Post-Reduction Emissions - Ethylene Dichloride Process Unit (EDC)..................................................................................... D-6 D-3 HAP Emissions Summary Ethylene Dichloride Process Unit (EDC)......................... D-8 E-1 1987 Base-Year Emissions - Per/Tri Process Unit (Per/Tri) ....................................... E-5 E-2 Emissions Reductions Strategy and Post-Reduction Emissions - Per/Tri Process Unit (Per/Tri) ................................................................................................... E-6 E-3 HAP Emissions Summary - Per/Tri Process Unit (Per/Tri)......................................... E-7 F-1 1987 Base-Year Emissions Shipping and Loading Process Unit (S/L) ...................F-2 F-2 Emissions Reductions Strategy and Post-Reduction Emissions - Shipping and Loading Process Unit (S/L) ...........................................................................................F-3 F-3 HAP Emissions Summary - Shipping and Loading Process Unit (S/L) ..................... F-5 G-1 1987 Base-Year Emissions - Tri-Ethane* Process Unit (TE-II).................................. G-10 G-2 Emissions Reductions Strategy and Post-Reduction Emissions Tri-Ethane* Process Unit (TE-II)....................................................................................................G-12 G-3 HAP Emissions Summary - Tri-Ethane* Process Unit (TE-II)...................................G-13 H-1 1987 Base-Year Emissions Vinyl Chloride Monomer Process Unit (VCM-II) ..........................................................................................................................H-6 55100016.01 SI* 025844 V Final 06/27/92 LIST OF TABLES (Cont'd) H-2 H-3 M 1*2 1-3 J-1 J-2 J-3 J-4 J-5 J-6 J-7 J-8 J-9 J-10 J-11 J-12 J-13 Emissions Reductions Strategy and Post-Reduction Emissions - Vinyl Chloride Monomer Process Unit(VCM-II).................................................................................... H-7 HAP Emissions Summary - Vinyl Chloride Monomer Process Unit (VCM-II) ............ H-8 1987 Base-Year Emissions Vinylidene Chloride Process Unit (VDCM).................... 1-6 Emissions Reductions Strategy and Post-Reduction Emissions Vinylidene Chloride Process Unit(VDCM)..................................................................................... 1-7 HAP Emissions Summary - Vinylidene Chloride Process Unit (VDCM) ................... 1-9 Representative Average Speciated Inlet Concentrations (ppm) to the Surge Pond ............................................................................................................................ j-12 Average Speciated Outlet Concentrations (ppm) from the Surge Pond.................J-13 Speciated Air Emissions from the Surge Pond from 1/1/87 to 6/28/87 ...............J-16 Speciated HAP Air Emissions from the Surge Pond for the Second Half of 1987 ...................................... J-20 Speciated Air Emissions from the Surge Pond for 1987 ............................................ J-21 Speciated Air Emissions from the API Separator from 1 /I/87 to 6/28/87 ............... J-25 Speciated Air Emissions from the North Classifier for 1987 ......................................J-26 Lift Stations.................................. j-28 Speciated Air Emissions from the Lift Stations with Open Tops for 1987 ........................................................................................................................ j-29 Vacuum Truck Base-Year Emissions ......................................................................... j-32 1987 Base-Year Emissions - Waste Treatment Unit................................................... J-33 Emissions Reduction Strategy and Post-Reduction Emissions - Waste Treatment Unit .............................................................................................................j-34 HAP Emissions Summary - Waste Treatment Unit......................................................J-36 LIST OF FIGURES 2- 1 Topographic Map ...........................................................................................................2-3 2-2 Plot Ran, Production Unit Layout.................................................................................. 2-5 The following are enclosed as Volume II: Confidential A-1 Plant B Chlorinated Organics Production Process Flow Diagram..............................A-5 B-1 Diaphragm - Chlorine and Caustic Production..............................................................B-2 B-2 Mercury - Chlorine and Caustic Production.................................................................. B-3 5510R016.01 0258^5 SL vi Final 05/27/92 LIST OF FIGURES (Cont'd) C-1 EC Process Schematic .................................................................................................. C-2 C-2 Ethyl Chloride..................................................................................................................C-3 C-3 HCI Process Schematic.................................................................................................. C-4 D-1 Uquid Phase EDC Process .........................................................................................D-2 D-2 Ethylene Dichloride (EDC) ..............................................................................................D-3 E-1 Per/Tri Process Schematic ............................................................................................E-2 E-2 Perchloroethylene - Trichloroethylene (Per/Tri) .............................................................E-3 G-1 Tri-Ethane* II Process Schematic................................................................................G-2 G-2 TE-II VCM Section...........................................................................................................G-3 G-3 TE-II 1,1-Dichloroethane Section (DCE)......................................................................... G-5 G-4 TE-II Methyl Chloroform (MC) Section........................................................................... G-6 G-5 OHC-II Process Schematic............................................................................................. G-8 G-6 TE-II OHC Section (EDC Production) ........................................................................... G-9 H-1 VCM-II Process Schematic.......................................................................................... H-2 H-2 VCM-II VCM Section ...................................................................................................... H-3 H-3 VCM-II Uquid Phase EDC and OHC (EDC) Sections...................................................H-4 1-1 VDCM Process Schematic ............................................................................................ 1-2 1-2 Vinylidene Chloride Monomer (VDCM) ........................................................................ 1-3 1-3 Transdichloroethylene Recovery................................................................................... 1-5 J-1 Bottoms Recovery Process Schematic.......................................................................... J-2 J-2A Waste Treatment Process Schematic............................................................................ J-3 J-2B Waste Treatment Process Schematic............................................................................ J-4 J-3 Waste Treatment Unit - Bottoms Plant ..........................................................................J-5 J-4 Chloropivaloyl Chloride - CPC ......................................................................................J*10 5510R018.01 vii FlnaJ 05/27/92 CERTIFICATE OF ENFORCEABLE COMMITMENT PPG Industries, Inc. (PPG) seeks to participate in and receive the benefits of the Early Reductions Program in accordance with 40 C.F.R.63, Subpart D. An Enforceable Commitment has been prepared for the PPG Industries. Inc. facility located in Lake Charles. Louisiana. This report presents the details of the Enforceable Commitment required to demonstrate that a 90 percent reduction in Hazardous Air Pollutants (HAPs) will be achieved by January 1994. The base year selected for the facility is 1987. The "source" is defined as all Synthetic Organic Chemical Manufacturing Industry (SOCMI) activities that occur within the contiguous property boundary of the facility. The 90 percent reduction in HAPs scheduled to occur at the Lake Charles plant prior to January 1. 1994 is derived from this SOCMI source. / I certify, as the Works Director, Environmental Assurance, for PPG Industries, Inc., that to the best of my knowledge the base year emissions presented in this report are accurate, and I acknowledge that these emission numbers are being submitted in response to an EPA request under Section 114 of the Clean Air Act. Furthermore, I commit to achieve before January 1, 1994 the stated post-reduction emission levels at the source. This compliance strategy will provide the 90 percent reduction required to qualify for the compliance extension from the Hazardous Organic NESHAP (HON) Section 112(d) standard. I also acknowledge that this commitment is enforceable as specified in 40 C.F.R.S63, Subpart D. David C. Anoell Name Works Director. Environmental Assurance Title Mav 22. 1992 Date Signed earlier on January 17, 1992 by Richard Rompala, Group Vice President, Chemicals, and submitted to EPA on January 20. 1992. 0258A7 1.0 INTRODUCTION EN31 This report discusses an emission reductions program that will be implemented at the PPG Industries, Incorporated, Chemical Division, (PPG) facility located at Lake Charles, Louisiana. This program commits PPG to achieve a 90 percent reduction in emissions of volatile organic hazardous air pollutants (HAP) by the January 1, 1994 regulatory deadline. This action will qualify PPG for participation in EPA's Early Reduction Program (ERP) in accordance with Title 40, Part 63, Subpart D of the Code of Federal Regulations. By participating in the early reductions program, PPG expects to be granted a six-year extension in the compliance deadline for Maximum Achievable Control Technology (MACT) requirements contained in applicable Section 112(d) standards. Participation in the ERP requires a source to achieve a 90 percent reduction in HAP emissions prior to proposal of a specific regulation, or to file an Enforceable Commitment to achieve the reductions by January 1, 1994. The nature of Synthetic Organic Chemical Manufacturing (SOCMI) operations at the PPG Lake Charles facility will not allow a 90 percent reduction to be realized prior to the expected Hazardous Organic NESHAP (HON) proposal date. HON is expected to be the first Section 112(d) standard to be proposed with MACT standards. Therefore, considering PPG's past efforts and future plans, with respect to emission reduction programs, an Enforceable Commitment is hereby submitted. 1.1 Overview PPG operates a chemical-producing facility in Lake Charles, Louisiana. The facility produces vinyl chloride, ethyl chloride, ethylene dichloride, vinylidene chloride, transdichloroethylene, chlorinated solvents (perchloroethylene, trichloroethylene, methyl chloroform), chlorine, caustic, silica products, and chloropivaloyl chloride. The production of these chemicals at the plant causes a major portion of plant operations to be classified as SOCMI processes. SL 025848 5510ft018.01 1-1 Final 05/27/92 PPG has in recent years initiated several projects to reduce plant-wide HAP emissions. The projects completed to date have achieved emission reductions by instituting process changes, eliminating sources, and through the use of add-on control technology. Furthermore, the PPG Lake Charles facility is currently participating in the following programs: Voluntary program initiated by the Louisiana Department of Environmental Quality (LDEQ) to further reduce HAP emissions; Development and implementation of projects to reduce HAP emissions in response to recent LDEQ rules and future New Source Performance Standards (NSPS) regulating vapor emission from marine loading operations; and The EPA 33/50 Industrial Toxics Project, a part of the overall Pollution Prevention Strategy initiative. The 1990 Clean Air Act Amendments (CAAA) call for the regulation of 189 HAP compounds over the next ten years. The CAAA requires EPA to define specific source categories that emit HAP emissions and develop MACT standards for each source category. This EPA regulatory strategy represents a shift in the focus of air toxic regulations from a compound to an emission source base. The first regulation scheduled for promulgation under Section 112 of the revised Clean Air Act is HON, which will address the SOCMI facilities. The HON regulation will affect PPG because the facility meets the following criteria: Produce one or more of an estimated 150 organic HAPs included in the CAAA list of 189 HAPs as a: primary product co-product, or by-product. Use one or more of an estimated 150 organic HAPs as a reactant. SL 025849 5510R016.01 1-2 Final 05/27/92 EPA anticipates proposing HON early in 1992. Since a majority of the emissions from the PPG Lake Charles plant are generated from SOCMI-related activities, HON will have a significant impact on the SOCMI activities. PPG is committed to reducing emissions in a timely, well planned manner. Because of emission reduction commitments initiated well before and since the 1990 CAAA were promulgated, PPG is in a position to participate in the Early Reduction Program. 1.2 Report Organization This report contains the key components required by the EPA for review of an Enforceable Commitment. The organization of the report is outlined below. Definition of `Source' (Section 2.0); Selection of Base Year (Section 3.0); and Demonstration of 90 percent reduction (Section 4.0 and Appendices). The Appendices accompanying this report include the following: A description of the facility and the process units; A discussion of the calculated base-year emissions; The proposed strategy to reduce base-year emissions by 90 percent; A discussion of the overall emission reductions; and The detailed calculations sheets that support the reported base-year emissions. Each appendix is subdivided into several sections: a summary of emissions from the process unit followed by the detailed calculation forms and worksheets section. In the summary section, a description of the process is given followed by base-year and post-reduction emission estimates. Tables 1 and 2 in each summary section present the emission estimates for the baseyear and post-reduction respectively. Table 3 in each summary section provides the summary of emissions for the subunit. 551OR016.01 SL 025850 1-3 Final 05/27/92 If the process unit contained storage or process tanks that emitted HAPs or separate subsection that discusses storage tank emissions was included in the appendix (Subsection A). This subsection contained a table showing tank emission calculations. A Tank Vent may be a point source for a single tank or a point source for several tanks. In either case, the emissions are calculated separately for each tank emitting through the vent. Total emissions for the Tank Vent is the addition of the emissions from all individual tanks calculated separately. This value is the reported emission estimate under the "HAP Emissions" column on Tables 1 and 2 in the summary section. A list of vapor pressures for pollutants can be found on Table 4-3. A subsection that showed detailed process vent emission calculations was included in each appendix (Subsection B), calculation procedures for process vents are provided. A process vent may have several operational scenarios (non-routine, startup, or shutdown) and usually emits more than one HAP. For each scenario of each process vent, a sample calculation worksheet is provided which shows how the emissions were calculated for one of the HAPs in the vent. Following the sample calculation worksheet, a summary table (Attachment I) showing all HAPs emitted from that vent is provided. Process vents emitting only one HAP are provided with a calculation worksheet for that HAP only and do not have an Attachment I. Some process vents have non-routine scenarios which had no emissions in the base year (1987). These vents are provided with calculation worksheets showing zero for the emissions. The calculation worksheets for these vents only provide information on what HAPs could potentially be emitted. SS10R016.01 SL 025851 Final 05/27/92 2.0 SOURCE DEFINITION ENR The PPG Lake Charles plant manufactures chlorine, chlorinated organics, caustic, and silica products. Intermediate and final organic chemical products manufactured at the facility qualify the plant as a member of the Synthetic Organic Chemical Manufacturing Industry (SOCMI) group defined in Title 40, Part 60, of the Code of Federal Regulations (CFR). For the Early Reduction Program, an applicant must define the source to which the Enforceable Commitment will be binding, using the guidelines in Subpart 0 of 40 CFR 63.73. PPG defines the 'source* for the Lake Charles facility as follows: Activities within the contiguous property boundary which will be subject to regulation under the Hazardous Organic NESHAP (HON), directly associated with the handling of raw materials, the handling, production or transport of intermediate and final products, and wastes of SOCMI chemicals, excluding all hazardous air pollutants (HAP) emissions from equipment leaks and non-SOCMI production units in operation at the facility. These activities are strictly limited to the those SOCMI chemical production units which are in operation prior to proposal of the HON. Included under this definition are all known points of emissions associated with the following list of activities: Raw Materials Transport and Storage Intermediate Product Storage and Handling Final Product Storage and Handling Waste Handling The specific SOCMI production units present on-site at the time of this filing includes: Chlorine Ethyl Chloride (EC)/Hydrogen Chloride (HCI) Ethylene Dichloride (EDC) 551 OF16.01 SL 025852 2-1 Final 05/27/92  Perchloroethylene/Trichloroethylene (PER/TRI) Shipping/Loading Operations Tri-Ethane !! (Methyl Chloroform, MC) Vinyl Chloride (VCM-II) Vinylidene Chloride (VDCM) Waste Treatment Unit (WTU) Not included under this definition are activities and HAP emissions associated with: On-site Power Generation Caustics Processing Silicas Plant This definition meets the regulatory requirements outlined under Section 63.73(a)(1) as it addresses: A portion of an entire contiguous facility under common ownership or control, Activities defined by a standards under Section 112(d) of the Act. The base-year HAP emissions from SOCMI production within the contiguous facility boundary exceeded 25 tpy. Therefore, the plant is classified as a major source under 40 CFR 63.73. Based on the HAP emission reductions scheduled to occur at this source by January 1, 1994, PPG expects that the Lake Charles facility will be granted a six-year extension from any and all Section 112(d) standards applicable to SOCMI activities at the facility. Figure 2-1 shows the contiguous plant boundary for the PPG Lake Charles facility overlayed on a topographic map. This section discusses the approach that was used to define HAP emissions from SOCMI activities. Section 2.1 discusses the process unit descriptions used to organize the information 5510R016.01 SL 025853 2-2 Final 05/27/92 ~ TnZi i to 025854 ENS presented in the report and appendices. Section 2.2 defines the HAP emissions from the source that are included in the Enforceable Commitment. 2.1 Process Unit Description The SOCMI chemical production activities at the Lake Charles plant are extensive. PPG has defined several independent areas of the facility, where similar activities are grouped into a single process unit. To prepare the Enforceable Commitment, the list of these process units was used to aid in organizing the information presented in this report. The process units used in this report are as follows: Chlorine Ethyl Chloride (EC)/Hydrogen Chloride (HCI) Ethylene Dichloride (EDC) Perchloroethylene/Trichloroethylene (PER/TRI) Shipping and Loading (S/L) Tri-Ethane* II (Methyl Chloroform, TE-II) Vinyl Chloride (VCM-II) Vinylidene Chloride (VDCM) Waste Treatment Unit (WTU) Figure 2-2 is a plot plan showing the general location of the process units. Appendix A presents a detailed discussion of the major production activities that occur at the plant. Chlorine is an important raw material used in the manufacture of chlorinated organics at the PPG Lake Charles facility. Therefore, the production of chlorine by electrolyzing sodium chloride in diaphragm and mercury cells is included in the PPG source definition. The PPG facility also includes the following process units: Caustic, 5510R016.01 SL 025855 2-4 Final 05/27/92 ftBSS&S ! ^ FIGURE 2-2 PLOT PLAN PRODUCTION UNIT LAYOUT e& r ' 1 CHEMICALS CMLfijdsLaajCI*(*UfToGufmHtNn fofoiupKUHdiK *1!5-!WSL4*5_ . owe 32A-602.2-i  Silica, and Power and Utilities. Intermediate and final products from the Silica and Caustic units are not SOCMI processes. Power and Utility process systems are not addressed as they do not constitute a SOCMI facility as defined in the proposed Hazardous Organic NESHAP. Therefore, the activities from these units are not included in the definition of source. 2.2 Hazardous Air Pollutant (HAP) Emission Sources HAP emissions were determined for each of the process units described in Section 2.1. The calculation of emissions was performed for the specific source types listed in the HON. This list includes: Process Vents, Storage Tanks, Transfer Operations (shipping and loading), Equipment Leaks, and Wastewater Treatment. The HON will regulate equipment leaks as a source type. However, HAP emissions from equipment leaks from afi production units were excluded from the definition of source. The decision to exclude equipment leaks from this Enforceable Commitment was based on uncertainties in establishing base-year emissions and calculating a control efficiency from the reductions associated with the leak detection and repair program at the PPG plant. Further, PPG has an intensive leak detection program in place that either currently meets MACT requirements or will require only minor modification to achieve compliance. Table 2-1 lists the HAP emission points by process. Also shown in Table 2-1 is the type of emission source (process vent (P), storage tank (T), chlorine manufacturing building fugitive emissions (B), transfer operations (S/L), and wastewater (WW)). Each emission point is 5510R016.01 SL 025857 2-6 Final 05/27/92 EMR identified by a unique Emission Inventory Questionnaire (EIQ) number. The EIQ identifier is used for reporting emissions to the LDEQ. Generally, EIQ numbers from 100 to 199 are assigned to emission points in the chlorine and caustic production units. EIQ numbers from 300 to 399 are assigned to the production of organic chemicals. 5510n016.01 Si 25858 2-7 Final 05/27/92 TABLE 2-1 Emission Point Descriptions EIQ No. 100 101 102 105 106 107 109 128 130 300 301 302 302A 302C 302D 303 304 305 306 307A 307B 308 Unit CHLORINE CHLORINE CHLORINE CHLORINE CHLORINE CHLORINE CHLORINE WTU CHLORINE EDC EDO VDCM VOCM VDCM VDCM PER/TRI EC/Ha TE-II TE-II VCM-II VCM-II S/L Description Mercury Cell H2 Vent Mercury Cell Cl2 Neutralizer Fume System Endbox Vent Plant C Absorber Circuit 15 Neut. Tower Circuit 16 Neut. Tower Sulfur Chloride Vent Outfall Sewer Vent Scrubber Sulfur Chloride Fume Scrubber No. 1 LP-EDC Startup Scrubber No. 2 LP-EDC Startup Scrubber VDCM/Trans Plant SU Scrubber No. 3 LP-EDC Scrubber/VDCM Plant Vent VDCM/No. 3 LP-EDC Scrubber VDCM/Trans Scrubber Per/Tri Startup Scrubber EC Scrubber MC/DCE Startup Scrubber No. 2 OHC Startup Scrubber VCM-II Startup Scrubber VCM-II Startup Scrubber VDCM Tank Car Vent Type P P P P P P P P P P P P P P P P P P P P P P 5510T016.01 SL 025859 2-8 Final 05/27/92 EIQ No. 309 310 311A 311B 312 313 314 315 316 317 318 319 320 321 322 323 324 325 326 327 328 329 330 331 __________________________ Eta TABLE 2-1 (Cont'd) Emission Point Descriptions Unit WTU TE-II WTU WTU EDC EDC EDC TE-H TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II PER/TRI PER/TRI PER/TRI PER/TRI PER/TRI Description CPC Unit Scrubber DCE Tank Vents No. 2 DH Still Tank Per/Tri Acid Steam Stripper System Scrubber LP-EDC Process Tanks No. 1 N. Dock EDC Tank No. 1 EDC Tank EDC Crude and Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Dock Storage TE Shipping Tank Per Dock Storage Tank Per Process Storage Per 208 Shipping Tank Trl Dock Storage Tri Process Storage Type P T T P T T T T T T T T T T T T T T T T T T T T 5510T016.01 SL 025860 2-9 Final 05/27/92 EIQ No. 332 333 334 335 337 338 339 340 341 342 343 344A 344B 345 346 347 348A 348B 353 355 358 359 360 361 _______________________ EKR TABLE 2-1 (Confd) Emission Point Descriptions Unit WTU wru perari WTU EC/Hd EC/HQ PERATM PERARi PERARI WTU WTU WTU WTU WTU WTU WTU WTU WTU TE-II TE-II TE-II PERARI PERARI VDCM Description Bottoms Tank No. 6301 PerArt Feed Tanks Tri Shipping Tank Puerto Rican Bottoms Tank VCM-I Plant Scrubber HQ Tails Tower Scrubber PerAri Still Line Scrubber PerAn DH System Vent Scrubber PerAri Acid Tank Scrubber WTU Scrubber S. Qassifler Scrubber Vent Bottoms Plant Tank Bottoms Plant Scrubber No. 1&2 Incinerator Sec. Scrubber No. 3 Incinerator Sec. Scrubber No. 4 Incinerator Incinerator Scrubber Incinerator Tanks Scrubber TCEAetra Tank No. 1 BLM Storage Tank TBL/MC Tank PerAri Product Dryer Regen. PerAri Still Line Tank TCE Tank Type T T T T P P P P P P P T P P P P P T T T T P T T S510T016.01 SL 025861 2-10 Final 05/27/92 TABLE 2-1 (Cont'd) Emission Point Descriptions EIQ No. 362 363 365 369 370 371 373 374 375 376 377 380 381 382 383 384 385 386 387 388 Unit PER/TRI PER/TRI CHLORINE CHLORINE CHLORINE CHLORINE EC/HCL EC/HCL WTU PER/TRI PER/TRI WTU WTU WTU WTU WTU WTU WTU WTU WTU Description Per/Tri BLM Tank No. 1 Per/Tri BLM Tank No. 2 Brine/HCL NeuL Reactor Tank Vent Scrubber No. 1 HCL Acid Storage Tank Scrubber HCL Acid Head Tank Scrubber D.l. Tank Vent North Rubber Lined Acid Tank Scrubber South Rubber Lined Acid Tank Scrubber HCL Acid Formate Destruction Unit Dowtherm 'A" Makeup Tank Dowtherm Recycle H20 Recovery Tank North Dock G.W. Collection Tank S. Terminal G.W. Collection Tank West Vacuum Tank Vent East Vacuum Tank Vent G.W. Pumps Vent North Classifier Lift Stations Surge Pond Vacuum Trucks Type T T T T T T T T T T T T T P P P WW WW WW WW 5510T016.01 SL 025862 2-11 Final 05/27/92 TABLE 2-1 (Cont'd) Emission Point Descriptions EIQ No. Unit Description 389 WTU API Separator 390 S/L 391 S/L 392 S/L 393 S/L 394 S/L Ships Barges Railcar Tank Trucks Drums p - Preen vent T Storage Tank WW< Fugitivewnttaton*fromwatitmetm SL Fugitive wMsskm* from (flipping and kMdttg operation* Su - Startup mode operation GW - Groundwater Set. - Scnibbar Sac. - Secondary NeuL - NeuMtzaOon Type WW SL SL SL SL SL 5510T016.01 025863 SL 2-12 Final 05/27/92 3.0 BASE-YEAR SELECTION Demonstrating compliance with the emission reduction requirements of the Early Reduction Program necessitates establishing the total base-year HAP emissions for the source. As required by EPA, "base-year emissions must represent actual and verifiable emissions for calendar year 1987 or later.' Selection of a base year must ensure HAP emissions are not artificially or substantially higher than would occur under normal operations. PPG has selected 1987 as the year for which the baseline emissions were calculated. The selection of 1987 is based on the following: Emissions in 1987 were not unusually high when compared to preceding and subsequent years and, therefore, are a reasonable representation of normal operations; Significant process modifications occurred in wastewater treatment methods in 1987 resulting in a significant reduction in HAP emissions; and PPG instituted a program of emissions reductions at the facility beginning in 1987 which included process changes, application of vent recovery, and incineration of process vents, also resulting in significant reductions in HAP emissions. Table 3-1 shows the production data for the chemicals manufactured and shipped from the PPG facility for the years 1985 to 1990. In fact, none of the major chemicals were produced at their maximum rates during 1987. Trichloroethylene and vinylidene chloride emissions peaked in 1985 and 1986, respectively. The peak production of the other chemicals except chloropivaloyl chloride occurred after 1987. 56i onoie.oi Sb 025866 3-1 Final 05/27/92 TABLE 3-1 Production Rate (TPY) Chemical ;i" . 1989 . 1990 Chlorine 916,415 1,032,949 1,149,972 1,157,817 1,185,665 1,189,842 Ethylene Dichloride 515.386 634,767 729,419 727,674 853.922 893,881 Ethyl Chloride Methyl Chloroform (Tri-Ethane* II) 22,934 74,452 28,854 82,821 24,894 83,710 30,235 79,602 42,990 81,251 60*232 ' 7;,;? PercNoroethyiene Trichloroethylene 36,946 ^008 38,048 21,441 46,551 25,254 26,241 48,461 27,464 41.552 24,245 Vinyl Chloride Vinylidene Chloride 254,502 11,066 298,416 344,661 12,412 i 9,564 343,652 7,366 356,335 7,207 369,064 10,295 Transdichloroethyiene 0 0 0 0 238 Chloroplvaloyl Chloride 0 414 2194 ! - PMk Production Yaar snadad production touu ara tna highaat production rata for aacn compound. 1606 1571 805 5510T016.01 SL 025865 3-2 Final 05/27/92 4.0 EARLY REDUCTION DEMONSTRATION This section discusses the results of the base and post-reduction emission calculations. A detailed presentation of the emission calculation for each of the PPG process units is included in Appendices B through J. Also discussed in this section is the proposed strategy to achieve the 90 percent reduction required by the early reduction program. 4.1 Emissions Summary Using representative stack sampling data and process specific information, emissions were calculated for the 1987 base year. Table 4-1 shows the unweighted and weighted base-year HAP emissions by process unit. The total unweighted base-year HAP emissions were 1634.192 Mg/yr compared to the total weighted HAP emissions of 2327.094 Mg/yr. The chemicals vinyl chloride, vinylidene chloride (1,1-dichloroethylene), and 1,1,2-2-tetrachloroethane were included in the list of high risk pollutants, and therefore, the base and post-reduction year emissions were multiplied by the factor 10 to determine the weighted HAP emissions. Unweighted post-reduction emissions were determined from the base-year emissions and the percent additional control to be applied by PPG prior to January 1, 1994. This resulted in a predicted post-reduction total of 105.962 Mg/yr. Post-reduction weighted HAP emissions were calculated in the same manner noted above giving a total of 151.880 Mg/yr. A 93.516 percent reduction in unweighted HAP emissions from SOCMI-related production at the PPG Lake Charles facility was calculated from the 1987 base-year emissions. For weighted HAP emissions, a 93.473 percent reduction was calculated. These reductions, which exceed 90 percent, qualify the PPG facility for participation in the early reduction program. 5510R01B.01 SL 025866 4-1 Final 05/27/92 Revised 05/29/92 TABLE 4-1 Early Reductions Emission Summary Process Unit Chlorine Ethyl Chloride (EC)/ Hydrogen Chloride (HCI) Ethylene Dichloride (EDC) Perchloroethytene/' Trichloroethylene (PER/TRI) Shipping and Loading (S/L) Tri-Ethane*il (TE-II) Vinyl Chloride (VCM-II) Vinytidene Chloride (VDCM) Waste Treatment Unit (WTU) Total Total Reduction Percent Reduction Unweighted HAP Emissions (Mg/Yr) Base Year PostReduction 0.192 0.056 4.286 0.141 6.784 206.784 0.868 25.535 164.402 46.266 11.690 41.260 1152.528 1634.192 9.637 30.536 9.434 0.001 29.754 105.962 1528.231 93.5t6 Weighted HAP Emissions (Mg/Yr) Base Year PostReduction 0.192 0.056 5.462 1.316 9.051 366.552 164.402 48.187 15.923 274.779 1442.546 2327.094 0.870 52.705 9.637 32.457 9.435 0.009 45.395 151.880 2175.214 93.473 5510T016.01 SL 025867 4-2 Final 05/27/92 Revised 05/29/92 4.2 Emission Reduction Strategy Table 4-2 presents the strategy that will be used to reduce the 1987 base-year emissions by the required 90 percent. The control device and the percent reduction in base-year emissions is shown. In the chlorine process unit, most EIQ sources were controlled to levels of 90 percent or greater in 1987. Additional control will be placed on EIQ 101. Otherwise, no further controls will be applied at this production unit. The majority of the emissions reductions in the wastewater treatment area was achieved by replacing the surge pond and API separator with surge tanks and clarifiers. A net reduction in unweighted HAP emissions of 1122.774 Mg/yr and weighted HAP emissions of 1397.151 resulted from these changes. Another significant source of emissions to be controlled by January 1, 1994 is the transfer operations emissions from loading drums, tank trucks, railcars, barges, and ships. HAP emissions from tank trucks and railcars will be collected and routed to an existing incinerator. Refrigerated condensers (98 percent control) followed by carbon adsorption (98 percent control) will be used to reduce barge and ship loading emissions of ethylene dichloride. A total HAP emissions reduction of 154.765 Mg/yr is calculated for transfer operations. The process vent and storage tank emissions will be reduced significantly using incineration and refrigerated condensers. In cases where incineration will be applied, non-routine emissions, have been estimated and are included in the emission totals. Non-routine emissions occur infrequently and are not expected to exceed 10 to 20 hours per year based on existing operating data. Further, projects are currently underway at the Lake Charles facility to improve the reliability of the existing incinerator systems, which will reduce the amount of non-routine emissions. S510R016.01 SL 25868 4-3 Final 05/27/92 Revised 05/29/92 TABLE 4-2 Strategy to Achieve Emissions Reductions EIQNo. 100 101 102 105 106 107 109 128 130 300(NR) 3Q0(SU) 300(S0) 301 (NR) 301 (SU) 301 (SO) 302 302A 302C(NR) 302C(SU) 302D 303(NR) Process Untt Description CHLORINE CHLORINE Mercury Cell H2 Vent Mercury Cell Clj Neutralizer CHLORINE Fume System Endbox Vent CHLORINE Plant C Absorber CHLORINE Circuit 15 Neutralizer Tower CHLORINE Circuit 16 Neutralizer Tower CHLORINE Sulfur Chloride Vent WTU Outfall Sewer Vent Scrubber CHLORINE Sulfur Chloride Fume Scrubber EDC No. 1 LP-EDC Startup Scrubber EDC No. 1 LP-EDC Startup Scrubber EDC No. 1 LP-EDC Startup Scrubber EDC No. 2 LP-EDC Startup Scrubber EDC No. 2 LP-EDC Startup Scrubber EDC No. 2 LP-EDC Startup Scrubber VDCM VDCM/Trans Plant SU. Scrubber VDCM No. 3 LP-EDC Scrubber/VDCM Plant Vent VDCM VDCM/No. 3 LP-EDC Scrubber VDCM VDCM/No. 3 LP-EDC Scrubber VDCM VDCM/Trans Scrubber PER/TRI Per/Tri Startup Scrubber Control Device 1987 1994 Vapor Rec Scrubber Vapor Rec Upgraded Scrubber Vapor Rec Vapor Rec Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Vapor Rec Vapor Rec None Scrubber Did Not Exist Scrubber Scrubber Scrubber Scrubber Scrubber Incinerator Incinerator Scrubber Scrubber Scrubber Incinerator Scrubber Incinerator Did Not Exist Incinerator Scrubber Deleted 1994 % Control 98.00 99.90 99.00 99.90 99.90 99.90 99.90 99.80 100 5/99* 99.99 99.99 5/99* 99.99 99.99 99.99 100 Scrubber Scrubber Did Not Exist Scrubber EIQ302 EIO 302 EIQ 302 Scrubber -- -- -- 5/99* 5510T016.01 SL 025869 4-4 Final 05/27/92 TABLE 4-2 (Cont'd) Strategy to Achieve Emissions Reductions EIQ No. 303(SU) 304(NR) 304(SU) 305(NR) 305(SU) 306(NR) 306(SU) 306(SD) 307A(NR) 307A(SU) 307B(NR) 307B(SD) 308 309(NR) 310 311A 311B 312 313 314 315 Procsss Unit PER/TRI EC/HCL EC/HCL TE-II TE-II TE-II TE-II TE-II VCM-II VCM-II VCM-II VCM-II S/L WTU TE-II WTU WTU EDC EDC EOC TE-II Description Per/Tri Startup Scrubber EC Scrubber EC Scrubber MC/0CE Startup Scrubber MC/DCE Startup Scrubber No. 2 OHC Startup Scrubber No. 2 OHC Startup Scrubber No. 2 OHC Startup Scrubber VCM-II Startup Scrubber VCM-II Startup Scrubber VCM-II Startup Scrubber VCM-II Startup Scrubber VDCM Tank Car Vent CPC Unit Scrubber DCE Tank Vents No. 2 DH Still Tank Per/Tri Acid Steam Stripper System LP-EDC Process Tanks No. 1 North Dock EDC Tank No. 1 EDC Tank EDC Crude and Storage Control Device 1987 1994 Scrubber Incinerator Scrubber Scrubber Scrubber Incinerator Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Incinerator Scrubber Scrubber Incinerator Scrubber Scrubber Scrubber None Incinerator Scrubber Scrubber Ref. Cond. Ref. Cond. Scrubber Did Not Exist Scrubber Scrubber Scrubber Ref. Cond. Scrubber Ref. Cond. Incinerator Ref. Cond. Incinerator Ref. Cond. 1994 % Control 99.99 5/99* 99.99 . 5/99* 5/99* 5/99* 5/99* 5/99* 99.99 99.99 5/99* 5/99* 99.99 5/99* 88.10 5/99* 5/99* 99.99 99.00 99.99 88.00 S510TD16.01 SL 025870 4-5 Final 05/27/92 TABLE 4-2 (Cont'd) Strategy to Achieve Emissions Reductions EIQ No. 316 317 318 319 320 321 322 323 324 325 326 327 328 329 330 331 332 333 334 335 337 338 Process Unit TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II per/TM PER/TRI PER/TRI PER/TRI PER/TRI WTU WTU PER/TRI WTU EC/HCL EC/HCL Description MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Dock Storage TE Shipping Tank Per Dock Storage Tank Per Process Storage Per 208 Shipping Tank Tri Dock Storage Tri Process Storage Bottoms Tank No. 6301 Per/Tri Feed Tanks Tri Shipping Tank Puerto Rican Bottoms Tank VCM-I Plant Scrubber HD Tails Tower Scrubber Control Device 1987 1994 None None None None None None None None Ref. Cond. Incinerator Incinerator Incinerator Incinerator Incinerator Incinerator Incinerator Incinerator Ref. Cond. Ref. Cond. Ref. Cond. None Incinerator None Ref. Cond. None Ref. Cond. None Ref. Cond. Incinerator Ref. Cond. Ref. Cond. Scrubber Ref. Cond. Incinerator Scrubber Incinerator None Incinerator Scrubber Removed Incinerator Incinerator Scrubber Scrubber ENS 1994 % Control 99.99 99.99 99.99 99.99 99.99 99.99 99.99 99.99 84.00 88.40 99.99 0.00 73.10 99.99 66.70 69.20 99.99 99.99 99.99 100.00 99.99 5/99* j 1 i 551OTOI 6.01 SL 025871 4-6 Final 05/27/92 TABLE 4-2 (Cont'd) Strategy to Achieve Emissions Reductions EIQ No. 339 340 341 342 343 344A 344B 345 346 347 348A 348B 353 355 358 359 360 361 362 Procsss Unit per/tri PER/TRI PER/TRI WTU wru WTU wru WTU WTU WTU WTU WTU TE-II TE-II TE-II PER/TRI PER/TRI VDCM PER/TRI Osscription Per/Tri Still Line Scrubber Per/Tri DH System Vent Scrubber Per/Tri Add Tank Scrubber WTU Scrubber S. Classifier Scrubber Vent Bottoms Plant Tank Bottoms Plant Scrubber No. 1&2 Incinerator Secondary Scrubber No. 3 Incinerator Sec. Scrubber No. 4 Incinerator Indnerator Scrubber Indnerator Tanks Scrubber TCE/Tetra Tank No. 1 BLM Storage Tank TBL/MC Tank Per/Tri Product Dryer Regeneration Per/Tri Still Line Tank TCE Tank Per/Tri BLM Tank No. 1 Control Device 1987 1994 Scrubber Incinerator Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Indnerator Scrubber Incinerator Incinerator Indnerator Incinerator Indnerator Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber None None Scrubber Scrubber Scrubber None Scrubber Scrubber Deleted Indnerator Scrubber None Indnerator Cool Water Condenser Incinerator Incinerator None 1994 % Control 98.00 5/99* 99.99 99.99 99.99 99.99 99.99 5/99* 5/99* 5/99* 100 99.99 5.00 0.00 99.99 99.0 99.99 99.99 0.0 5510T01S.01 SL 025872 4-7 Final 05/27/92 TABLE 4-2 (Cont'd) Strategy to Achieve Emissions Reductions EIQ No. 363 365 369 370 371 373 374 375 376 377 360 381 382 363 364 365 386 387 388 Process Unit Description Control Oevice 1987 1994 PER/TRI CHLORINE CHLORINE Par/Tri BLM Tank No. 2 Brina/HCL Neut. Reactor Tank Vent Scrubber No. 1 HCL Add Storage Tank Scrubber None Scrubber Scrubber None Scrubber Scrubber CHLORINE HCL Add Head Tank Scrubber CHLORINE 0.1. Tank Vent EC/HCL North Rubber Lined Add Tank Scrubber EC/HCL South Rubber Lined Add Tank Scrubber WTU HCL Add Formate Destruction Unit PER/TRI Dowtherm *A* Makeup Tank PER/TRI Dowtherm Recyde H20 Recovery Tank Scrubber Scrubber Scrubber Scrubber Scrubber None None Scrubber Scrubber Scrubber Scrubber Scrubber None None WTU N. Dock Q.W. Collection Tank None None WTU S. Terminal G.W. Collection Tank None CB WTU WTU WTU WTU WTU West Vacuum Tank Vent East Vacuum Tank Vent Ground Water Pumps Vent North Classifier Lift Stations None None None None None/Covered None None None Replace Covered/CB WTU Surge Pond None Removed WTU Vacuum Trucks None Process Changes EMK 1994 % Control 0.0 99.0 99.0 99.0 99.0 99.0 99.0 99.0 0.00 0.00 0.00 98.0 0.00 0.00 0.00 99.99 90.0 100 98.0 5510T016.01 SL 25873 4-8 Final 05/27/92 TABLE 4-2 (Cont'd) Strategy to Achieve Emissions Reductions EIQNo. 389 Proceed Unit WTU Description API Separator 390 S/L Ships (EDO) Ships (Other Chemicals) 391 S/L Barges (EDC) Barges (Other Chemicals) 392 S/L Railcars 393 S/L Tank Trucks 394 S/L Drums Ser- Sounder Sac* Secondary flat. Cond. - nefrtgerated Condenser Vapor nac Vapor Recovery Cool WM * CooNng Tower Water S/L - Stripping and loading fugfttva ammions NR - NorvftouOne Operation Su - Startup moda operation $0 SIkMoimi Moda Operation C8 Carbon adMrpdon * - Scnriaber Me S% efficiency tar hydrocarbon and B0K atnciency tar HCL Control Device 1987 1994 None Not in Service None Ref. Cond./CB None None None Ref. Cond./CB None None None Incinerator None Incinerator None CB 1994 % Control 100 OQ Oft 0.00 99.96 0.00 99.99 99.99 98.0 5510T016.01 SL 025874 4*9 Final 05/27/92 Chemical Name Chloroform Trichloroethylene Carbon Tetrachloride 1,2-Dichloroethane 1,1-Dlchloroethane 1,1,2-Dichloroethane 1,2-Dlchloroethylene Perchloroethlyene Ethyl Chloride Vinylldene Dichloride 1,1,2-TricNoroethylene Methyl Chloroform Vinyl Chloride 1,1,2,2-symTetrachloroethane Methyl Chloride Pentachloroethane HexacNoro 1,3-Butadiene Tert Butyialcohol Hexachloroethane Chlorobenzene Heavy Chloride 1,4-Dioxane TABLE 4-3 Vapor Pressure of Pollutants Abbreviation chq3 Tri ca4 EDC DCE Unsym CIS Per EC VDCM TCE MC VC SYM Vap. Pres*. @ 70F (psia) 3.154 1.45 1.767 1.33 3.67 0.215 3.33 0.27 20.37 9.656 0.38 2.02 51.35 0.1 MeCl Penta HCBD TBL HEXA C6H5Q Hvy-Chlori DOX 73.96 0.069 0.002 0.63 0.0083 0.18 0.046 0.55 5510T010.01 SL 025875 4-10 Final 05/27/92 TABLE 4-3 (Cont'd) Vapor Pressure of Pollutants Chemical Name Dioxolane 2-Nitropropane Nitromethane Sec-Butyl alcohol 1,2-Butylene Oxide Hexachiorobenzene Bromomethane Toluene Trans 1,2Oichloroethylene Dimethoxy methane Butyl Tertiary Ether Penta Chloro Butadiene Methylene Chloride n-Propanol Biphenyl Hydrogen Chloride (Aqueous) Abbreviation DOL NTE NRE SBL BLM HCB Bromo TLE trans DME BTE PCBD MeQ2 NPL Biphenyl HO * These are partial pressures at 70* F, Vap. Press. @ 70F (psia) 1.37 0.2 0.56 0.17 2.83 0.03 0.07 0.48 5.21 6.38 1.93 0.286 7.74 0.3 0.052 (6% HQ) 0.000147* (20% HQ) 0.003965* (30% HQ) 0.205* SL 025876 5510T016.01 4-11 Final 05/27/92 5.0 GLOSSARY OF ABBREVIATIONS Adsorption American Petroleum Institute Best Available Technology Carbon Bed Adsorption Carbon Tetrachloride Chlorine Chloroform Chloropivaloyl Chloride Clean Air Act Amendments Code of Federal Regulations Condenser Dehydration 1,1-Dichloroethane Early Reduction Program Emissions Inventory Questionnaire Ethyl Chloride Ethylene Dichloride (1,2-Dichloroethane) Fugitive Emissions Groundwater Hazardous Air Pollutant Hazardous Organic NESHAP Hexachloro-1, 3-Butadiene Hexachloroethane Hydrogen Chloride Liquid Phase Louisiana Department of Environmental Quality Maximum Achievable Control Technology Mercury Methyl Chloride Methyl Chloroform Methylene Chloride Million Grams Per Year (Megagrams Per Year) National Emission Standard for Hazardous Air Pollutant Neutralizing New Source Performance Standards 551OROI 6.01 SL 025877 5-1 ENSt Adsorp API BAT CB CCI4 Cl2 chci3 CPC CAAA CFR Cond DH DCE ERP EIQ EC EDC F G.W. HAP HON HCBD HEXA HCI LP LDEQ MACT Hg MECI MC MEC!2 Mg/Yr NESHAP Neut NSPS Final 05/27/92 2-Nitropropane Non-Routine Oxygen Oxyhydrochlorination Perchloroethylene (Tetrachloroethylene) Plant Pivaloyl Chloride Process Vent Railcar Refrigerated Refrigerated Vent Recovery Scrubber Secondary Shipping and Loading Shutdown Startup Storage Tank Synthetic Organic Chemical Manufacturing Industries Tank Truck Thermal Conductivity Detector 1.1.2.2-tetrachloroethane Tons Per Year Transfer Operations Tri-Ethane* II Process Unit 1.1.2- trichloroethane Trichloroethylene United States Environmental Protection Agency Vinyl Chloride Vinyl Chloride Process Unit Vinylidene Chloride Vinylidene Chloride Process Unit Waste Treatment Unit Wastewater Water 5510H010.01 SL 025878 5-2 ENSR NTE NR 02 OHC PER Pit PC P RC Ref RVR SCR Sec S/L SD SU T SOCMI XT TCD SYM (TETRA) tpy S/L XE-II JCE TRI EPA VC VCM II VDC VDCM WTU WW h20 Fml 05/27/92 APPENDIX A FACILITY DESCRIPTION SSI OROI 6.01 SL 025879 Final 05/27/92 APPENDIX A FACILITY DESCRIPTION A.1 Facility Identifying Information Company Name: Address: City/State/Zip: PPG Industries, Inc. Columbia Southern Road P.O. Box 1000 Lake Charles, LA 70602 Corporate Official: Title: Telephone Number: Address: City/State/Zip: Richard Rompala Group Vice President, Chemicals (412) 434-2515 (Business) PPG Industries, Inc. One PPG Place Pittsburgh, PA 15272 Local Responsible Official: Title: Telephone Number: Address: City/State/Zip: Dave Angell Works Director, Environmental Assurance (318) 491-4823 (Business) P.O. Box 1000 Lake Charles, LA 70602 Local Plant Contact: Title: Telephone Number: Lamar White Manager, Derivatives (318) 491-4712 (Business) Local Plant Contact: Title: Telephone Number: Jim Wyche Environmental Manager (318) 491-4830 (Business) S510M>16.01A 0 A-1 Final 05/27/92 Source: Activities within the contiguous property boundary which will be subject to regulation under the Hazardous Organic NESHAP (HON), directly associated with the handling of raw materials, the handling, production or transport of intermediate and final products, and wastes of SOCMI chemicals, excluding all hazardous air pollutants (HAP) emissions from equipment leaks and non-SOCMI production units in operation at the facility. These activities are strictly limited to the those SOCMI chemical production units which are in operation prior to proposal of the HON. Included under this definition are all known points of emissions associated with the following list of activities: Raw Materials Transport and Storage Intermediate Product Storage and Handling Final Product Storage and Handling Waste Handling The specific SOCMI production units present on-site at the time of this filing includes: Chlorine Ethyl Chlorine (EC)/Hydrogen Chloride (HCI) Ethylene Dichloride (EDC) Perchloroethylene/Trichloroethylene (PER/TRI) Shipping/Loading Operations Tri-Ethane II* (Methyl Chloroform, MC) Vinyl Chloride (VCM-II) Vinylidene Chloride (VDCM) Waste Treatment Unit (WTU) Not included under this definition are activities and HAP emissions associated with: On-site Power Generation Caustics Processing Silicas Rant This definition meets the regulatory requirements outlined under Section 63.73(a)(1) as it addresses: A portion of an entire contiguous facility under common ownership or control, Activities defined by a standards under Section 112(d) of the Act. 5510N018.01A SL 2588l A-2 Final 05/27/92 E1KR Activity Causing HAP Emissions: Emissions of raw materials, intermediate products, by-products, and final products from process vents, storage tanks, shipping/loading, and waste treatment from the production of chlorinated organics and chlorine. General Source Description: The PPG Lake Charles facility is divided into three production areas: Plant A - Chlorine and Caustic Production Plant B - Chlorinated Organics Production Plant C - Chlorine, Caustic, and Silica Production Several of the emissions vent identifications and the process flow diagrams discussed in the following appendjces refer to Plant B, the chlorinated organics production area and Plants A and C, chlorine production. Products manufactured in Plant B include vinyl chloride, chloropivaloyl chloride, transdichloroethylene, ethyl chloride, vinylidene dichloride, perchloroethylene, trichloroethylene, methyl chloroform, hydrogen chloride, and ethylene dichloride.. In addition to these finished products, several intermediate products are made and internally consumed. Table A-l presents the primary products, by-products, and intermediates found in the plant and aids in understanding the nomenclature used in the following Appendices. Figure A-l shows the interrelationships in the production processes. The primary raw materials required in Plant B are ethylene and chlorine. Ethylene is purchased from the area petrochemical industry and chlorine is supplied from within the Lake Charles facility by Plant A. Because of the importance of chlorine as a raw material, and because chlorine is 5510R016.01A SL 025882 A-3 Final 05/27/92 TABLE A-1 Common Hydrocarbon Compounds Found in Plant B Common Nam* Ethylene Vinyl chloride Vinylidene dichloride Cis-dlchloroethylene Trans-dichloroethylene Trichloroethylene Perchloroethylene Ethyl cNoride Ethylene dichloride, (1,2-Dichloroethane) 1,1-Dichloroethane Methyl chloroform, (1,1,1-trlchloroethane) 1,1,2-trichloroethane UnsymmetricaJ tetrachloroethane 1,1,1,2-tetrachloroethane Symmetrical tetrachloroethane 1.1,2,2-tetrachloroethane Pentachloroethane Hexachloroethane Hydrogen chloride Abbreviation Primary End Use C2H4 Raw Material VC Plastics VDC Plastics Cis Intermediate By-Product Trans TRI Intermediate By-Product Solvent PER Solvent EC Ethylene Glycol EDC Intermediate Product DCE Intermediate Product MC Solvent TCE Intermediate Product Unsym Intermediate Product Sym Intermediate Product Penta Hexa HCI Intermediate Product Undesirable By-Product Muriatic Acid 5510T016.01 SL 025883 Final 05/27/92 Figure A-1: Plant B Chlorinated Organics Production Process Flow Diagram See Volume II - Confidential 5510R018.01A SL 025884 A-5 Final 05/27/92 manufactured on site, HAP emissions from chlorine production are included in base-year emissions. For organizational purposes, HAP emissions from the PPG facility are reported by functional unit. The functional units, discussed in detail in the following Appendices are as follows: Chlorine; Ethyl Chloride (EC)/Hydrogen Chloride (HCI); Ethylene Dichioride (EDC); Perchloroethylene/Trichloroethylene (Per/Tri); Shipping/Loading (S/L); Tri-Ethane* II (TE-II); Vinyl Chloride (VCM-II); Vinylldene Chloride (VDCM); and Waste Treatment Unit (WTU). 5510R016.01A SL 025885 A-6 Final 05/37/92 APPENDIX B CHLORINE PROCESS UNIT ssionoieoi SL 025886 Final 05/27/92 APPENDIX B CHLORINE PROCESS UNIT B.1 Process Description Sodium chloride is electrolyzed in cells to produce chlorine and sodium hydroxide. The electrolysis is achieved in a series of mercury cells and diaphragm cells. The feed to the chlorine manufacturing processes is brine from salt domes mined at nearby facilities. The products of electrolysis are chlorine, sodium hydroxide, and hydrogen. Chlorine is used internally to manufacture chlorinated organics or is sold in the merchant market. Nearly all the caustic is sold and the hydrogen is burned as fuel or sold. Chlorine is produced in two areas of the PPG plant, designated as Chlorine Plants A and C. These two areas are combined as one production unit; the 'Chlorine Manufacturing Unit" (CHLORINE). Figures B-1 and B-2 show the major equipment associated with both types of chlorine production. The HAP emissions associated with chlorine manufacture are small amounts of Cl2 gas and mercury vapors. B.2 1987 Base-Year Emissions Table B-1 shows the total base-year emissions for the chlorine process unit. The total unweighted HAP emissions were 0.1916 Mg/yr. Since none of the sources emitted pollutants that are considered high risk pollutants and subject to multiplication by a weighting factor, the total weighted HAP base-year emissions equal the total unweighted HAP base-year emissions. B.3 Emissions Reduction Strategy Table B-2 shows the control strategy for the chlorine unit that will be implemented to help achieve a plantwide reduction in emissions for all SOCMI sources at the facility. Only one of the vents (EIQ 101, mercury cell Cl2 neutralizer) will have additional controls, a higher efficiency scrubber, which will reduce the emissions from that vent to 0.005 Mg/yr. 5510R016.01A SL 025887 B-1 Final 05/27/92 Figure B-1: Diaphragm - Chlorine and Caustic Production See Volume II - Confidential ENat 5510R016.0M SL 025888 B-2 Final 05/27/92 Figure B-2: Mercury - Chlorine and Caustic Production See Volume II - Confidential ENat SL 025889 5510A016.01A B*3 Final 05/27/92 (r/] o to Cn CO o TABLE B-1 1907 BASE YEAR EMISSIONS CHLORINE MANUFACTURING UNIT EIQ DESCRIPTION TYPE CHLORINE 100 CHLORINE 101 CHLORINE 102 CHLORINE 105 CHLORINE 106 CHLORINE 107 CHLORINE 109 CHLORINE 130 Mercury Cell H2 Vent Mercury Cell CI2 Neutralizer Fume System Endbox Vent Plant C Absorber Circuit 15 Neut. Tower Circuit 16 Neut. Tower Sulfur Chloride vent Sulfur Chloride Fume Scrubber CHLORINE 365 CHLORINE 369 CHLORINE 370 CHLORINE 371 Brine/HCI Neut. Reactor Tk. Vent Scr. No. 1 HCI Acid Storage Tank Scrubber HCi Acid Head Tank Scrubber D.i. Tank Vent P P P P P P P P T T T T BASE YEAR CONTROL D EVICE HAP EMISSIONS % UNWEIGHTED WEIGHTED TYPE CONTROL MG/YR Vapor Rec. 98.00 0.006 0.006 Scrubber 97.00 0.140 0.140 Vapor Rec. 99.00 0.042 0.042 Scrubber 99.90 0.002 0.002 Scrubber 99.90 0.000 0.000 Scrubber 99.90 0.000 0.000 Vapor Rec. 99.90 0.002 0.002 Did Not Exist 0.00 0.000 0.000 Subtotal Process Vents 0.1916 0.1916 Scrubber 99.00 0.000 0.000 Scrubber 99.00 0.000 0.000 Scrubber 99.00 0.000 0.000 Scrubber 99.00 0.000 0.000 Subtotal Tank Vents 0.000 0.000 _________________ 1 Total Base Year Emissions I 0.192 0.192 FILE: CLBASE c-n< MO Ln 00 TABLE B-2 EMISSIONS REDUCTIONS STRATEGY AND POST REDUCTION EMISSIONS CHLORINE MANUFACTURING UNIT EIQ DESCRIPTION CHLORINE too CHLORINE 101 CHLORINE 102 CHLORINE 10S CHLORINE 106 CHLORINE 107 CHLORINE 109 CHLORINE 130 Mercury Cell H2 Vent Mercury Cell CI2 Neutralizer Fume System Endbox Vent Plant C Absorber Circuit 15 Neut. Tower Circuit 16 Neut. Tower Sullur Chloride vent Sulfur Chloride Fume Scrubber CHLORINE 365 CHLORINE 369 CHLORINE 370 CHLORINE 371 Brine/HCI Neut. Reactor Tk. Vent Scr. No. 1 HCI Acid Storage Tank Scrubber HCI Acid Head Tank Scrubber D.l. Tank Vent POST REDUCTION TYPE P P P P P P P P T T T T ADDITIONAL CONTROL HAP EM SSIONS rooi UNWEIGHTED WEIGHTED % CONTROL MG/YR MG/YR None 98.00 0.006 0.006 Higher Efficiency Scr. 99.90 0.005 0.005 None 99.00 0.042 0.042 None 99.90 0.002 0.002 None 99.90 0.000 0.000 None 99.90 0.000 0.000 None 99.90 0.002 0.002 Scrubber 100.00 0.000 0.000 Subtotal Process Vents 0.056 0.056 None 99.00 0.000 0.000 None 99.00 0.000 0.000 None 99.00 0.000 0.000 None 99.00 0.000 0.000 Subtotal Tank Vents 0000 0.000 _____________________________________ 1 Total Post Reduction Emissions I 0.0561 0.056 FILE: CLPOST B.4 Post-Reduction Emissions ENkR Table B-3 shows the total weighted and unweighted HAP emissions for the chlorine process unit. The total post-reduction emissions of 0.056 Mg/yr represent a 0.136 Mg/yr decrease (70.83% reduction) in base-year emissions. 5510R016.01A SI* 025892 B-6 Final 05/27/92 w 025893 TABLE B-3 HAP EMISSIONS SUMMARY CHLORINE PROCESS UNIT Unweighted HAP Emissions Weighted HAP Emissions Post Percent Post Percent Type Base Year Reduction Reduction Base Year Reduction Reduction (Units) P (Mgfrr) 0.192 (Mfl/yr) 0.056 <% 70.83 (Mg/yr) 0.192 (Mg/yr) 0.056 <%) 70.83 T 0.000 0.000 0.00 0.000 0.000 0.00 F Total Total Percent Reduction _____ m_____ P-Ptocms Vnts T-TankVmto F - FugWv* amiulons 0.192 0.056 70.83 0.192 0.056 70.83 1 fi 0258''4 st Source: HON subunit(s) Chlorine Unit fCl.^ CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM FIXED ROOF STORAGE TANKS (SAMPLE) HAP: Hydrogen Chloride fHCl) Date: Year: 1987___________ _____05/13792------------Calculator: J. Greer Tank Designation: EIQ 365 BrineAHCl Neutralization Reactor Tank Scrubber (60-16021 product: Hy.<teaqen Chl<?riti<L HCl (3Q%) Tank Characteristics Inside diameter, (ft) Height, (ft) Capacity, (gal) * n Djh * 7.48 gal. 4 ft3 if not known Roof color _ Yellow Shell color Yellow Vapor space height, (ft)4 * * * * Ambient Conditions Average atmospheric pressure (psia) (defaults 14.7 psia) Average ambient diurnal temperature (F)b Average annual ambient temperature (F) Bulk Liguid_Characte_ristics Stored liquid temperature (F)C Total throughput per year (gal) Number of turnovers per year Molecular weight of HAP (lb/lb mole) Mole percent of HAP Partial pressure of the HAP at liquid conditions (psia) Adjustment Factors Paint factor Small diameter tank factor Turnover factorf Product factor9 6 8__ 1.900 4 ______14.7 ______18 70 70_________ 913.997 ____4-81.05 36.46 11.0 0.000435 ______1.3 ______0.2824 ______0.23 ______1.0 D HT V H Pa dT ta TS an N Mv % P FP C kn Kc B-9 Source: HON subunit (s) Chlorine Unit (Cl-^ CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM FIXED ROOF STORAGE TANKS (SAMPLE) (CONTINUED) Baseline Control Control device Scrubber HAP control efficiency (%) Calculations1* ______99% eff Breathing Loss (Mg/yr) = _ 10.88 Lb = 1.02E-05 (Mv) SEL (91-7WsW`50(^(C)(Ky (PA) ` (P> - 1.02E-05 (36.46) (6)1-73(4)-8,(18)oso(1.3)(0.2824)(1) 2.17xl0"5 Mg/yr Working Loss (Mg/yr)= 1^ - 1.09E-08 MVP VNKnKc " 1.09E-08(36.46)(0.000435)(1,900)(481.05)(0.23)(1) = 3.62xl0-5 Mg/yr Total Loss (Mg/yr) = TL = LB + L,, - (2.17 X 10"5) + (3.62 x 10-5) 5.79xl0"5 Mg/yr If a control device is employed, HAP Emissions (E^pj = Total Loss (1 - eff/100) - 5.79 x 10-5 (1 - 99/100) 5.79X10-7 Mg/yr SL 025897 B-10 Source: HON subunit(s) Chlorine Unit (Cl:) CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM FIXED ROOF STORAGE TANKS (SAMPLE) (CONTINUED) Calculation (Continued) Weighted HAP Emissions1 ~ ehap = (5.79 x 10"5) fhr (l) 5.79xl0"7 Mg/yr aIf vapor space height is unknown for shell, assume H equals one half tank height. If tank has a cone roof, adjust vapor space height by adding 1/3 of height of cone. bIf average ambient diurnal temperature change is unknown, assume 20F. cStored liquid temperature may be approximated from average annual ambient temperature. dN = AH where N = number of turnovers per year V AN = total throughput per year (gal) V = tank capacity (gal) For D> 30ft, C*l; For 6 <, D < 30 ft, C = 0.0771D-0.0013D2-0.1334. fFor turnovers > 36, KN * (180 + N)/(6 * N) where KN = turnover factor (dimensionless) N * number of turnovers per year For turnovers <, 36, KN * 1 gKc = 1.0 for volatile organic liquids hExpression for computing HAP emissions are from "Procedures for Establishing Base Year and Post-Reduction HAP Emissions." The calculation procedure is consistent with AP-42. iFor emissions of other HAPs from this EIQ, see summary of calculated emissions from fixed roof storage tanks. SL 025898 SL 025899 PPG 05/20/92 SUMMARY OF THE CALCULATION INPUTS FOR FIXED-ROOF STORAGE TANKS ASSOCIATED WITH THE CHLORINE PROCESS UNIT (CL2) EIQ Tank NO. ID Tank Description HAP 365 60-1602 Brins/ HCLNeuL Reactor Tank Vent Scrubbf-i20* 365 60-1602 Brine/ HCL Neut Reactor Tank Vert ScnbbHCL 369 60016 #1 HCL Storage Tank H20* 369 60-918 #1 HCL Storage Tank HCL 369 60019 #2 HCL Storage Tank H20* 369 60-019 #2 HCL Storage Tank HCL 370 60927 HCL Add Head Tank Scnbber H20* 370 60927 HCL Acid Head Tank Scribber HCL 371 60-1526 D.l. Tank (HCL) H20* 371 60-1526 D.l. Tank (HCL) HCL Mole Percent Tank Color D Inside Diameter (1L) V Capacity <9*) H Vapor Space Height <fL) Te Stared Liquid Temp. (oF) N Mv P Fp C Number of Molecular Partial Paint Small KN Turnovers Weight Pressise Factor Diameter Tirnever per Year (b/b mole) (psia) Fader Factor 69.00 11.00 62.52 17.48 82.52 17.46 76.98 19.23 97.48 2.54 Yellow Yellow Amber Amber Amber Amber Yellow Yellow Brown Brown 6.00 6.00 12.00 1200 12.00 12.00 10.00 10.00 20.00 20.00 1900 1900 31300 31300 31300 31300 6500 6500 75000 75000 4.00 4.00 10.00 10.00 10.00 10.00 6.00 6.00 16.00 16.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 461.05 481.05 47.43 47.43 23.71 23.71 96.47 96.47 0.20 0.20 18.020 36.460 18.020 36.460 18.020 36.460 18.020 36.460 18.020 36.460 0.177 0.000 0.086 0.036 0.086 0.036 0.063 0.039 0.300 0.000 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.40 1.40 0.2624 0.2824 0.6046 0.6046 0.6046 0.6046 0.5076 0.5076 0.8886 0.8886 0.23 0.23 0.80 0.80 1.00 1.00 0.48 0.48 1.00 1.00 = NON HAP. Emission is not included as a HAP emission. PPG 05/20/92 SUMMARY OF CALCULATED EMISSIONS FROM FIXED-ROOF STORAGE TANKS ASSOCIATED WITH THE CHLORINE PROCESS UNIT (CL2) t? Era Tank NO. ID Tank Description HAP 025900 365 60-1602 Brine/HCl NeuL Reactor Tank Vent Scrubber H20* 365 60-1602 Brine/ HCL Neut Reactor Tank Vent Scrubber HCL 369 60-916 #1 HCL Storage Tar* H20* 369 60-918 #1 HCL Storage Tank HCL 369 60919 #2 HCL Storage Tar* H20* 369 60919 #2 HCL Storage Tar* HCL 370 60927 HCL Add Head Tar* Scrubber H20* 370 60927 HCL Add Head Tar* Scrubber HCL 371 60-1526 D.L Tar* (HCL) H20* 371 60-1526 D.L Tar* (HCL) HCL <3 4> LB Breathing Loss (Mg/yr) 0.00000 0.00002 0.00000 0.00495 0.00000 0.00495 0.00000 0.00249 0.00000 0.00001 LW Working Lose (Mg/yr) 0.00000 0.00004 0.00000 0.01690 0.00000 0.01057 0.00000 0.00469 0.00000 0.00000 LT Total Loss (Mg/yr) Conkol Device 1907 Control Unweighted Efficiency HAP Emissions (%) (Mg/yr) 1907 Weighted HAP Emissions (Mg/yr) 0.00000 0.00006 0.00000 0.02184 0.00000 0.01552 0.00000 0.00718 0.00000 0.00001 Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber 0.00 99.00 0.00 99.00 0.00 99.00 0.00 99.00 0.00 99.00 O.OOE+OO 5.79E-07 O.OOE+OO 2.16E94 O.OOE+OO 1.55E-04 O.OOE+OO 7.18E-05 O.OOE+OO 9.83E-08 O.OOE+OO 5.79E-07 O.OOE+OO 2.18E94 O.OOE+OO 1.55E-04 O.OOE+OO 7.18E05 O.OOE+OO 9.83E-08 * = NON HAPS, mission is not included as a HAP emission EKR APPENDIX B-B CHLORINE PROCESS UNIT PROCESS VENT CALCULATIONS ssionoie.oiA SL 025901 B-14 Final 05/27/92 Source: HON subunit(s)___ Chlorine Process Unit CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: Mercury fHq)_______________________ Year: 1987 Calculator: Date: April 1992 S.R. Process Vent Identification: 100 Description: __Mercury Cell Hydrogen Vent_______________________ Process Conditions/Sampling Date of flow measurement Method of flow measurement EPA Methods 1-4 Date of concentration measurement Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) EPA Method 101 Describe any problems encountered during testing None Identified Production rate during flow determination (lbs/hr) Production rate during sampling (lbs/hr) Average production rate during base year (lbs/hr) 1287 1987 262., 194 16^.94 ^62^194 Stream Characteristics Average vent stream flow rate (ft3/min) HAP concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risk weighting factor 4.892 n 427 87 201 14.7 l =Q =C =h =T = MW =P Con&TPl Control device Vapor Recovery__________________ HAP control efficiency (%) 98 = eff Calculations* Uncontrolled Emissions (E0) f2.54E-09^ 0 c h MW P T + 460 Uncontrolled Emissions (E0) = (2.54E-09)(4.892) (11) (427) (201) (14.7) (87) + 460 0.315 Mg/yr HAP Emissions (E^) = E0 (1 - eff/100) SL 025902 B-15 Source: HON subunit(s) Chlorine Process Unit CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (Ejy^p) = 0.315 (1 - 98/100) 0.006 Mg/yr Weighted HAP Emissions Weighted HAP Emissions ehap (0.007) fhr (1) 0.006 Mg/yr If the conditions during testing are not representative of has year operation, make the appropriate extrapolation below and xplain: N/A If the flow or concentration were not measured using an EPA reference method, EPA conditional method or validated using Method 301, provide justification and supporting calculations: N/A Expression provided in "Procedures for Establishing Base Year and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. SL 025903 B-16 Source: HON subunit(s) Chlorine Process Unit CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: Chlorine (Cl^____________________ Year: 1987 _______________________ Date: April 1992 Calculator: S.R. Process Vent Identification: 101 Description: Mercury Cell Cl2_Neutralization Tower Process Conditions/Samplinq Date of flow measurement Method of flow measurement Process Design Rate Date of concentration measurement Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) CEM_____________ Describe any problems encountered during testing Hpfl? Identified Production rate during flow determination (lbs/hr) Production rate during sampling (lbs/hr) Average production rate during base year (lbs/hr) .1987 not available not available 262.194 Stream Characteristics Average vent stream flow rate (ft3/min) HAP concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risk weighting factor 3,528. 33 8.562 100 70 14.7 l Control Control device Scrubber_______________________ HAP control efficiency (%) 97 = eff Calculations* Uncontrolled Emissions (Ew) = {2.54E-091 O C h MW P T + 460 Uncontrolled Emissions (E,,) = (2.54E-09)(3.528)(33^ f8.562)f70)(14.71 (100) + 460 4.652 Mg/yr HAP Emissions (E^) = E0 (1 - eff/100) SL 025904 B-17 Source: HON subunit(s) Chlorine Process Unit CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (E^p) 4.652 (1 - 97/100) 0.14 Mg/yr Weighted HAP Emissions = EHAP Weighted HAP Emissions 0.14) fhr (1) 0.14 Mg/yr If the conditions during testing are not representative of base year operation, make the appropriate extrapolation below and explain: N/A If the flow or concentration were not measured using an EPA reference method, EPA conditional method or validated using Method 301, pr vide justification and supporting calculations: The flow rate is representative of the maximum design flow rate and the Cl2 concentration is based on an averaged CEM data. Expression provided in "Procedures for Establishing Base Year and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. SL 025905 B-18 Source: HON subunitfs) chlorine Process Unit CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: Mercury (Hq)_______________________ Year: 1987 Calculator: Date: April 1992 S.R. Process Vent Identification: 102 Description: Fume System (Endbox Ventilation System)_______ Process Conditions/Sampling Date of flow measurement Method of flow measurement EPA Methods 1-4 Date of concentration measurement Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) EPA Method 101 Describe any problems encountered during testing None Identified Production rate during flow determination (lbs/hr) Production rate during sampling (lbs/hr) Average production rate during base year (lbs/hr) 1986 1986 235.512 235.512 262.194 Stream Characteristics Average vent stream flow rate (ft3/min) HAP concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risk weighting factor 2.825 = Q 12 = c 8.568 = h 59 = T 201 = MW 14.7 = P l = FHR Control Control device Vapor Recovery HAP control efficiency (%) 99 = eff Calculations* Uncontrolled Emissions (Ew) * f2.54E-09l o c h MW P T + 460 Uncontrolled Emissions (Ejj) = (2.54E-09) (2.8.2.5.) U.2) (8.568) (201) (14.7) (59) + 460 4.2 Mg/yr HAP Emissions (E^p) = E0 (1 - eff/100) SL 025906 B-19 Source: HON subunit(s) Chlorine Process Unit CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS ____FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (Ej^) = 4.2 (1 - 99/100) 0.042 Mg/yr Weighted HAP Emissions Weighted HAP Emissions ehap (0.042) fhr (1) 0.042 Mg/yr If the conditions during testing are not representative of base year operation, make the appropriate extrapolation below and xplain: Flow rate and sampling analysis were done in 1986. Chlorine manufactured in 1986 and 1987 (base year) were very close. No extrapolation was conducted. If the flow or concentration were not measured using an EPA reference method, EPA conditional method or validated using M thod 301, provide justification and supporting calculations: N/A Expression provided in ''Procedures for Establishing Base Year and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. SL 025907 B-20 Sourc : HON subunit(s) Chlorine Process Unit CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: Chlorine____________________________ Year: 1987 Calculator: Date: April 1992 S.R. Process Vent Identification: 105 Description: Plant C Absorber___________________________________ Process Conditions/Sampling Date of flow measurement ----- Method of flow measurement Process Design Rate Date of concentration measurement ----- Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) Engineering Judgement Describe any problems encountered during testing None Identified Production rate during flow determination (lbs/hr) 262.194 Production rate during sampling (lbs/hr) 262.194 Average production rate during base year (lbs/hr) 262.194 Stream Characteristics Average vent stream flow rate (ft3/min) HAP concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risk weighting factor 48.300 l.ooo 10 70 70 14.7 l Cantral Control device Scrubber_______________________________________ HAP control efficiency (%) 99.9 = eff Calculationsa Uncontrolled Emissions (E0) = (2.54E-091 o C h MW P T + 460 Uncontrolled Emissions (0) = (2.54E-09)(48.300)fl.000)(101f701(14.71 (70) + 460 2.382 Mg/yr HAP Emissions (E^p) * E0 (1 - eff/100) 025908 Sourc : HON subunit(s) Chlorine Process Unit CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (E^p) * 2.382 (1 - 99.9/100) 0.002 Mg/yr Weighted HAP Emissions Weighted HAP Emissions ehap (0.002) ehr (1) 0.002 Mg/yr If the conditions during testing are not representative of has year operation, make the appropriate extrapolation below and xplaint N/A If the flow or concentration were not measured using an EPA reference method, EPA conditional method or validated using M thod 301, provide justification and supporting calculations: N/A Expression provided in "Procedures for Establishing Base Year and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. SL 025909 B-22 Source: HON subunit(s) Chlorine Process Unit CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: Chlorine____________________________ Year: 1987 Calculator: Date: April 1992 S.R. Process Vent Identification: 106 Description: __circuit 15 Neutralizing Tower___________________ Process Conditions/Sampling Date of flow measurement Method of flow measurement Calculated Date of concentration measurement Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) Calculated Describe any problems encountered during testing None Identified Production rate during flow determination (lbs/hr) Production rate during sampling (lbs/hr) Average production rate during base year (lbs/hr) --------- 235.512 235.512 262.194 Stream Characteristics Average vent stream flow rate (ft3/min) HAP concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risk weighting factor 3.020 ,34!L 140 TSL 11*2. Control Control device Scrubber________________________________ HAP control efficiency (%) 99.9 = eff Q c h T MW P FHR Calculations* Uncontrolled Emissions (Ew) - (2.54E-091 o c h MW P T + 460 Uncontrolled Emissions (Ew) = f2.54E-09)f3.020)f345112) (70)(14.7) (140) + 460 0.009 Mg/yr HAP Emissions (E^p) = Eu (1 - eff/100) SL 025910 B-23 Sourc : HON subunit(s) _Chlorine Process Unit CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (E^p) = 0.009 (1 - 99.9/100) 0.0 Mg/yr Weighted HAP Emissions = E^p F^ Weighted HAP Emissions - (0) (1) 0.0 Mg/yr If the conditions during testing are not representative of bas year operation, make the appropriate extrapolation below and xplain: N/A If the flow or concentration were not measured using an EPA reference method, EPA conditional method or validated using Method 301, provide justification and supporting calculations: Chlorine flow rate at 75 kilo amp. * 41,542 lb/hr At 45 kilo amp. = 41,542 x - 24,925 lb/hr 75 Air in Cl2 on startups as 40% air. Therefore, 24,925 x Ifr-fflglg x Jn_ x 379 ft3 x 0.4 Air = 1478 scfm, air 71 lb 60 min lb-mole 0.6 Cl, Tower Vent Flow - 1478 x 630 520 = 1791 acfm, air Mole fraction of H20 = 1^22 14.7 = 0.407, mole fraction of air = 0.593 Therefore, total vent flow = 1791 = 3020 acfm 0.593 Expression provided in "Procedures for Establishing Base Year and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. SL 025911 B-24 Source: HON subunit(s) Chlorine Process Unit CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: Chlorine (Cl2)______________________ Year: 1987____________.______________ Date: April 1992 Calculator: S.R. Process Vent Identification: 107 Description: __Circuit 16 Neutralizing Tower___________________ Process Conditions/Sampling Date of flow measurement Method of flow measurement Calculated Date of concentration measurement Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) Calculated Describe any problems encountered during testing Mong-lflentlfled Production rate during flow determination (lbs/hr) Production rate during sampling (lbs/hr) Average production rate during base year (lbs/hr) --------- 235.512 235.512 262.194 Stream Characteristics Average vent stream flow rate (ft3/min) HAP concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risk weighting factor 3-uO ?Q 3.45 = Q C 3140__________ = T 70__________ * MW ____11,7 - - P 1= h F,,, Control Control device Scrubber____________ HAP control efficiency (%) 99.9 = eff Calculations* Uncontrolled Emissions (Eg) = (2.54E-091 o C h MW P T + 460 Uncontrolled Emissions (E0) * (2.54E-09113.020)(345112\(1Q\ (14.71 (140) + 460 0.009 Mg/yr HAP Emissions (E^p) = Ew (1 - eff/100) B-25 Source: HON subunit(s) Chlorine Process Unit CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (E^p) = 0.009 (1 - 99.9/100) 0.0 Mg/yr Weighted HAP Emissions = I weighted HAP Emissions = 0.0 Mg/yr If the conditions during testing srs not representative of bas year operation, make the appropriate extrapolation below and explain: N/A If the flow or concentration were not measured using an EPA reference method, EPA conditional method or validated using Method 301, provide justification and supporting calculations: Chlorine flow rate at 75 kilo amp. = 41,542 lb/hr At 45 kilo amp. = 41,542 x 15 - 24,925 lb/hr 75 Air in Cl2 on startups 40% air. Therefore, 24,925 x lb-mole x hr x 379 ft3 x 0,4 Air = 1478 scfm, air 71 lb 60 min lb-mole 0.6 Cl2 Tower Vent Flow = 1478 x 630 520 = 1791 acfm, air Mole fraction of H20 - 5.99 14.7 0.407, mole fraction of air * 0.593 Therefore, total vent flow = 1791 * 3020 acfm 0.593 Expression provided in "Procedures for Establishing Base Year and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. B-26 Source: HON subunit(s) Chlorine Process Unit CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: Chlorine____________________________ Year: 1987 Calculator: Date: April 1992 S.R. Process Vent Identification: 109 Description: Sulfur Chloride Vent______________________________ Process Conditions/Sampling Date of flow measurement 1987 Method of flow measurement Process Flow Meter Date of concentration measurement 1987 Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) Hexane Imoinaer/IR Spectroscopy Describe any problems encountered during testing None Identified Production rate during flow determination (lbs/hr) 262.194 Production rate during sampling (lbs/hr) 262.194 Average production rate during base year (lbs/hr) 262.194 Stream Characteristics Average vent stream flow rate (ft3/min) HAP concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risk weighting factor 740 42 8.760 -10 70 14.7 l ggntrol Control device Vapor Recovery________________ HAP control efficiency (%) 99.9 eff Calculations* Uncontrolled Emissions (Eg) (2.54E-091 0 c h MW P T + 460 Uncontrolled Emissions (E0) * (2.54E-09)f740^(42)(B.760)(70)(14.7) (-10) + 460 1.581 Mg/yr HAP Emissions (E^p) Ew (1 - eff/100) SL 025914 Source: HON subunit(s) Chlorine Process Unit CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (Ejy^,) * 1.581 (l - 99.9/100) 0.0016 Mg/yr Weighted HAP Emissions = Ej^ FHR Weighted HAP Emissions * (0.0016) (l) 0.0016 Mg/yr If the conditions during testing are not representative of base year operation, make the appropriate extrapolation below and xplaint N/A If the flow or concentration were not measured using an EPA reference method, EPA conditional method or validated using Method 301, provide justification and supporting calculations: N/A Expression provided in "Procedures for Establishing Base Year and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. SL 025915 B-28 APPENDIX C ETHYL CHLORIDE PROCESS UNIT (EC) AND HYDROGEN CHLORIDE PROCESS UNIT (HCL) SL 025916 551OROI 6.01 Final 05/27/92 APPENDIX C ETHYL CHLORIDE PROCESS UNIT (EC) AND HYDROGEN CHLORIDE PROCESS UNIT (HCL) C.1 Process Description The Ethyl Chloride Unit is designed to produce a high purity liquid ethyl chloride (EC) product by reacting anhydrous hydrogen chloride (HCI) and ethylene. The reaction is as follows: Ethylene (C2H*) + Hydrogen Chloride ------------- Ethyl Chloride Catalyst (HCI) (C2HsCI) The reaction between these two gases takes place under pressure in the presence of a catalyst in a liquid phase reactor. Figure C-1 outlines the major steps in ethyl chloride production. Non-volatile tars and catalysts remaining after boiling off EC in the reactor are transferred in a portable tank to the Waste Treatment Unit. Heavy impurities that remain after removal of HCI impurities from the EC in the primary stripper are removed by a "heavies* still and sent to the Bottoms Recovery Unit, which is included in the Waste Treatment Unit. EC is shipped by truck and railcar to customers. The major equipment used in the EC production includes a reactor, coolers, a condenser, strippers, a distillation column, and day and dock storage tanks. A process schematic showing the major equipment is shown in Figure C-2. The Hydrogen Chloride unit is in the Ethyl Chloride processing area. Figure C-3 shows the process steps. The Hydrogen Chloride Unit is designed to perform the following jobs: 1) Store weak acid produced by the incinerators and distribute it to consumers inside the plant and customers outside the plant. 2) Purify weak acid in weak acid purification equipment for use in the Mercury Cell Area. 5510R016.01A C-1 Fins) OS/27/92 Figure C-1: EC Process Schematic See Volume II - Confidential EN3t 02591 S510R016.01A C-2 Final 05/27/92 Figure C-2: Ethyl Chloride See Volume II - Confidential ------sv S510R016.01A 9^ C-3 Final 05/27/92 Figure C-3: HCI Process Schematic See Volume II - Confidential SL 025920 5510R016.01A C*4 Final 05/27/92 3) Utilize anhydrous HCI gas to produce strong acid to supply consumers inside the plant when weak acid is not available. The major equipment used in the HCI unit are carbon filters, absorbers, storage tanks, and a vent scrubber. C.2 1987 Base-Year Emissions Table C-1 shows the total base-year emissions for the EC and the HCI process units. The total unweighted HAP emissions were 4.286 Mg/yr and the weighted HAP emissions were 5.461 Mg/yr. C.3 Emissions Reduction Strategy The EC and HCI process units have three process vents. Two of these have a scrubber for the control of emissions (EIQ 304 and 338), and the emissions from the remaining process vent (EIQ 337) are currently being incinerated. Emissions from EIQ 304 (startup mode only) will be incinerated as part of the early reduction program. (See Tables C-1 and C-2.) C.4 Post-Reduction Emissions Table C-3 shows the total post-reduction unweighted and weighted HAP emissions for the EC and HCI process units. The total post-reduction unweighted emissions of 0.141 Mg/yr represent a 96.71% decrease in unweighted base-year emissions. The total post-reduction weighted emissions of 1.316 Mg/yr represent a 75.91% decrease in weighted base-year emissions. SL 025921 S510R016.01A C-5 Final 05/27/92 tO-*l Kf\CoN)oon) TABLE C-1 1987 BASE YEAR EMISSIONS ETHYL CHLORIDE PROCESS UNIT (EC) HYDROGEN CHLORIDE PROCESS UNIT (HCL) BASE YEAR UNIT EIQ EC/HCL EC/HCL EC/HCL 304 337 338" EC/HCL 373 EC/HCL 374 DESCRIPTION EC Scrubber VCM-I Plant Scrubber HCI Tails Tower Scrubber North Rubber Lined Acid Tank South Rubber Lined Acid Tank TYPE P P P T T CONTROL DEVICE HAP EM SSIONS % UNWEIGHTED WEIGHTED TYPE CONTROL* MG/YR MG/YR Scrubber 5.00 4.146 4.146 Incinerator 99.99 0.000 0.000 Scrubber 5.00 0.139 1.314 Subtotal Process Vents 4.285 5.46 Scrubber 99.00 0.000 0.000 Scrubber 99.00 0.001 0.001 Subtotal Tank Vents 0.001 0.001 _____________________________________1 * Control officbnciM hr scrubber* represent efficiencies far hyrfrocarbons, these scrubbers have 99% efficiency far HCI. " EK3 338 also conSols emissions from several tanks. These emissions were calculated to be 0.0011 (see tank calculations on pages C-13and C-14) and are included In the emissions shown. Total Base Year Emissions 1 4.286 5.461 FILE: ECBASE tC-Or o VOtOor to Co TABLE C-2 EMISSIONS REDUCTIONS STRATEGY AND POST REDUCTION EMISSIONS ETHYL CHLORIDE PROCESS UNIT (EC) HYDROGEN CHLORIDE PROCESS UNIT (HCL) unit EIQ EC/HCL EC/HCL EC/HCL 304**' 337 338** EC/HCL EC/HCL 373 374 DESCRIPTION EC Scrubber VCM-I Plant Scrubber HCI Tails Tower Scrubber North Rubber Lined Acid Tank South Rubber Lined Acid Tank TYPE P P P T T POST REOUCTiON ADDITIONAL CONTROL 1994 % CONTROL* Inclnwfttor 99.99 None 99.99 Nona 5.00 Subtotal Process Verde Nona 99.00 Nona 99.00 Subtotal Tank Vents HAP EMISSIONS UNWEIGHTED WEIGHTED MG/YR MG/YR 0.001 0.001 0.000 0.000 0.139 1.314 0.14 1.315 0.000 0.000 0.001 0.001 0.001 0.001 ___________________________________________________1 Total Post Reduction Emissions * Contot efficiencies far scrubbers represent efficbnciee far hydrocarbons, thasa scrubbers hava 99% efficiency far HCI. * * EIQ 33S also conSofa amissions from savaral tanks. Thasa amissions wars calculated to ba 0.0011 (saa tank calculations on pagaaC-10 and C-11) and ars included in the amissions shown. * * * These vents hava three operating scenar Ios: non-routine (NR), startup (Su), and shut down (SD). Only die SU and SO modes will be incinerated at 99.99% efficiency. The NR emissions will ba vented through the scrubber. | 0.141 1.316 FILE: ECPOST tC-O* TABLE C-3 HAP EMISSIONS SUMMARY ETHYL CHLORIDE PROCESS UNIT (EC) HYDROGEN CHLORIDE PROCESS UNIT (HCL) Unweighted HAP Emissions Weighted HAP Emissions Post Parcent Post Percent o do Type Bate Year Reduction Reduction Base Year Reduction Reduction (Units) (Mg/yr) (Mg/yr) (%> (Mg/yr) (Mg/yr) <*) P 4.28S 0.140 96.73 5.461 1.315 75.92 T 0.001 0.001 0.00 0.001 0.001 0.00 F Total Total Percent Reduction 4.286 0.141 96.71 5.462 1.316 75.91 P-ProcM V*rrt T-Tank Vnta F - Fugitfv* Emissions EM3* APPENDIX C-A EC PROCESS UNIT STORAGE TANK CALCULATIONS 5510H016.01A Si 025925 C-9 Final 05/27/92 Source: HON subunit(s) Ethvlene Chloride (EC) CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM FIXED ROOF STORAGE TANKS (SAMPLE) HAP: Hydrogen Chloride (HC1)_________ Year: 1987 __________ Date: 05/13/92 Calculator: J. Greer Tank Designation: EIO 373. North Rubber-lined Tank (60-970) Product: HC1 Acid (20%)________________________________________________ Tank Characteristics Inside diameter, (ft) Height, (ft) Capacity, (gal) = n * 7.48 gal, 4 ft? if not known Roof color White Shell color White Vapor space height, (ft)a Ambient. Conditions Average atmospheric pressure (psia) (defaults 14.7 psia) Average ambient diurnal temperature (F)b Average annual ambient temperature (F) Bulk Liauid_Characteristics Stored liquid temperature (F)C Total throughput per year (gal) Number of turnovers per yeard Molecular weight of HAP (lb/lb mole) Mole percent of HAP Partial pressure of the HAP at liquid conditions (psia) Adjustment Factors Paint factor Small diameter tank factor Turnover factorf Product factor9 ______30 ______30 143.640 ______15 ______14.7 ______18 ______70 70 566.652.4 -- -3.94 36.46 ______ U-iflO. _______ 0.004 ________i.o ________l.o ________i.o ________i.o D HT V H Pa dT TS an N Mv % P Fp C kn KC SL 025926 C-10 Sourc : HON subunit(s) Ethvl Chloride (Ecn CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM FIXED ROOF STORAGE TANKS (SAMPLE) (CONTINUED) Baseline Control Control device Gas Scrubber HAP control efficiency (%) Calculations11 99 = eff Breathing Loss (Mg/yr) 10.68 Lb = 1.02E-05 (Mv) IEL (P)'TM(H)*'(cr7)00S.500(/Fp)(C)(Kc) (Pa) - (Pi * 1.02E-05 (36.46) '"(15)"(18)(1 )(1 )(1) 0.0084 Mg/yr Working Loss (Mg/yr) =L,, = 1.09E-08 MyPVNKjjKj, =1.09E-08(36.46)(0.004)(143,640)(3.94)(1)(1) Total Loss (Mg/yr) tl * Lb + Lw If a control device is employed, HAP Emissions (E^j SL 025927 = Total Loss (1 - eff/100) = 0.00929 (1 - 99/100) 9.29X10"5 Mg/yr C-ll Source: HON subunit(s) Ethvl Chloride fEen CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM FIXED ROOF STORAGE TANKS (SAMPLE) (CONTINUED) Calculation (Continued! Weighted HAP Emissions1 ehap - fhp (9.29 X 10~5)_________(1) 9.29X10-5 Mg/yr aIf vapor space height is unknown for shell, assume H equals one half tank height. If tank has a cone roof, adjust vapor space height by adding 1/3 of height of cone. bIf average ambient diurnal temperature change is unknown, assume 20F. cstored liquid temperature may be approximated from average annual ambient temperature. dN = where N = number of turnovers per year V AN total throughput per year (gal) V * tank capacity (gal) For Di 30ft, C=l; For 6 5 D < 30 ft, C = 0.0771D-0.0013D2-0.1334. fFor turnovers > 36, KN = (180 + N)/(6 * N) where KN = turnover factor (dimensionless) N * number of turnovers per year For turnovers 36, K,, 1 gKc * 1.0 for volatile organic liquids hExpression for computing HAP emissions are from "Procedures for Establishing Base Year and Post-Reduction HAP Emissions." The calculation procedure is consistent with AP-42. iFor emissions of other HAPs from this EIQ, see summary of calculat d missions from fixed roof storage tanks. 0259^ SL C-12 si. 025929 PPG 05/20/92 SUMMARY OF THE CALCULATION INPUTS FOR FIXED-ROOF STORAGE TANKS ASSOCIATED WITH THE ETHYL CHLORIDE PROCESS UNIT (EC) EIQ Tank NO. ID Tank Description 338(1)60811 Strong #1 HCL Add Tank 338(1)60-611 Stong #1 HCL Add Tank 338{t)60612 Stong #2 HCL Add Tank 338(t)60612 Strong #2 HCL Add Tank 338(1)60613 Weak #1 HCL Add Tank 338(1) 60613 Weak #1 HCL Add Tank 338(1)60614 Weak #2 HCL Add Tank 3380)60614 Weak #2 HCL Add Tank 373 60670 North Rubber Lined Add Tank 373 60670 North RUbber Lined Add Tank 374 60-1192 South Rubber Lined Add Tank 374 60-1192 South Rubber Lined Add Tank HAP H20* HCL H20* HCL H20* HCL H20* HCL H20 HCL H20* HCL Mole Percent Tank Color 0 Inside Diameter (It) V Capacity (9d.) H Vapor Space Height (It) Ts Stored liquid Temp. (oF) N Mv P Fp C Number of Molecular Partial Paint Small KN Tirnovers Weight Pressire Fader Diameter Tirnover per Year (fa/I) mole) (psla) Factor Factor 62.52 17.48 62.52 17.48 89.00 11.00 89.00 11.00 89.00 11.00 82.52 17.48 Yellow Yellow Yellow Yellow Green Green Green Green White White White White 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 30.00 30.00 43.00 43.00 20000 20000 20000 20000 20000 20000 20000 20000 143640 143640 325600 325800 13.00 13.00 13.00 13.00 13.00 13.00 13.00 13.00 15.00 15.00 15.00 15.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 42.77 42.77 42.77 42.77 44.86 44.88 44.88 44.88 3.94 3.94 11.69 11.69 18.020 36.460 18.020 36.460 18.020 36.460 18.020 36.460 18.020 36.460 16.020 36.460 0.1046 0.2050 0.1046 0.2050 0.1990 0.0040 0.1990 0.0040 0.1990 0.0040 0.1046 0.2050 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 0.87 0.87 0.87 0.87 0.84 0.84 0.84 0.84 1.00 1.00 1.00 1.00 (t) = This tank emits through EIQ 338 which Is a soiree. Emissions trom this tank are included in the emissions shown on Tables 0-1 and 02. = NON HAP, Emission is no* included as a HAP emission. SL 0 2 5 9 3 0 PPG 05/2Q/92 SUMMARY OF CALCULATED EMISSIONS FROM FIXED-ROOF STORAGE TANKS ASSOCIATED WITH THE ETHYL CHLORIDE PROCESS UNIT (EC) EIQ Tank NO. 10 Tank Description 338(1} 338(1} 338(t) 338(Q 338(9 338(9 336(9 338(9 373 373 374 374 60-611 60-611 60-612 60612 60613 60-613 60614 60614 60670 60670 601192 601192 Strong #1 HCL Add Tar* Stong#1 HCL Add Tank S*ong#2HCL Add Tank Stong #2 HCL Add Tank Weak #1 HCL Add Tank Weak #1 HCL Add Tank Weak #2 HCL Add Tank Weak #2 HCL Add Tank North Rubber Uned Add Tank North Rubber Lined Add Tank South RU*mt Lined Add Tank South Rubber Uned Add Tank HAP H20* HCL H20* HCL H20* HCL H20* HCL H20* HCL H20* HCL LB Breathing Loss (Mg/yr) 0.00000 0.01868 0.00000 0.01866 0.00000 0.00126 0.00000 0.00126 0.00000 0.00643 0.00000 0.23234 LW Working Loss (Mg/yr) 0.00000 0.06060 0.00000 0.06060 0.00000 0.00118 0.00000 0.00118 0.00000 0.00069 0.00000 0.31024 LT Total Loss (Mg/yr) Corrtrd Device 1987 Conkd Unweighted Efficiency HAP Emissions <%> (Mg/yr) 1987 Weighted HAP Emissions (Mg/yr) 0.00000 0.07916 0.00000 0.07916 0.00000 0.00244 0.00000 0.00244 0.00000 0.00933 0.00000 0.542S8 Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber 0.00 99.00 0.00 99.00 0.00 99.00 0.00 99.00 0.00 99.00 0.00 99.00 O.OOE-HX) 7.92E-04 0.00E+00 7.92E-04 0.00E+00 2.44E65 0.00E+00 2.44E65 0.00E+00 9.33E-05 0.00 E+00 5.43E-03 0.00 E+00 7.92604 0.00 E+00 7.926-04 0.006+00 2.44E-05 0.006+00 2.44605 0.006+00 9.33605 O.OOE+OO 5.43603 (t) = This tank emits through EK9 338 which is a soiree. Emissions from this tank are included in the emissions shown on Tables C-l and C-2. = NON HAPS, emission is not included as a HAP emission Source: HON subunit(s) Ethvlene Dichloride fEDO_______________ HAPs mitted: Ethvlene Dichloride (EDO. Hexachloro 1.3-Butadiene (HCBD) . Hexachloroethane (HEXA) . 1.1,2.2-Tetrachloroethane (SYM) , 1.1.2-Trichloroethane (TCE)_____________ CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM FIXED ROOF STORAGE TANKS (SAMPLE) HAP: Ethvlene Dichloride fEDC)______ Year: _____1987 __________ Date: 05/13/92 Calculator: J. Greer Tank Designation: EIO 312. EDC Bottoms Tank No. 4 (60-0340) Product: Ethvlene Dichloride EDC Tank Characteristics Inside diameter, (ft) Height, (ft) Capacity, (gal) = n P2h * 7.48 gal. 4 fP if not known Roof color Green Shell color Green Vapor space height, (ft)a fonkient cgnflitiong Average atmospheric pressure (psia) (defaults 14.7 psia) Average ambient diurnal temperature (F)b Average annual ambient temperature (F) Bulk Liquid Characteristics Stored liquid temperature (F)C Total throughput per year (gal) Number of turnovers per yeard Molecular weight of HAP (lb/lb mole) Mole percent of HAP Partial pressure of the HAP at liquid conditions (psia) Adjustment Factors Paint factor Small diameter tank factor' Turnover factor* Product factor9 12 30 25.400 T 15 ______14.7 ______18 ______70 =H = PA * dT = TA ______80 358.850.3 ______14.13 ______98.97 ______76.55 _______ 1.294 -= % =p 1*3_____ k, ,6_ l.O 1.0 = Fp =C * Kn - Kc SL 025954 D-10 Source: HON subunit(s) Ethvlen Dichloride (EDCV__________ HAPs mitted: EPg,___ HCBD. HEXA, SYM, TCE_________________________ CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS ___________FROM FIXED ROOF STORAGE TANKS (SAMPLE) (CONTINUED) BasaUne control Control device Scrubber HAP control efficiency (%) Calculations11 _______ 5% eff Breathing Loss (Mg/yr) = ' 0 68 Lb = 1.02E-05 (Mv) _J2_ <V*W-6Ww(^(C)(Ky (Pa) - (P) = 1.02E-05 (98.97) !^Lp(i2)vn(15)Mi(,8)(i.3)(0.6046)(1) 0.201 Mg/yr Working Loss (Mg/yr) L,, - 1.09E-08 MvPVNKnKc 1.09E-08 (98.97)(1.294)(25,400)(14.13)(1) (1) Total Loss (Mg/yr) * TL = LB + = (0.201) + (0.500) If a control device is employed, HAP Emissions (E^pj 0.701 Mg/yr = Total Loss (1 - eff/100) - 0.701 (1 - 5/100) 0.666 Mg/yr SL 025955 D-ll Source: HON subunit(s) Ethvlene Dichloride (EDO HAPs emitted: EDC. HCBD. HEXA. SYM. TCE______________ CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM FIXED ROOF STORAGE TANKS (SAMPLE) (CONTINUED) Calculation (Continued) Weighted HAP Emissions1 = Ej^ FHR - (0.666) ( 1 ) " 0.666 Mg/yr aIf vapor space height is unknown for shell, assume H equals one half tank height. If tank has a cone roof, adjust vapor space height by adding 1/3 of height of cone. bIf average ambient diurnal temperature change is unknown, assume 20F. cStored liquid temperature may be approximated from average annual ambient temperature. dN = iyi where N * number of turnovers per year V AN = total throughput per year (gal) V = tank capacity (gal) eFor D> 30ft, C=l; For 6 < D < 30 ft, C = 0.0771D-0.0013D2-0.1334. fFor turnovers > 36, KN = (180 + N)/(6 * N) where KN = turnover factor (dimensionless) N * number of turnovers per year For turnovers 36, KN = 1 gKc = 1.0 for volatile organic liquids hExpression for computing HAP emissions are from "Procedures for Establishing Base Year and Post-Reduction HAP Emissions." The calculation procedure is consistent with AP-42. ^For emissions of other HAPs from this EIQ, see summary of calculated emissions from fixed roof storage tanks. SL 025956 D-12 PPG 05/2Q/92 trn1 SUMMARY OF THE CALCULATION INPUTS FOR FIXED-ROOF STORAGE TANKS ASSOCIATED WITH THE ETHYLENE DICHLORIDE PROCESS UNIT (EDC) 025957 U1 u* <iEtQ NO. Tank ID Tank Description 312 60-0340 EDC Bottoms Storage Tank No. 4 312 60-0340 EDC Bottoms Starage Tank No. 4 312 60-0340 EDC Bottoms Storage Tank No. 4 312 600340 EDC Bottoms Storage Tank No. 4 312 600340 EDC Bottoms Storage Tank No. 4 312 600342 EDC Bottoms Storage Tank No. 2 312 600342 EDC Bottoms Storage Tank No. 2 312 600342 EDC Bottoms Storage Tank No. 2 312 600342 EDC Bottoms Storage Tank No. 2 312 600342 EDC Bottoms Storage Tank No. 2 313 600330 EDC North Dock Storage No. 1 313 600330 EDC North Dock Storage No. 1 313 600347 EDC North Dock Storage No 2 313 600347 EDC North Dock Storage No. 2 314 60-1213 EDC South Dock Storage No. 1 314 60-1213 EDC South Dock Storage No. 1 314 60-1213 EDC South Dock Storage No. 1 314 60-1213 EDC South Dock Storage No. 1 314 60-1213 EDC South Dock Storage No. 1 314 60-1213 EDC South Dock Storage No. 1 314 60-1213 EDC South Dock Storage No. 1 314 60-1213 EDC South Dock Storage No. 1 314 60-1213 EDC South Dock Storage No. 1 314 60-1213 EDC South Dock Storage No. 1 314 60-1213 EDC South Dock Storage No. 1 314 60-1213 EDC South Dock Storage No. 1 314 60-1213 EDC South Dock Storage No. 1 314 60-1213 EDC South Dock Storage No. 1 314 60-1213 EDC South Dock Storage No. 1 314 60-1213 EDC South Dock Storage No. 1 314 60-1213 EDC South Dock Storage No. 1 HAP Mote Percent Tank Color D Inside Diameter (ft) EDC HCBO HEXA STM TCE EDC HCBD HEXA SYM TCE EDC TCE EDC TCE BROMO* CCL4 CIS* Chloroform DCE EC EDC HCB HEXA PENTA* PER SYM TCE TRI UNKNOWN UNSYM* VCM 76.55 Green 0.76 Green 2.71 Green 4.55 Green 15.42 Green 76.55 Blue 0.78 Blue 2.71 Blue 4.55 Blue 15.42 Blue 75.88 Aqua Green 24.12 Aqua Green 75.68 Aqua Green 24.12 Aqua Green 0.83 White 4.44 White 1.46 White 1.68 White 5.22 White 1.09 White 43.47 White 0.25 White 0.56 White 0.04 White 1.65 White 0.81 White 17.09 White 0.57 White 19.60 White 0.86 White 0.29 White 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 50.00 50.00 50.00 50.00 100.00 too.oo 100.00 100.00 100.00 100.00 100.00 100.00 100.00 too.oo 100.00 100.00 100.00 100.00 100.00 100.00 too.oo V Capacity (9"l-> H Vapor Space Height (ft) 25400 25400 25400 25400 25400 25400 25400 25400 25400 25400 470000 470000 470000 470000 2520000 2520000 2520000 2520000 2520000 2520000 2520000 2520000 2520000 2520000 2520000 2520000 2520000 2520000 2520000 2520000 2520000 15.00 15.00 15.00 15.00 15.00 15.00 15.00 15.00 15.00 15.00 15.00 15.00 15.00 15.00 22.00 22.00 22.00 22.00 22.00 22.00 22.00 22.00 22.00 22.00 22.00 22.00 22.00 22.00 22.00 22.00 22.00 Ts Stored N Mv P Fp C Liquid Number of Molecular Partial Paint Small KN Temp. Turnovers Weight Pressure Factor Diameter Tunover (oF) per Year (b/b mole) (peia) Factor Factor -V* 80.00 80.00 80.00 80.00 80.00 80.00 80.00 80.00 80.00 80.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 14.13 14.13 14.13 14.13 14.13 14.13 14.13 14.13 14.13 14.13 8.64 8.64 6.64 8.64 0.97 0.97 0.97 0.97 0.97 0.97 0.97 0.97 0.97 0.97 0.97 0.97 0.97 0.97 0.97 0.97 0.97 98.970 260.760 236.760 167.660 133.410 98.970 260.760 236.760 167.860 133.410 98.970 133.410 96.970 133.410 143.430 153.820 96.940 119.370 98.970 64.520 96.970 284.800 236.760 202.290 165.850 167.850 133.410 131.380 250.000 167.664 62.490 1.294 0.000 0.000 0.006 0.077 1.294 0.000 0.000 0.006 0.077 1.009 0.092 1.009 0.092 0.001 0.053 0.049 0.053 0.191 0.221 0.578 0.000 0.000 0.000 0.005 0.001 0.065 0.007 0.255 0.002 0.150 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 1.0000 1.30 1.0000 1.30 1.0000 1.30 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1 0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1,00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 = NON HAP, Emission is not inducted as a HAP emission. SL 025958 PPG 05/20/92 SUMMARY OF CALCULATED EMISSIONS FROM FIXED-ROOF STORAGE TANKS ASSOCIATED WITH THE ETHYLENE DICHLORIDE PROCESS UNIT (EDC ) EIO Tank NO. ID Tank Description 312 60-0340 EDC Bottoms Storage Tank No. 4 312 60-0340 EDC Bottoms Storage Tank No. 4 312 60-0340 EDC Bottoms Storage Tank No. 4 312 600340 EDC Bottoms Storage Tank No. 4 312 600340 EDC Bottoms Storage Tank No. 4 312 600342 EDC Bottoms Storage Tank No. 2 312 600342 EDC Bottoms Storage Tank No. 2 312 600342 EDC Bottoms Storage Tank No. 2 312 600342 EDC Bottoms Storage Tank No. 2 312 600342 EDC Bottoms Storage Tank No. 2 313 600330 EDC North Dock Storage No. 1 313 600330 EDC North Dock Storage No. 1 313 600347 EDC North Dock Storage No. 2 313 600347 EDC North Dock Storage No. 2 314 601213 EDC South Dock Storage No. 1 314 60-1213 EDC South Dock Storage No. 1 314 601213 EDC South Dock Storage No. 1 314 601213 EDC South Dock Storage No. 1 314 60-1213 EDC South Dock Storage No. 1 314 601213 EDC South Dock Storage No. 1 314 60-1213 EDC South Dock Storage No. 1 314 601213 EDC South Dock Storage No. 1 314 601213 EDC South Dock Storage No. 1 314 601213 EDC South Dock Storage No. 1 314 601213 EDC South Dock Storage No. 1 314 601213 EDC South Dock Storage No. 1 314 601213 EDC South Dock Storage No. 1 314 601213 EDC South Dock Storage No. 1 314 601213 EDC South Dock Storage No. 1 314 601213 EDC South Dock Storage No. 1 314 601213 EDC South Dock Storage No. 1 HAP EDC HCBD HEXA 8YM TCE EDC WCBO HEXA SYM TCE EDC TCE EDC TCE BROMO* CCL4 CIS* Chtarokxm DCE EC EDC HCB HEXA PENTA* PER SYM TCE TRI UNKNOWN* UNSYM* VCM LB Breathing 1 QM (Mg/yr) 0.20110 0.00029 000168 0.00865 0.03755 0.20110 0.00029 0.00168 0.00865 0.03755 3.27059 0.82562 3.27069 0.82562 0.00000 2.03850 0.00000 1.57464 3.14928 2.27001 6.00181 0.04346 0.02682 0.00000 0.42569 0.12883 2.02316 0.42800 0.00000 0.00000 1.68021 LW Working |_oes (Mg/yr) 0.50079 0.00002 0.00032 0.00419 0 04023 0.50079 0.00002 0.00032 0.00419 0.04023 4.41903 0.54111 4.41903 0.54111 0.00000 0.21866 0.00000 0.16654 0.50532 0.38108 1.52622 0.00067 0.00091 0.00000 0.02116 0.00363 0.23104 0.02380 0.00000 0.00000 0.24977 LT Total Loes (Mg/yr) Confroi Device 1987 Contol Unweighted Efficiency HAP Emissions (%) (Mg/yr) 1987 Weighted HAP Emissions (Mg/yr) 0.70188 0.00031 0.00200 0.01283 0.07777 0.70188 0.00091 0.00200 0.01289 0.07777 7.68962 1.36672 7.68962 1.36672 0.00000 2.25715 0.00000 1.74318 3.65460 2.65109 8.32803 0.04403 0.02713 0.00000 0.44664 0.13246 2.25420 0.45180 0.00000 0.00000 1.92996 Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber RVR RVR RVR RVR INC INC INC INC INC INC INC INC INC INC INC INC INC INC INC INC INC 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 99.00 99.00 99.00 99.00 89.00 89.00 69.00 69.00 89.00 89.00 69.00 89.00 69.00 89.00 89.00 89.00 89.00 89.00 69.00 69.00 89.00 0.66679 0.00030 0.00190 0.01219 0.07389 0.66679 0.00030 0.00190 0.01219 0.07389 0.07690 0.01367 0.07690 0.01367 0.00000 0.24829 0.00000 0.19175 0.40201 0.29162 0.91608 0.00484 0.00298 0.00000 0.04915 0.01457 0.24796 0.04970 0.00000 0.00000 0.21230 0.66679 0.00030 0.00190 0.12189 0.07389 0.66679 0.00030 0.00190 0.12189 0.07989 0.07690 0.01367 0.07690 0.01367 0.00000 0.24629 0.00000 0.19175 0.40201 0.29162 0.91608 0.04843 0.00298 0.00000 0.04915 0.14571 0.24796 0.04970 0.00000 0.00000 2.12298 NON HAPS, emission is not included as a HAP emission APPENDIX D-B EDC PROCESS UNIT PROCESS VENT CALCULATIONS S510R01S.01A SL 025959 D-15 Final 05/27/92 Source: HON subunit(s) Ethvlene Dichloride Process Unit fEDC) HAPs emitted: Ethyl Chloride (EC). Ethvlene Dichloride (EDO. and Hydgagea Chlorite (ffcp CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: Ethvl Chloride (EC)______________ Year: 1987___________________________ Date: April 1992 Calculator: S.R. Process Vent Identification: 300 (non-routine) Description: __No. 1 LP-EDC Startup Scrubber___________________ Propesg C2ndifct0.il?/Sfimp_lipg Date of flow measurement ----- Method of flow measurement Process Design Rate Date of concentration measurement 1985 Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) Svrinae Sample. GC/TCD Describe any problems encountered during testing None Identified Production rate during flow determination (lbs/hr) 75.846 Production rate during sampling (lbs/hr) 75.846 Average production rate during base year (lbs/hr) 109.995 Stream Characteristics Average vent stream flow rate (ft3/min) 84.6 * Q HAP concentration (ppmv) 20.000 = c Annual hours of operation (hrs) 2=h Vent stream discharge temperature (F) 80 = T HAP molecular weight (lb/lb-mole) 64 = MW Pressure at point of discharge (psia) 14.7 = P HAP high-risk weighting factor --------1----------------- - Fhr Control Control device Scrubber HAP control efficiency (%) ______ = eff Calculations* Uncontrolled Emissions (Eu) = (2.54E-09) o c h MW P T + 460 Uncontrolled Emissions (E0) = m1^4=.0H,(8^.61i20^p0D) (6-4) (J.4.?) (80) + 460 0.0149 Mg/yr HAP Emissions (E^p) E0 (1 - eff/100) SL 025960 D-16 Source: HON subunit(s) Ethvlene Dichloride Process Unit (EDO CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (E^) - 0.0149 (1 - 5/100) 0.014 Mg/yr Weighted HAP Emissions Weighted HAP Emissions ehap (0.014) fhr (1) 0.014 Mg/yr This emission rate is for EC, total emissions can be found in Attachment I. Total HAP Emissions* = 0.07 Mg/yr Total Weighted HAP Emissions * 0.07 Mg/yr If the conditions during testing are not representative of bas year operation, make the appropriate extrapolation below and xplain: Stack 300 operates in three modes, non-routine, startup and shutdown. Emission data calculated here are for the non routine mode. Non-routine emissions occur sporadically throughout the year. In 1987, there were two hours of such emissions. It is difficult to predict how many hours of non routine emissions will occur, and therefore, no extrapolation can be justified. The actual hours used here are those of 1987, the composition data is from 1985. If the flow or concentration were not measured using an EPA reference method, EPA conditional method or validated using Method 301, provide justification and supporting calculations: A typical non-routine vent was analyzed in 1985. Sample was taken by a syringe from the stack and analyzed by GC using a TC detector. The composition of the vent was as follows: SL 025961 D-17 Sourc : HON subunit(s) Ethvlene Dichloride Process Unit rEDC) Component PPffiV CH EC (ethyl chloride) EDC (1,2-dichloroethane) 50.000 20.000 50.000 60.000 350.000 400.000 20,000 50,000 Vent flow at maximum operating rate of 570 tpd is: 6000 scfh 2 psig, 40F The flow rate is therefore: (6000scff# / HR \ \60MIN) f40+460'j (14.7\ \ 520 Jll6.7j Expression provided in "Procedures for Establishing Base Year and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. See Attachment I for calculation results for other HAPs emitted. SL 025962 D-18 CP V* g6S^t ATTACHMENT I SUBUNIT: VENT ID: SCENARIO: DESCRIPTION: EDC 300 NON-ROUTINE NO. 1 LP--EDC STARTUP SCRUBBER YEAR: 1967 Q Average vent stream flow rate (ft3Anin) C HAP Concentration (ppmv) h Annual hours of operation (hrs) T Vent stream discharge temperature (F) MW HAP molecular weight (Ih/lb-mole) P Pressure at point of discharge (psia) FHR HAP high risk weighting factor eft HAP control efficiency (%) EU Uncontrolled emissions (Mg/yr) EU - (2.54E-09xQ X C Khx MWx P) / (T + 460) EHAP Controlled emissions (Mg/yr) EHAP - EU x (1 -(MV100)) Hai* EW Weighted HAP emissions (MgiYr) ; EW - EHAP x FHR VO COMPONENT Q C h MW P T eff FHR EU EHAP EW EC 04.6 20,000 2 64 14.7 00 5.00 1 0.015 0.014 0.014 EDC 04.6 50,000 2 99 14.7 00 5.00 1 0.050 0.055 0.055 HCL 04.6 350,000 2 36 14.7 00 99.00 1 0.147 0.001 0.001 FILE: Nl TOTAL 0.220 0.071 0.071 Source: HON subunit(s) Ethvlene Dichloride Process Unit fEDC) _ HAPs emitted: Ethyl Chloride (EC). Ethvlene Dichloride fEDC). and Hydrogen Chloride_(HCl)__________ ____ _ CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: Ethyl Chloride CEO______________ Year: 1987 Calculator: Date: April,. 1222. S.R. Process Vent Identification: 300 (startup) Description: No. 1 LP-EDC Startup Scrubber----------------------------- Process Conditions/Sampling Date of flow measurement Method of flow measurement Calculated Date of concentration measurement Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) Calculated Describe any problems encountered during testing N/A Production rate during flow determination (lbs/hr) Production rate during sampling (lbs/hr) Average production rate during base year (lbs/hr) 15.ZA6 75.846 109^99,5 Stream -Charagtariatiga Average vent stream flow rate (ft^/min) HAP concentration (ppmv) Annual hours of operation (hrs) vent stream discharge temperature (F) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risk weighting factor 84.6 2.913 ______2 80 64_ 14.7 1 gQIltEPl Control device Scrubber________________________ HAP control efficiency (%) 5 = eff calcpiatlens Uncontrolled Emissions (Ey) = (2.54E-09) Q C h MW p T + 460 Uncontrolled Emissions (Ey) = f2.54E-091(84.6^(2.913)(2)(64)(14.7) (80) + 460 0.002 Mg/yr HAP Emissions (E^p) Ey (1 - eff/100) 0^ sv D-20 Source: HON subunit(s) Ethvlene Dichloride Process Unit fEDC) CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (Ej^p) * 0.002 (1 - 5/100) 0.002 Mg/yr Weighted HAP Emissions Weighted HAP Emissions ehap (0.002) fhr (1) 0.002 Mg/yr This emission rate is for EC, total emissions can be found in Attachment I. Total HAP Emissions* = 0.084 Mg/yr Total Weighted HAP Emissions = 0.084 Mg/yr If the conditions during testing are not representative of base year operation, mate the appropriate extrapolation belov and explain: This is the startup scenario of Stack 300. Quantity of gas going through the scrubber is specific to the process. A typical startup sequence is as follows: Step One: Ethylene purge for 20 minutes 500 scfm. (500sdntf (60MIN\ nSTj ( ZBLB l379lSf 2216 LB ~HR HR SL 025965 D-21 Source: HON subunit(s) ethylene Dichloride Process Unit (F.DC) 79 moles ethylene leave at 40F, 11 psig vapor pressure of EDC at 40F is 0.57 psia. Hole fraction of EDC in the vapor phase is <2-* Z PSifr * 0.022 (11 + 14.7) psia 1 - .022 0.978 Total Flow to Scrubber is then 79 MOLES C2H4 0.978 81 MOLE MOLES EDC - 81 -79 - 2 MOLE HR 198 44 EDC 66 LB 20 MIN Step TWQs 45 minute reaction temperature rise ethylene feed is raised to 665 scfm and CL2 is added to 500 scfro. Emissions will be due to excess ethylene (667 - 500 167 scfm), stripped EDC and inerts. CL2 is 99% pure, therefore, inerts are neglected. Excess ethylene lost is: SL 025966 D-22 Source: HON subunit(s) .Ethylene Dichloride Process Unit fEDC) 26.4 Moles Ethylene leave at 40F, 11 psig. Vapor pressure of EDC at 40F is 0.57 psia. Mole fraction of EDO in the vapor phase is: ^EDC ~ 0.57 psia = 0.022 (11 + 14.7) psia YC2H4 - 1 - .022 = 0.978 Total Flow to the Scrubber is: 26 MOLES q//4 = 26.6 0.976 HR TOTAL 26.6 - 26 0.6 EDC HR 0.6 x -- ^ = 59 -- LB MOLE HR 44 LB 25 MIN EDC Step Three: 10 minutes EDC vents diversion while at maximum rates: Component LSU1SLJUH Ethyl Chloride (EC) 3.0 1,2-Dichloroethane (EDC) 9.1 HCL 4.5 Startup HAP Emissions: component Ethyl Chloride (EC) EBZ75-jm 3.0 1,2-Dichloroethane (EDC) 119 HCL 4.5 lb/hr 2.4 95.2 3.6 These rates were specified for 1985 and are unchanged therefore, no extrapolation is needed. For determination of HAP emission in the base year (1987) these rates are used along with the startup hours in 1987. (Th se are uncontrolled emissions.) SL 025967 D-23 Source: HON subunit(s) Ethvlene Dichloride Process Unit (EDO Concentration of pollutants in the vent can be calculated as follows: A = K XWim SOMEQNENT) = MOLE POLL Q (FT3/MIN VENT) X 60 MIN/HR X MW FTJ VENT C = AX 0.7302 (FT3 ATM/LB MOLE *R) X (T + 460) x 106 = PPM 1 ATM No extrapolation is needed since startup emissions do not change with production rate. Xf the flow or concentration were not measured using an EPA reference method/ EPA conditional method or validated using M thod 301/ provide justification and supporting calculations: Mass flow rates of HAPs were calculated, see above. The average flow rate (Q) is assumed to the same as that for the non-routine mode. Expression provided in "Procedures for Establishing Base Year and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. *See Attachment I for calculation results for other HAPs emitted. SL 025968 D-24 01 r4 o O' vOD' v> SUBUNIT: VENT ID: SCENARIO: DESCRIPTION: ATTACHMENT I EDC 300 STARTUP NO. 1 LP--EDC STARTUP SCRUBBER Q C h T MW P FHR eff EU EHAP EW Average vent stream flow rate (ft3Anin) HAP Concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (Ib/lb-mole) Pressure at point of discharge (psia) HAP high risk weighting factor HAP control efficiency (%) Uncontrolled emissions (Mg/yr) ; Controlled emissions (Mg/yr) Weighted HAP emissions (Mg/yr) ; YEAR: tST EU - (2.54E-09xQxCxhxMW x P) / (T + 46) EHAP - EU x (i - (ff/loo)) EW - EHAP x FHR COMPONENT EC EDC HCL Q 84.6 64.6 84.6 C 2,913 74,700 7,768 h 2 2 2 MW 64 99 36 P 14.7 14.7 14.7 T 80 80 60 eff 5.00 5.00 99.00 FHR 1 1 1 EU 0.002 0.087 0.003 EHAP 0.002 0.082 0.000 EW 0.002 0.082 0.000 D-25 file: re TOTAL 0.092 0.084 0.084 Sourc : HON subunit(s) Ethvlene Dichloride Process Unit (EDO CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: Ethvlene Dichloride (EDO_______ Year: 1987______________________________ Date: --ApE.il .199,2 Calculator: S.R. Process Vent Identification: 300 (shutdown) Description: No. 1 LP-EDC Startup Scrubber____________________ process Conditions/Saroolinq Date of flow measurement Method of flow measurement Calculated___________ Date of concentration measurement Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) Calculated Describe any problems encountered during testing N/A Production rate during flow determination (lbs/hr) Production rate during sampling (lbs/hr) Average production rate during base year (lbs/hr) 75.846 75.846 109.995 stream Characteristics Average vent stream flow rate (ft3/min) HAP concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risk weighting factor ______84.6 155.362 ________0.2? 80 _ 99 _ ______ 14.7 _ 1 =Q =c =h =T = MW =P COBfrCffil Control device Scrubbed________________________ HAP control efficiency (%) ________5 = eff Calculations* Uncontrolled Emissions Uncontrolled Emissions (Ey) = (2.54E-09) o c h MW P T + 460 (Ev) (2.54E-09) (84.61 (155.3621 (0.21) (99^ (14.7) (80) + 460 0.024 Mg/yr HAP Emissions (E^p) = E0 (1 - eff/100) SL 025970 Source: HON subunit(s) EthvleneDichloride Process Unit fEDO CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (E^) = 0.024 (1 - 5/100) 0.023 Mg/yr Weighted HAP Emissions E^ Weighted HAP Emissions * (0.018) F^ (1) 0.023 Mg/yr If the conditions during testing ere not representative of base year operation, make the appropriate extrapolation below and explain: This is the shutdown scenario of Stack 300. Rates are cut and vents are sent to the scrubber. An ethylene purge remains for 10 minutes 500 scfm. = 79 MQE HR 79 moles ethylene leave at 40F, 11 psig. Vapor pressure of EDC at 40F is 0.57 psia. Mole fraction of EDC in the vapor phase is: -? psia (11 + 14.7) psia 0.022 Yc2H4 = 1 - .022 = 0.978 SL 025971 Sourc : HON subunit(s) _Ethglene. Dichloride Process Unit..(EDC) Total Flow to Scrubber is then: 79 MOLES CiH4 0.978 81 MOLE HR MOLES EDO * 81 -79 * 2 x- 99 LB LB MOLE 2 M0LE HR 198 "I EDC HR Concentrations are calculated same as in 300 startup. If the flow or concentration were not measured using an EPA reference method, EPA conditional method or validated using Meth d 301, provide justification and supporting calculations: Mass flow of HAPs was calculated, see above. The average flow rate (Q) is same as that for the non-routine mode. Expression provided in "Procedures for Establishing Base Year and Post-Reduction HAP Emissions" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. SL 025972 D-28 Source: HON subunit(s) Ethylene Dichloride Process Unit (EDC) HAPs emitted: Ethvl Chloride (EC1. Ethvlene Dichloride fEDC), and HY-dFpggn Chloride (HC1)________ ______________________________ CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: Ethvl Chloride _(EC)_ Year: 1987 Date: April 1992 Calculator: S.R. Process Vent Identification: 301 (non-routine) DescriDtion: No. 2 LP-EDC Startup Scrubber______________ Process Conditions/Sampling Date of flow measurement Method of flow measurement -Process Design Rats_____ Date of concentration measurement 1985 Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) Svrinoe Sample. GC/TCD Describe any problems encountered during testing None Identified Production rate during flow determination (lbs/hr) 75.846 Production rate during sampling (lbs/hr) 75.846 Average production rate during base year (lbs/hr) 109.995 Stream Characteristics Average vent stream flow rate (ft3/min) HAP concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risk weighting factor 98.75 ls.ooo 24 80 64 14.7 l control Control device Scrubber_________________________________________ HAP control efficiency (%) ______ = eff Calculations* Uncontrolled Emissions Uncontrolled Emissions (E0) = f2.54E-09i o c h mw P T + 460 (Ejj) = (2.54E-09) (98.75) (15.000) (24) (64) f!4.7) (80) + 460 0.157 Mg/yr HAP Emissions (E^p) = (1 - eff/100) SL 025973 D-29 Source: HON subunit(s) Ethvlene Dichloride process Unit fEDC) CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (E^p) = 0.157 (1 - 5/100) 0.15 Mg/yr Weighted HAP Emissions Weighted HAP Emissions ehap (0.15) fhr (l) 0.15 Mg/yr Total HAP Emissions* = 0.614 Mg/yr Total Weighted HAP Emissions * 0.614 Mg/yr If the conditions during testing are not representative of has year operation, make the appropriate extrapolation below and explain: Stack 301 operates in three modes, non-routine, startup and shutdown. Emission data calculated here are for the non routine mode. Non-routine emissions occur sporadically throughout the year. In 1987, there were 24 hours of such emissions. It is difficult to predict how many hours of non routine emissions will occur, and therefore, no extrapolation can be justified. The actual hours of non-routine emission used here are those of 1987, the composition data is from 1985. If the flow or concentration were not measured using an EPA reference method, EPA conditional method or validated using Method 301, provide justification and supporting calculations: A typical non-routine vent was analyzed in 1985. Sample was taken by a syringe from the stack and analyzed by GC using a TC detector. The composition of the vent was as follows: Si* 025974 D-30 Source: HON subunit(s) Ethvlene Dichlorid Process Unit fEDcn Component ppmv C2H4 ch4 c2h6 EC (ethyl chloride) EDO (1,2-Dichloroethane) HCL 150.000 20,000 240.000 120.000 190,000 15,000 15,000 3.000 4.000 Vent flow at maximum operating rate of 570 tpd is: 7000 scfh 2 psig, 40F The flow rate is, therefore: (7000scffy x HR \ 60M/N) (40 +460) (14.7 psia\ { 520 J {16.7 psia) 98.75 FT3 MIN Expression provided in "Procedures for Establishing Base Year and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. See Attachment I for calculation results for other HAPs emitted. 025975 ATTACHMENT I SL 025976 SUBUNIT: VENT ID: SCENARIO: DESCRIPTION: EDC 301 NON--ROUTINE NO, 2 LP-EDC STARTUP SCRUBBER YEAR: 1NT Q Average vent stream flow rale (ftSAnin) C HAP Concentration (ppmv) h Annual hours of operation (hrs) T Vent stream discharge temperature (F) MW HAP molecular weight (Ib/lb-moie) P Pressure at point of discharge (psta) FHR HAP high risk weighting factor elf HAP control efficiency (%) EU Uncontrolled emissions (Mg/yr) ; BJ - (2.ME -OSxQxCxhx MW x P) / (T + 4eo) EHAP Controlled emissions (Mg/yr) EHAP - EU x (t - (att/100)) EW Weighted HAP emissions (Mgfyr) ; EW - EHAP x FHR 0u1> to COMPONENT Q C h MW P T eff FHR EU EHAP EW EC 98.8 15,000 24 64 14.7 80 5.00 1 0.157 0.149 0.149 EDC 98.8 30,000 24 99 14.7 80 5.00 1 0.487 0.462 0.462 HCL 96.8 40,000 24 36 14.7 80 99.00 1 0.236 0.002 0.002 FILE: N4 TOTAL 0.660 0.614 0.614 Sourc : HON subunit(s) Ethvlene Dichloride Process Unit fEDC) HAPs emitted: Ethvl Chloride (EC), Ethvlene Dichloride (EDC). and Hydrogen Chloride (HC1) CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: Ethvl Chloride (EC)_______________ Year: 1987_______ __________________ Date: April 1992 Calculator: S.R. Process Vent Identification: 301 (startup) Description: No. 2 LP-EDC startup Scrubber____________________ Process Conditions/Samplinq Date of flow measurement Method of flow measurement Calculated___________ Date of concentration measurement Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) Calculated Describe any problems encountered during testing N/A Production rate during flow determination (lbs/hr) Production rate during sampling (lbs/hr) Average production rate during base year (lbs/hr) -13 75.846 109.995 Stream Characteristics Average vent stream flow rate (ft3/min) HAP concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risk weighting factor ______ 98.75 2.495 13 ______ 80 64 ______ 14.7 l Control Control device Scrubber____________________________ HAP control efficiency (%) 5 = eff Calculations* Uncontrolled Emissions Uncontrolled Emissions (Ey) * (2.54E-09) o c h mw p T + 460 (Eg) = (2.54E-09) (98.75) (2,495) (13) (64) (14.7) (80) + 460 0.014 Mg/yr HAP Emissions (E^p) = Ew (1 - eff/100) SL 025977 D-33 Source: HON subunit(s) _Ethvlene Dichloride Process Unit fEDCM CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (E^) = 0.014 (1 - 5/100) 0.013 Mg/yr Weighted HAP Emissions = ehap Weighted HAP Emissions = (0.013) fhr (1) 0.013 Mg/yr Total HAP Emissions* * 0.548 Mg/yr Total Weighted HAP Emissions = 0.548 Mg/yr X? the conditions during testing are not representative of base year operation, make the appropriate extrapolation below and xplain: This is the startup scenario of stack 301. Mass flow of gas going through the scrubber is same as that for stack 300 (startup). The calculated total uncontrolled HAP emissions are: Compgpent EC EDC HCL LB/HR 2.4 95.2 3.6 .)These rates do not change with production rate. (See Page D- 20 SL 025978 D-34 Source: HON subunit(s) Ethvlene Dichloride Process Unit fEDcn If the flow or concentration were not measured using an CPA reference method/ EPA conditional method or validated using Method 301/ provide justification and supporting calculations: Mass flow rates of HAPs and concentrations were calculated same as in 300 startup. The average vent flow rate is same as that for the non-routine mode.* * Expression provided in "Procedures for Establishing Base Year and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. *See Attachment I for calculation results for other HAPs emitted. SL 025979 D-35 SL 025980 ATTACHMENT I SUBUNIT: VENT 10: SCENARIO: DESCRIPTION: EDC 801 8TARTUP NO. 2 LP--EDC 8TARTUP SCRUBBER 1 YEAR: tser Q Average vent stream flow rate (ftSAnin) C HAP Concentration (ppmv) h Annual hours of operation (hrs) T Vent stream discharge temperature (F) MW HAP molecular weight (Ib/lb-mole) P Pressure at point of discharge (peia) FHR HAP high risk weighting factor eff HAP control efficiency (%) EU Uncontrolled emissions (Mg/yr) EU - (2.54E-09xQ xc xhxMW xP) / fT + 60) EHAP Controlled emissions (Mg/yr) EHAP - EU x (1 - (efl/ioo)) EW Weighted HAP emissions (Mg/yr) ; EW - EHAP k FHR OuI> m COMPONENT Q C ft MW P T eff FHR EU EHAP EW EC 96.75 2,495 13 64 14.7 60 5.00 1 0.014 0.013 0.013 EDC 98.75 63,995 13 99 14.7 60 5.00 1 0562 0.534 0534 HCL 98.75 6,655 13 36 14.7 80 99.00 1 0.021 0.000 0.000 FILE: NS total 0.598 0.548 0546 Source: HON subunit(s) Ethvlene Dichloride Process Unit fEDC^ CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: Ethvl Dichloride fEDC) Year: 1987_________________ Date: April 1992 Calculator: S.R. Process Vent Identification: 301 (shutdown) Description: No. 2 LP-EDC Startup Scrubber Process Conditions/Samplinq Date of flow measurement Method of flow measurement Calculated Date of concentration measurement Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) Calculated Describe any problems encountered during testing N/A Production rate during flow determination (lbs/hr) Production rate during sampling (lbs/hr) Average production rate during base year (lbs/hr) Stream Characteristics Average vent stream flow rate (ft3/min) HAP concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risk weighting factor 91a 7 m, IPO XI 99 Ukxl 1 - 75.846 75.846 159.395 -Q MW Cpnfcrol Control device Scrubber HAP control efficiency (%) 1 eff Calculations* Uncontrolled Emissions (Eu) = (2.54E-09) o c h MW P T + 460 Uncontrolled Emissions (Ey) * (Zr 54E-09( 9J.J.5 n.ma 001 (U U9il (L4-i_2_) (80) + 460 1.17 Mg/yr HAP Emissions (E^p) = Eu (1 - eff/100) SL 025981 D-37 Sourc : HON subunit(s) Ethvlene Dichloride Process Unit fEDC) CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (E^) 1.17 (1 - 5/100) 1.11 Mg/yr Weighted HAP Emissions Weighted HAP Emissions ehap (1.11) fhr (1) 1.11 Mg/yr If the conditions during testing are not representative of bas year operation/ make the appropriate extrapolation below and xplain: This is the shutdown scenario of Stack 301. vent flow calculations are identical to Stack 300. Total mass flow of HAPs to the scrubber is 198 LB/HR EDC. Concentrations are calculated same as in 300 startup. The hourly emissions from shutdown operations do not change with production rate. If the flow or concentration were not measured using an EPA reference method/ EPA conditional method or validated using Method 301/ provide justification and supporting calculations: Mass flow of HAP was calculated, see above. The average flow rate (Q) is same as that for the non-routine mode. Expression provided in "Procedures for Establishing Base Year and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. SL 025982 D-38 ENSR APPENDIX E PERCHLOROETHYLENE/TRICHLOROETHYLENE PROCESS UNIT (PER/TRI) 5510R016.01 SI* 025983 Final 05/27/92 ENSR APPENDIX E PERCHLOROETHYLENE/TRICHLOROETHYLENE PROCESS UNIT (PER/TRI) E.l Process Description Perchloroethylene (Per) and Trichloroethylene (Tri) are manufactured simultaneously in the Per/Tri Unit from a feedstock of oxygen, 1,1,2-trichloroethane (TCE), 1,1,2,2-tetrachloroethane (Sym), 1,1,1,2-tetrachloroethane (Unsym), and heavier chlorinated organics. 1,1,2-Trichloroethane (C2H3Cl3) Trichloroethylene (CjHClg) + Heavies + Hydrogen Chloride + Oxygen -----------Catalyst (HCI) (02) + Perchloroethylene + Water + Hydrogen Chloride <QA> (HjO) (HCI) Per and Tri are formed by a complex series of successive chlorination and cracking reactions in which HCI is cracked off the chlorinated molecules. There are five similar independently operated reactors. Figure E-1 outlines the major steps in the production of these solvents. Figure E-2 is a flow diagram showing the major equipment used in the process and the location of vents. Feed stocks of oxygen and vaporized organics enter the reactors and rise through the fluid bed of suspended catalyst particles. A mixture of Per, Tri, water and other gaseous organics flow out the reactor to graphite condensers. This mixture is condensed except for inerts which are vented to the incinerators. The resulting organic/water mixture is dried by phase separation and azeotropic distillation. A dry crude product is sent to the distillation section for purification. At the distillation section the crude organic mixture is first split into a crude Per product and a crude Tri product. The crude Per product is purified by first removing heavies in a heavies still. Then two Per stills remove light impurities to produce a Per product which is neutralized and stored. Heavy impurities are sent to the Bottoms Unit in the Waste Treatment Unit and lights are recycled back into the system. E-1CC10R016.01A Final 05/27/92 SL 025984 Figure E-2: Perchloroethylene - Trichloroethylene (PER/TRI) See Volume II - Confidential ENR 5510R01&01A SL 025986 E-3 Final OS/27/92 The crude Tri product is separated from light impurities. The lights are transferred to either transdichloroethyiene recovery or recycled to the PER/TRI reactors. A pure Tri product is neutralized and stored. Both Per and Tri are stabilized with special chemicals and then sent to product storage to await shipment via barges, ships, tank trucks, drums, and railcars. E.2 1987 Base-Year Emissions Table E-1 shows the total base-year emissions for the PER/TRI process unit. The total unweighted HAP emissions were 206.784 Mg/yr. Emissions from four process vents (EIQ 303, 339, 340 and 341) and one storage tank (EIQ 360) required using weighting factors. The total base-year weighted HAP emissions for the PER/TRI unit were 366.552 Mg/yr. E.3 Emissions Reduction Strategy Table E-2 shows the control strategy for the PER/TRI unit that will be implemented to help achieve a plantwide reduction in emissions for all SOCMI sources at the facility. The general control strategy is as follows: Emissions from four process vents, EIQ 303 (startup mode only), 339, and 341 will be incinerated, Emissions from one process vent, EIQ 359, will be vented to a cooling tower water condenser, and e Emissions from three storage tanks, EIQ 329, 334, and 360, will be incinerated. With the inclusion of these controls, the total overall control level for the PER/TRI unit is estimated to be 87.65% for unweighted HAPs and 85.62% for weighted HAPs. E.4 Post-Reduction Emissions Table E-3 shows the total unweighted and weighted HAP emissions for the PER/TRI process unit. The total post-reduction unweighted emissions of 25.535 Mg/yr represent a 181.249 Mg/yr decrease (87.65% reduction) in unweighted HAP base-year emissions. The total post-reduction weighted emissions of 52.705 Mg/yr represent a 313.847 Mg/yr decrease (85.62% reduction) in weighted HAP base-year emissions. 5510R016.Q1A SL 025987 E-4 Final 05/27/92 09 CD TABLE E--1 1987 BASE YEAR EMISSIONS PERCHLOROETHYLENE/TRICHLOROETHYLENE PROCESS UNIT (PER/TRI) BASE YEAR UNIT EIQ DESCRIPTION TYPE PER/TRI PER/TRI PER/TRI PER/TRI PER/TRI 303 339 340 341 359 PER/TRI PER/TRI PER/TRI PER/TRI PER/TRI PER/TRI PER/TRI PER/TRI PER/TRI PER/TRI PER/TRI 327 328 329 330 331 334 360 362 363 376 377 Per/Tri Startup Scrubber Per/Tri Still Line Scrubber Per/Tri DH System Vent Scrubber Per/Tri Acid Tank Scrubber Per/Trl Product Dryer Regen. Per Dock Storage Tank Per Process Storage Per 208 Shipping Tank Tri Dock Storage Tri Process Storage Tri Shipping Tank Per/Tri StHI Line Tk. Per/Tri BLM Tank No. 1 PerfTri BLM Tank No. 2 Dowtherm "A" Makup Tank Dowtherm Recycle Water recovery Tk. P P P P P T T T T T T T T T T T CONTROL DEVICE HAP EMISSIONS % UNWEIGHTED WEIGHTED TYPE CONTROL* MG/YR MG/YR Scrubber 5.00 7.157 32.341 Scrubber 5.00 67.524 190.118 Scrubber 5.00 0.095 0.901 Scrubber 5.00 1.964 5.956 Scrubber 5.00 87.140 87.140 Subtotal Process Vents 163.880 316.456 None 0.00 7.179 7.179 Ref. Cond. 73.10 1.051 1.051 None 0.00 0.681 0.681 Ref. Cond. 66.70 4.782 4.782 Ref. Cond. 69.20 3.172 3.172 None 0.00 2.162 2.162 Scrubber 5.00 23.721 30.913 None 0.00 0.152 0.152 None 0.00 0.000 0,000 None 0.00 0.004 0.004 None 0.00 0.000 0.000 Subtotal Tank Vents 42.904 50.096 ______________________________________ 1 * Control fflctanciM for scrubbers rsprsssnt efficiencies for hycfiocarbona, these scrubbers have 99% efficiency for HCI. Total Base Year Emissions I 206.784 366.552 FILE: PTBASE SL 025989 TABLE E-2 EMISSIONS REDUCTIONS STRATEGY AND POST REDUCTION EMISSIONS PERCHLOROETHYLENE/TRICHLOROETHYLENE PROCESS UNIT (PER/TRI) POST REDUCTION UNIT EIQ DESCRIPTION TYPE HAP EM SSIONS ADDITIONAL 1994 UNWEIGHTED WEIGHTED PER/TRI 303 Per/Tri Su Scrubber CONTROL % CONTROL* MG/YR MG/YR P Incinerator 99.99 6.759 30.543 PER/TRI 339 PER/TRI 340 Per/Tr) Still Line Scrubber Per/Tri DH System Scrubber P Incinerator P None 98.00** 5.00 1.422 0.095 4.000 0.901 PER/TRI 341 PER/TRI 359 Per/Tri acid Tank scrubber Per/Tri Product Dryer Regen. P Incinerator P Coding Water Cond. 99.99 99.00 0.000 0.917 0.001 0.917 Subtotal Process Vents 9.193 36.362 m PER/TRI 327 Per Dock Storage Tank T None 0.00 7.179 7.179 PER/TRI 326 Per Process Storage T None 73.10 1.051 1.051 PER/TRI 329 Per 208 Shipping Tank T Incinerator 99.99 0.000 0.000 PER/TRI 330 Tri Dock Storage T None 66.70 4.762 4.782 PER/TRI 331 Tri Process Storage T None 69.20 3.172 3.172 PER/TRI 334 Tri Shipping Tank T Incinerator 99.99 0.000 0.000 PER/TRI 360 Per/Tri StiHUneTk. T Incinerator 99.99 0.002 0.003 PER/TRi 362 Per/Tri BLM Tank No. 1 T None 0.00 0.152 0.152 PER/TRI 363 Per/Tri BLM Tank No. 2 T None 0.00 0.000 0.000 PER/TRI 376 Dowtherm "A* Makup Tank T None 0.00 0.004 0.004 PER/TRI 377 Dowtherm Recycle Water recovery Tk. T None 0.00 0.000 0.000 Subtotal Tan k Vents 16.342 16.343 ' Confroi atticlanelas tar scrubbars rsprtsant ffictsnclM tar hycfrocarboos, Dim scrubbars hav* 99% affictancy tor HCI. Total Post Reducticm Emissions * * Dua to process spacific conditions, some vents from this source will not be Incinerated. Therefor , the confroi efficiency is 98% rather than 99.99% in order to allow room far operations which will not be routed to the Incinerator. 25.535 52.705 FILE: PTPOST co 025990 TABLE E-3 HAP EMISSIONS SUMMARY PERCHLOROETHYLENE / TRICHLOROETHYLENE PROCESS UNIT (PER/TRI) Unweighted HAP Emissions Weighted HAP Emissions Post Percent Post Percent Type Base Year Reduction Reduction Base Year Reduction Reduction 5 (Units) (Mg/yr) (Mg/yr) (%) (Mg/yr) (Mg/yr) (%) P 163.680 9.193 94.39 316.456 36.362 88.51 T 42.904 16.342 61.91 50.096 16.343 67.38 F Total Total Percent Reduction ______isy______ P- Process Vsnts T-Tar* Vsnts F- Fugttfv* Emfsskjns 206.784 25.535 87.65 366.552 52.705 85.62 APPENDIX E-A PERCHLOROETHYLENE/TRICHLOROETHYLENE PROCESS UNIT STORAGE TANK CALCULATIONS SS10R016.01A SL 025991 E-8 Rnai 05/27/02 Source: HON subunit(s) P rchloroethvlene/Trichloroethylene fP/TM CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM FIXED ROOF STORAGE TANKS (SAMPLE) HAP: Perchloroethvlene (Per) Date: Year: _____1987____________ 05/13/92 Calculator: J. Greer Tank Designation: EIO 327 Per Dock Storage Tank No. l (60-0523^ Product: Perchloroethvlene Tank Characteristics Inside diameter, (ft) Height, (ft) Capacity, (gal) * v Eik * 7.48 gal, 4 fp if not known Roof color White Shell color White Vapor space height, (ft)a Ambient Conditions Average atmospheric pressure (psia) (defaults 14.7 psia) Average ambient diurnal temperature (F)b Average annual ambient temperature (F) Bulk Liquid Characteristics Stored liquid temperature (F)C Total throughput per year (gal) Number of turnovers per yeard Molecular weight of HAP (lb/lb mole) Mole percent of HAP Partial pressure of the HAP at liquid conditions (psia) Adjustment Factors Paint factor Small diameter tank factore Turnover factorf Product factor5 ______ 48 32 433.135 ______ 16 ______ 14.7 ______ is ______ 70 _________70 1.643.490 3.79 165.82 ______iog 0.29 ___________i.o ___________l.o ___________i. p ___________i. p D Hx V H PA dT TA TS AN N P Fp C kn Kc SL 025992 E-9 Source: HON subunit(s) Perchloroethvlene/Trichloroethylene HAPs emitt d: Perchloroethvlene (Per) CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM FIXED ROOF STORAGE TANKS (SAMPLE) (CONTINUED) Baseline control Control device None HAP control efficiency (%) calculations11 Breathing Loss (Mg/yr) = ________o% eff Lb = 1.02E-05 {Mv) (flL (PA) - (*> r= 1.025-05 (165.82) 0.29 (48)173(16)0-51 (18)050(1 )(1 )(1) 14.7 - 0.29 Working Loss (Mg/yr)- L* - 1.09E-08 MvPVNKnKc = 1.09E-08(165.82)(0.29)(433,135)(3.79)(1)(1) Total Loss (Mg/yr) tl = Lb + (1.68) + (0.86) If a control device is employed, HAP Emissions (,,.. = Total Loss (l - eff/100) - 2.540 (1 - 0/100) 2.540 Mg/yr SL 025993 E-10 Source: HON subunit(s) Perchloroethvlene/Trichloroethvlene fP/T) HAPs emitted: Perchloroethvlene (P r)_____________ CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM FIXED ROOF STORAGE TANKS (SAMPLE) (CONTINUED) Calculation (Continued) Weighted HAP Emissions1 ehap (2.54) 2.54 Mg/yr aIf vapor space height is unknown for shell, assume H equals one half tank height. If tank has a cone roof, adjust vapor space height by adding 1/3 of height of cone. bIf average ambient diurnal temperature change is unknown, assume 20F. cStored liquid temperature may be approximated from average annual ambient temperature. dN = AH where N number of turnovers per year V AN = total throughput per year (gal) V = tank capacity (gal) eFor D 30ft, C*l; For 6 D < 30 ft, C * 0.0771D-0.0013D2-0.1334. fFor turnovers > 36, KN = (180 + N)/(6 * N) where K,, - turnover factor (dimensionless) N " number of turnovers per year For turnovers 36, KN = l 9Kc *= 1.0 for volatile organic liquids hExpression for computing HAP emissions are from "Procedures for Establishing Base Year and Post-Reduction HAP Emissions." The calculation procedure is consistent with AP-42. 1For emissions of other HAPs from this EIQ, see summary of calculat d emissions from fixed roof storage tanks. SL 025994 E-ll trn* o PPG 05/20/92 t(viUoJDO!i SUMMAHY OF THE CALCULATION INPUTS FOR FIXED-ROOF STORAGE TANKS ASSOCIATED WITH THE PERCHLOROETHYLENE / TRICHLOROETHYLENE PROCESS UNIT (PER/TRI) EIQ Tank NO. ID Tank Description 327 60-0523 PER Dock Storage Tar* No. 1 327 60-0823 PER Dock Starage Tar* No. 2 327 60-1142 PER Dock Storage Tank No. 3 328 600483 DG3PER 232 Batch Tank 328 600484 DG 4 PER 232 Batch T* 328 600498 No. 2 DG PER Stsb Tar* 328 600501 No. 1 DG PER Stab Tar* 328 60-1138 PER 232 Shipping Tank 328 60-1139 No. 1 PER Stab Tank 328 60-1140 No. 2 PER Stab Tank 329 600427 PER 206 Shipping Tank 330 600522 TRI-Dock Storage Tar* No. 1 330 600824 TRFDock Storage Tar* No. 2 330 60-1141 TRt-Oock Storage Tank No. 3 331 600649 No. 1 HP Stab Tank 331 600650 No. 2 HP Stab Tank 331 600652 N . 3 HP Stab Tank 331 60-1137 No. 1 TRI Stab Tar* 331 60-1216 No. 3 TRi Stab Tar* 334 600428 TRI Shipping Tank 341 P/T Acid TPer/ Trl Acid Tar* Scrubber 341 P/T Acid TPer/ Tri Acid Tar* Scrubber 341 P/T Acid TPer/ Trl Acid Tar* Scrtbber 341 P/T Acid TPer/ Tri Acid Tar* Scribber 341 P/T Acid TPer/ Tri Acid Tar* ScrUbber 341 P/T Acid TPer/ Trl Add Tar* ScrUbber 341 P/T Acid TPer/ Tri Acid Tar* Scnbber 341 P/T Acid TPer/ Tri Add Tar* ScrUbber 360 600466 No. 1 Still Line Feed Tar* 360 600468 No. 1 Still Line Feed Tar* 360 600468 No. 1 Still Line Feed Tar* 360 600468 No. 1 Still Line Feed Tar* 360 600468 No. 1 Still Line Feed Tar* 360 600468 N . 1 Still Line Feed Tar* HAP PER PER PER PER PER PER PER PER PER PER PER TRI TRI TRI TRI TRI TRI TRI TRI TRI DCE EDC H20* MECL2 SYM TCE UNSYM* VDC CCL4 CIS* HCBD HEXA PCBD* PENTA* Mde Percent Tank Odor D Inside Diameter (ft.) V Capacity (9L ) H Vapor Space Height (ft.) Ts Stored Liquid Temp. (oF) N Mv Number d Molecular P Fp C Partial Paint Small KN Turnovers Weight Prassure Factor Diameter Tisnever per Year (b/b mde) (psla) Factor Factor 100.00 White 100.00 While 100.00 White 100.00 Green 100.00 Green 100.00 LL Beige 100.00 LL Beige 100.00 Green 100.00 Pink 100.00 Pink 100.00 Aqua Green 100.00 White 100.00 White 100.00 White 100.00 Li Beige 100.00 Lt. Beige 100.00 LL Beige 100.00 LL Blue 100.00 LL Blue 100.00 White 0.00 Black 0.00 Black 99.99 Black 0.00 Black 0.00 Black 0.00 Black 0.00 Black 0.00 Black 1.53 LL Blue 0.81 Lt. Blue 1.80 LL Blue 0.13 Lt. Blue 0.35 Lt. Blue 0.70 LL Blue 48.00 48.00 46.00 12.00 12.00 12.00 12.00 20.00 20.00 20.00 12.00 48.00 48.00 46.00 12.00 12.00 12.00 20.00 20.00 12.00 10.50 10.50 10.50 10.50 10.50 10.50 10.50 10.50 12.00 12.00 12.00 12.00 12.00 12.00 433135 433135 433135 14800 14800 14800 14800 70500 70500 70600 25400 433135 433135 433135 14800 14800 14800 70500 70500 25400 10000 10000 10000 10000 10000 10000 10000 10000 20000 20000 20000 20000 20000 20000 16.00 16.00 16.00 9.00 9.00 9.00 9.00 15.00 15.00 15.00 15.00 16.00 16.00 16.00 9.00 9.00 9.00 15.00 15.00 15.00 4.00 4.00 4.00 4.00 4.00 4.00 4.00 4.00 12.00 12.00 12.00 12.00 12.00 12.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 3.79 2.82 2.82 46.88 46.88 7.87 7.87 9.84 16.77 16.77 74.81 1.52 1.52 1.52 10.02 7.48 7.48 30.05 30.05 90.43 5.83 5.63 5.83 5.83 5.83 5.83 5.63 5.83 315.25 315.25 315.25 315.25 315.25 31525 165.820 165.820 165.620 165.820 165.620 165.820 165.820 165.820 165.820 165.620 165.820 131.400 131.400 131.400 131.400 131.400 131.400 131.400 131.400 131.400 98.970 98.970 18.020 84.930 167.850 133.410 167.850 96.940 153.620 96.950 260.760 236.760 226.200 202.290 0.290 0.290 0.290 0.290 0.290 0.290 0.290 0.290 0.290 0.290 0.290 t.200 1.200 1.200 1.200 1.200 1.200 1.200 1.200 1.200 0.000 0.000 0.950 0.000 0.000 0.000 0.000 0.000 0.055 0.054 0.000 0000 0.001 0.001 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.8886 1.30 0.6866 1.30 0.8886 1.30 0.6046 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6886 1.30 0.8888 1.00 0.6046 1.50 0.5326 1.50 0.5328 1.50 0.5328 1.50 0.5328 1.50 0.5328 1.50 0.5328 1.50 0.5328 1.50 0.5328 1.30 0.6046 1.30 0.6046 1.30 0.6046 1,30 0.6046 1.30 0.6046 1.30 0.6046 1.00 1.00 1.00 0.81 0.61 1.00 1.00 1.00 1.00 1.00 0.57 too 1.00 1.00 1.00 1.00 1.00 1.00 1.00 0.50 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 0.26 0.26 0.26 0.26 0.26 0.26 = NON HAP, Emission is not included as a HAP emission. PPG 05/20/92 SUMMARY OF CALCULATED EMISSIONS FROM FIXED-ROOF STORAGE TANKS r ASSOCIATED WITH THE PER / TRI PROCESS UNIT ( PER / TRI ) 025996 EIQ Tank NO. ID Tank Description 327 60-0523 PER Dock Storage Tank No. 1 327 600823 PER Dock Storage Tank No. 2 327 60-1142 PER Dock Storage Tank No. 3 328 600483 DG 3 PER 232 Batch Tank 328 600484 DG 4 PER 232 Batch Tank 328 600498 No. 2 DG PER Stab Tank 328 600501 No. 1 DG PER Stab Tar* 328 601138 PER 232 Shipping Tank 328 60t 139 No. 1 PER Stab Tank 328 601140 No. 2 PER Stab Tank 329 600427 PER 208 Shipping Tar* 330 600522 TBI-Oock Storage Tank No. 1 330 600824 TRt-Dock Storage Tank No. 2 330 601141 TRi-Docfc Storage Tank No. 3 331 600649 No. 1 HP Stab Tank 331 600650 No. 2 HP Stab Tank 331 600652 No. 3 HP Stab Tank 331 601137 No. 1 TRI Stab Tank 331 601216 No. 3 TRI Stab Tank 334 600428 TRI Shipping Tank 341 P/T Acid TKPer/Tfl Add Tank Scrubber 341 P/T Add TKFer/ Trl Add Tank Scrubber 341 P/T Add TK Per/ Trl Add Tank Scrubber 341 P/T Add TKPer/ Trl Add Tank Scrubber 341 P/T Add TKPer/ Trl Add Tank Scrubber 341 P/T Add TKPer/Tri Acid Tank Scrubber 341 P/T Add TKPer/ Trl Add Tank Scrubber 341 P/T Add TKPer/ Tri Acid Tank Scrubber 360 600468 No. 1 Stitt Line Feed Tank 360 600468 No. 1 StUI Line Feed Tank 360 600468 No. 1 SUN Line Feed Tank 360 600468 No. 1 StUI Line Feed Tank 360 600468 No. 1 Still Line Feed Tank 360 600468 No. 1 SUN Line Feed Tank NON HAPS, emission is not included as a HAP emission HAP PER PER PER PER PER PER PER PER PER PER PER TRI TRI TRI TRI TRI TRI TRI TRI TRI DOE EDO H20* MECL2 SYM TCE UNSYM* VDC CCL4 CIS* HCBD HEXA PCBD* PENTA* LB Breathing Loaa (Mg/yr) 1.67904 1.67904 1.67904 0.08943 0.08943 0.08943 0.08943 0.41272 0.41272 0.41272 0.11804 3.65339 3.65339 3.65339 0.19458 0.19458 0.19458 0.89802 0.89802 0.19423 0.00027 0.00015 0.00000 0.00012 0.00000 0.00000 0.00000 0.00014 0.03078 0.00000 0.00075 0.00031 0.00000 0.00000 LW Working Loaa (Mg/yr) 0.86145 0.64016 0.64016 0.29334 0.29334 0.06102 0.06102 0.36371 0.61967 0.61967 0.56540 1.13371 1.13371 1.13371 0.25488 0.19026 0.19028 3.64066 3.64098 1.96761 0.00002 0.00001 0.00000 0.00001 0.00000 0.00000 0.00000 0.00001 0.15301 0.00000 0.00061 0.00015 0.00000 0.00000 LT Total Loaa (Mg/yr) Control Device 1987 Control Unweighted Efficiency HAP Emissions (%> (Mg/yr) 1987 Weighted HAP Emissions (Mg/yr) 2.54049 2.31920 2.31920 0.38277 0.38277 0.15044 0.15044 0.77642 1.03238 1.03238 0.68144 4.76710 4.78710 4.78710 0.44945 0.38487 0.38487 4.53896 4.53896 2.18164 0.00029 0.00016 0.00000 0.00013 0.00000 0.00000 0.00000 0.00015 0.18379 0.00000 0.00126 0.00046 0.00000 0.00000 None None None RVR RVR RVR RVR RVR RVR RVR None RVR RVR RVR RVR RVR RVR RVR RVR None None None None None None None None None Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber 0.00 0.00 0.00 73.10 73.10 73.10 73.10 73.10 73.10 73.10 0.00 66.70 66.70 66.70 69.20 69.20 69.20 69.20 69.20 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 5.00 5.00 5.00 5.00 5.00 5.00 2.54049 2.31920 2.31920 0.10297 0.10297 0.04047 0.04047 0.20886 0.27771 0.27771 0.66144 1.59411 1.59411 1.59411 0.13843 0.11854 0.11854 1.39801 1.3980t 2.16184 0.00029 0.00016 0.00000 0.00013 0.00000 0.00000 0.00000 0.00015 0.17460 0.00000 0.00119 0.00044 0.00000 0.00000 2.54049 2.31920 2.31920 0.10297 0.10297 0.04047 0.04047 0.20886 0.27771 0.27771 0.68144 1.59411 1.59411 1.59411 0.13643 0.11854 0.11854 1.39801 1.39801 2.16184 0.00029 0.00016 0.00000 0.00013 0.00003 0.00000 0.00000 0.00149 0.17460 0.00000 0.00119 0.00044 0.00000 0.00000 PPG 05/2QI92 SUMMARY OF THE CALCULATION INPUTS FOR FIXED-ROOF STORAGE TANKS o ASSOCIATED WITH THE PERCHLQROETHYLENE / TRICHLOROETHYLENE PROCESS UNIT ( PER / TRI > tn _________________________ .____________________________________ ____________________ i) - ~ ~ ......- --------------- - ------------- -------------- -- ....... ~~ -- VO H Ts J Era Tank Tank Mole Tank D Inside Vapor Stared N Mv P FP C V Space Liquid Number ot Molecular Partial Paint Small KN NO. 10 Description HAP Percent Color Diameter Capacity Height Temp. Tienarers Weight Pressue Fackx Diameter Turnmer (ft) (9*L ) (ft) (oF) par Year (b/b mole) (psia) Factor Factor 360 600466 No. 1 Still Line Feed Tank 360 600468 No. 1 Still Line Feed Tank 360 600466 No. 1 Still Une Feed Tark 360 600468 No. 1 Still Line Feed Ter* 360 600468 No. 1 StHI Une Feed Tark 360 600468 N . 1 Still Line Feed Tank 360 600468 No. 1 Still Line Feed Tar* 360 600472 No. 2 Still Une Feed Tar* 360 600472 No. 2 Still Une Feed Tar* 360 600472 No. 2 Still Une Feed Tark 360 600472 No. 2 Still Une Feed Tar* 360 600472 No. 2 Still Line Feed Tar* 360 600472 N .2 Still Une Feed Tar* 360 600472 No. 2 Still Une Feed Tar* 360 600472 No. 2 Still Line Feed Tar* 360 600472 No. 2 Stilt Une Feed Tar* 360 600472 No. 2 StHI Line Feed Tar* 360 600472 No. 2 Still Une Feed Tar* 360 600472 No. 2 Still Line Feed Tar* 360 600472 No. 2 SHI Une Feed Tar* 360 600490 No. 1 Aux line Feed Tank 360 600490 N . 1 Auk Line Feed Tank 360 600490 No. 1 Aux Une Feed Tank 360 600490 No. 1 Auk Une Feed Tank 360 600490 No, 1 Aux Une Feed Tank 360 600490 No. 1 Aik Una Feed Tank 360 600490 No. 1 Auk Une Feed Tank 360 600491 No. 2 Auk Une Feed Tank 360 600491 No. 2 Aux Line Feed Tank 360 600491 No. 2 Aux Une Feed Tank 360 600491 N . 2 Aux Une Feed Tank 360 600491 No. 2 Aux Line Feed Tank 360 600491 No. 2 Auk Une Feed Tank 360 600491 No. 2 Aux Une Feed Tank PER SYM TCE TRANS* TRI UNSYM* VDC CCL4 CIS* HCBO HEXA PCBD* PENTA* PER SYM TCE TRANS* TRI UNSYM* VDC HCBD HEXA PCBD* PENTA* PER SYM TCE HCBD HEXA PC BO* PENTA* PER SYM TCE 64.22 U. Blue 0.03 U Blue 0.12 Lt Blue 0.32 Lt Blue 29.79 LL Blue 0.05 Li Blue 0.16 Lt Blue 1.53 LL Blue 0.81 Lt Blue 1.80 Li. Blue 0.13 LL Blue 0.35 Lt Blue 0.70 Lt Blue 64.22 Lt Blue 0.03 U. Blue 0.12 Li Blue 0.32 Lt Blue 29.79 Lt Blue 0.05 Lt Blue 0.16 Lt Blue 1.29 Aqua Green 0.71 Aqua Green 0.74 Aqua Green 2.08 Aqua Green 87.18 Aqua Green 5.51 Aqua Green 2.52 Aqua Green 1.29 Aqua Green 0.71 Aqua Green 0.74 Aqua Green 2.08 Aqua Green 87.16 Aqua Green 5.51 Aqua Green 2.52 Aqua Green 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 20000 20000 20000 20000 20000 20000 20000 20000 20000 20000 20000 20000 20000 20000 20000 20000 20000 20000 20000 20000 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 f2.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 315.25 315.25 315.25 315.25 315.25 315.25 315.25 315.25 315.25 315.25 315.25 315.25 315.25 315.25 315.25 315.25 315.25 315.25 315.25 315.25 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 037 037 0.37 165.820 167.860 133.410 96.950 131.400 167.864 96.950 153.820 96.950 260.760 236.760 226.200 202.290 165.820 167.860 133.410 97.000 131.400 167.864 96.950 260.760 236.760 226.200 202.290 165.820 167.860 133.410 260.760 236.760 226.200 202.290 165.820 167.860 133.410 0.440 0.000 0.001 0.033 0.751 0.000 0.028 0.055 0.054 0.000 0.000 0.001 0.001 0.440 0.000 0.001 0.033 0.751 0.000 0.028 0.000 0.000 0.001 0.001 0.253 0.006 0.010 0.000 0.000 0.001 0.001 0.253 0.006 0.010 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 t.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 0.26 0.26 0.26 0.26 0.26 0.26 0.26 0.26 0.26 0.26 0.26 0.26 0.26 0.26 0.26 0.26 0.26 0.26 0.26 0.26 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 too 1.00 1.00 1 00 1.00 = NON HAP, Emission is not included os a HAP emission. PPG 05/2CY92 cfn oNUJt \v0O CO 71 Ul SUMMARY OF CALCULATED EMISSIONS FROM FIXED-ROOF STORAGE TANKS ASSOCIATED WITH THE PER / TRI PROCESS UNIT ( PER / TRI ) EIQ Tank NO. ID Tank Description 360 60-0468 No. 1 Stil Lirw Faad Tank 360 600468 No. 1 StM Lin* FMd Tank 360 600468 No. 1 Stil Un FMd Tank 360 600468 No. 1 StM Lin* Fm6 Tank 360 600468 No. 1 SUN Una FMd Tank 360 600468 No. 1 Sttl Urw FMd Tar* 360 600468 No. 1 SIM Urw FMd Tank 360 600472 No. 2 SB* Urw FMd Tank 360 600472 No. 2 SIM Urw FMd Tar* 360 600472 No. 2 SDH Lina FMd Tank 360 600472 No. 2 SIM Urw FMd Tar* 360 600472 No. 2 SIM Urw FMd Tar* 360 600472 No. 2 SIM Urw F*d Tank 360 600472 No. 2 SIM Urw FMd Tar* 360 600472 No. 2 SIM Urw Feed Tar* 360 600472 No. 2 StM Urw FMd Tar* 360 600472 No. 2 SIM Urw Feed Tar* 360 600472 No. 2 SIM Urw Fad Tar* 360 600472 No. 2 SIM Urw FMd Tar* 360 600472 No. 2 StM Urw Fad Tar* 360 600490 No. 1 Aux Urw Feed Tar* 360 600490 No. 1 Aux Urw FMd Tar* 360 600490 No. t Aux Lina Faad Tar* 360 600490 No. 1 Aux Urw Faad Tank 360 600490 No. 1 Aux Urw Faad Tank 360 600490 No. 1 Aux Urw Faad Tank 360 600490 No. 1 Aux Urw Faad Tar* 360 600491 No. 2 Aux Urw Faad Tar* 360 600491 No. 2 Aux Una Faad Tar* 360 600491 No. 2 Aux Una Faad Tank 360 600491 No. 2 Aux Lina Faad Tar* 360 600491 No. 2 Aux Lina Faad Tank 360 600491 No. 2 Aux Urw Faad Tank 360 600491 No. 2 Aux Urw Faad Tank HAP PER SYM TCE TRANS* TRI UNSYM* VDC CCL4 CIS* HCBO HEXA PC BO* PENTA* PER SYM TCE TRANS* TRI UNSYM* VDC HCBO HEXA PCBO* PENTA* PER SYM TCE HCBO HEXA PCBO* PENTA* PER SYM TCE LB Breathing Loss (Mg/yr) 0.13837 0.00036 0.00177 0.00000 0.16020 0.00000 0.01224 0.03075 0.00000 0.00075 0.00031 0.00000 0.00000 0.13837 0.00038 000177 0.00000 0.16021 0.00000 0.01224 0.00028 0.00047 0.00000 0.00000 0.09415 0.00698 0.00809 0.00028 0.00047 0.00000 0.00000 0.09415 0.00698 0.00809 LW Working Loss (Mg/yr) 1.31138 0.00021 0.00246 0.00000 1.77522 0.00000 0.04909 0.15275 0.00000 0.00061 0.00015 0.00000 0.00000 1.31139 0.00021 0.00248 0.00000 1.77522 0.00000 0.04909 0.00000 0.00000 0.00000 0.00000 0.00249 0.00005 0.00008 0.00000 0.00000 0.00000 0.00000 0.00249 0.00005 0.00008 LT Total Loss (Mg/yr) Control Device 1987 Control Unweighted Efficiency HAP Emissions (%) (Mg/yr) 1987 Weighted HAP Emissions (Mg/yr) 1.44976 0.00057 0.00423 0.00000 1.93542 0.00000 0.06134 0.18350 0.00000 0.00126 0.00046 0.00000 0.00000 1.44976 0.00057 0.00423 0.00000 1.93543 0.00000 0.06134 0.00028 0.00047 0.00000 0.00000 0.09664 0.00704 0.00616 0.00028 0.00047 0.00000 0.00000 0.09664 0.00704 0.00816 Scrubber Scrubber Scrubbar Scrubber Scrubber Scrubbar Scrubber Scrubber Scrubber Scrubbar Scrubbar Scrubber Scrubbar Scrubbar Scrubber Scrubbar Scrubbar Scrubbar Scrubber ScriJsbar Scrubber Scrubbar Scrubber Scrubber Scrubber Scrubber Scrubbar Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scnbber 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 1.37727 0.00054 0.00402 0.00000 1.63865 0.00000 0.05827 0.17432 0.00000 0.00119 0.00044 0.00000 0.00000 1.37727 0.00054 0.00402 0.00000 1.83865 0.00000 0.05827 0.00027 0.00044 0.00000 0.00000 0.09181 0.00669 0.00775 0.00027 0.00044 0.00000 0.00000 0.09181 0.00669 0.00775 1.37727 0.00545 0.00402 0.00000 1.83865 0.00000 0.58268 0.17432 0.00000 0.00119 0.00044 0.00000 0.00000 1.37727 0.00545 0.00402 0.00000 1.83865 0.00000 0.58268 0.00027 0.00044 0.00000 0.00000 0.09181 0.06686 0.00775 0.00027 0.00044 0.00000 0.00000 0.09181 0.06686 0.00775 NON HAPS, mission is not included as a HAP mission PPG 05/20/92 SUMMARY OF THE CALCULATION INPUTS FOR FIXED-ROOF STORAGE TANKS ASSOCIATED WITH THE PERCHLOROETHYLENE / TRICHLOROETHYLENE PROCESS UNIT ( PER / TRI) EIQ Tank NO. ID Tank Description 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 60-0492 600492 600492 600492 600492 600492 600492 600493 600493 600493 600493 600493 600493 600493 600494 600494 600494 600494 600494 600494 600494 600495 600495 600495 600495 600495 600495 600495 600496 600496 600496 600496 600496 600496 No. 4 Aux Line Feed Tank No. 4 Auk Line Feed Tank No. 4 Auk Una Feed Tank No. 4 Aim Line Feed Tank No. 4 Aux Line Feed Tank No. 4 Auk Una Feed Tank No. 4 Aux Line Feed Tank No. 3 Aim Una Feed Tank No. 3 Aux Una Feed Tank No. 3 Aim Una Feed Tank No. 3 Aim Line Feed Tank No. 3 Aim Una Feed Tank No. 3 Aux Line Feed Tank No. 3 Aim Una Feed Tank No. 7 Aim Line Feed Tank No. 7 Aim Line Feed Tank No, 7 Aim Line Feed Tank No. 7 Aux Line Feed Tank No. 7 Aim Line Feed Tank No. 7 Aim Line Feed Tank No, 7 Aim Una Feed Tank No. 5 Aim Line Feed Tank No. 5 Aim Une Feed Tank No. 5 Aim Line Feed Tank No. 5 Auk Une Feed Tank No. 5 Aux Line Feed Tank No. 5 Auk Una Feed Tank No. 5 Aux Line Feed Tank No. 6 Auk Une Feed Tank No. 6 Auk Line Feed Tank No. 6 Aux Une Feed Tank No. 6 Aux Une Feed Tank No. 6 Aim Une Feed Tank No. 6 Auk Une Feed Tank HAP HCBD HEXA PCBD* PENTA* PER SYM TCE HOBO HEXA PCBO* PENTA* PER SYM TCE HCBD HEXA PCBD* PENTA* PER SYM TCE HCBD HEXA PCBD* PENTA* PER SYM TCE HC60 HEXA PCBO* PENTA* PER SYM Mole Tank Percent Cater 0 Inside 1 Diameter (It) V Capacity (0N.) H Vapor Space Height (It) Ts Stared Liquid Temp. (oF) N Mv P Fp C Number at Molecular Partial Paint Smal KN Ttrnovers Weight Pressise Factor Diameter Turnover per Year (b/b mole) (psia) Factor Factor 1.29 Aqua Green 0.71 Aqua Green 0.74 Aqua Green 2.06 Aqua Green 87.16 Aqua Green 5.51 Aqua Green 2.52 Aqua Green 1.29 Aqua Green 0.71 Aqua Green 0.74 Aqua Green 2.08 Aqua Green 87.16 Aqua Green 5.51 Aqua Green 2.52 Aqua Green 1.29 Aqua Green 0.71 Aqua Green 0.74 Aqua Green 2.06 Aqua Green 87.16 Aqua Green 5.51 Aqua Green 2.52 Aqua Green 1.29 Aqua Green 0.71 Aqua Green 0.74 Aqua Green 2.08 Aqua Green 67.16 Aqua Green 5.51 Aqua Green 2.52 Aqua Green 1.29 Aqua Green 0.71 Aqua Green 0.74 Aqua Green 2.06 Aqua Green 87.16 Aqua Green 5.51 Aqua Green 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 1200 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 037 0.37 260.760 236.760 226.200 202.290 165.820 167.860 133.410 260.760 236.760 226.200 202.290 165.820 167.860 133.410 260.760 236.760 226.200 202.290 165.820 167.860 133.410 260.760 236.760 226.200 202.290 165.820 167.660 133.410 260.760 236.760 226 200 202.290 165.620 167.860 0.000 0.000 0.001 0.001 0.253 0.006 o.oto 0.000 0.000 0.001 0.001 0.253 0.006 0.010 0000 0.000 0.001 0.001 0.253 0.006 0.010 0.000 0.000 0.001 0.001 0.253 0.006 0.010 0.000 0.000 0.001 0.001 0.253 0.006 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1,00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1 00 = NON HAP, Emission is not included as a HAP emission. PPG 05/20/92 SUMMARY OF CALCULATED EMISSIONS FROM FIXED-ROOF STORAGE TANKS ASSOCIATED WITH THE PER/TRI PROCESS UNIT (PER/TRI) SL 026000 EIQ Tank NO. to Tank Description 360 600492 No. 4 Aux Line Feed Tar* 360 600492 No. 4 Aux Line Feed Tank 360 600492 No. 4 Aux Line Feed Tank 360 600492 No. 4 Aux Line Feed Tank 360 600492 No 4 Aux Una Feed Tank 360 600492 No. 4 Aux Une Feed Tank 360 600492 No. 4 Aux Line Feed Tank 360 600493 No. 3 Aux Line Feed Tank 360 600493 No! 3 Aux Line Feed Tar* 360 600493 No. 3 Aux Line Feed Tar* 360 600493 No. 3 Aux Line Feed Tar* 360 600493 No. 3 Aux Line Feed Tar* 360 600493 No. 3 Aux Une Feed Tar* 360 600493 No. 3 Aux Une Feed Tank 360 600494 No. 7 Aux Une Feed Tar* 360 600494 No. 7 Aux Une Feed Tank 360 600494 No. 7 Aux Une Feed Tar* 360 600494 No. 7 Aux Une Feed Tank 360 600494 No. 7 Aux Une Feed Tar* 360 600494 No. 7 Aux Une Feed Tank 360 600494 No. 7 Aux Une Feed Tank 360 600495 No. 5 Aux Una Feed Tar* 360 600495 No. 5 Aux Une Feed Tank 360 600495 No. 5 Aux Une Feed Tank 360 600495 No. 5 Aux Line Feed Tar* 360 600495 No. 5 Aux Line Feed Tar* 360 600495 No. 5 Aux Une Feed Tank 360 600495 No. 5 Aux Line Feed Tank 360 600496 No. 6 Aux Line Feed Tar* 360 600496 No. 6 Aux Line Feed Tank 360 600496 No. 6 Aux Line Feed Tar* 360 600496 No. 6 Aux Line Feed Tank 360 600496 No. 6 Aux Line Feed Tank 360 600496 N . 6 Aux Une Feed Tank = NON HAPS, emission is not included as a HAP emission HAP HC80 HEXA PCBO* PENTA* PER SYM TCE HCBO HEXA PC80* PENTA* PER SYM TCE HCBO HEXA PC BO* PENTA* PER SYM TCE HCBO HEXA PC BO* PENTA* PER SYM TCE HCBO HEXA PCBO* PENTA* PER SYM LB Breathing Lou 0.00028 0.00047 0.00000 0.00000 0.09415 0.00698 0.00809 0.00028 0.00047 0.00000 0.00000 0.09415 0.00696 0.00809 0.00028 0.00047 0.00000 0.00000 0.09415 0.00698 0.00809 0.00028 0.00047 0.00000 0.00000 0.09415 0.00698 0.00809 0.00Q28 0.00047 0.00000 0.00000 0.09415 0.00698 LW Working Loss <Mg/yr) 0.00000 0.00000 0.00000 0.00000 0.00249 0.00005 0.00008 0.00000 0.00000 0.00000 0.00000 0.00249 0.00005 0.00008 0.00000 0.00000 0.00000 0.00000 0.00249 0.00005 0.00008 0.00000 0.00000 0.00000 0.00000 0.00249 0.00005 0.00006 0.00000 0.00000 0.00000 0.00000 0.00249 0.00005 LT Total Loss (Mg/yr) Confcol Device 1987 Control Unweighted Efficiency HAP Emissions (%) (Mg/yr) 1987 Weighted HAP Emissions (Mg/*) 0.00028 0.00047 0.00000 0.00000 0.09664 0.00704 0.00816 0.00028 0.00047 0.00000 0.00000 0.09664 0.00704 0.00816 0.00028 0.00047 0.00000 0.00000 0.09664 0.00704 0.00816 0.00028 0.00047 0.00000 0.00000 0.09664 0.00704 0.00816 0.00028 0.00047 0.00000 0.00000 0.09664 0.00704 Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Snubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5 00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 0.00027 0.00044 0.00000 0.00000 0.09161 0.00669 0.00775 0.00027 0.00044 0.00000 0.00000 0.09181 0.00669 0.00775 0.00027 0.00044 0.00000 0.00000 0.09181 0.00669 0.00775 0.00027 0.00044 0.00000 0.00000 0.09181 0.00669 0.00775 0.00027 0.00044 0.00000 0.00000 0.09181 0.00669 0.00027 0.00044 0.00000 0.00000 0.09181 0.08686 0.00775 0.00027 0.00044 0.00000 0.00000 0.09161 0.06686 0.00775 0.00027 0.00044 0.00000 0.00000 0.09181 0.06686 0.00775 0.00027 0.00044 0.00000 ooogoo 0.09181 0.06686 0.00775 0.00027 0.00044 0.00000 0.00000 0.09181 0.06686 PPG 05/20/92 SL 026001 SUMMARY OF THE CALCULATION INPUTS FOR FIXED-ROOF STORAGE TANKS ASSOCIATED WITH THE PERCHLOROETHYLENE / TRICHLOROETHYLENE PROCESS UNIT ( PER / TRIJ EIQ Tank NO. ID Tar* Desorption 360 600496 No. 6 Aux Line Feed Tank 360 600499 No. 10 Aux Una Feed Tar* 360 600499 N . 10 Aux Une Feed Tar* 360 600499 No. 10 Aux Line Feed Tar* 360 600499 No. 10 Aux Line Feed Tar* 360 600499 No. 10 Aux Line Feed Tar* 360 600499 N . 10 Aux Line Feed Tar* 360 600499 N . 10 Aux Line Feed Tar* 360 600500 No. 9 Aux Line Feed Tank 360 600500 N . 9 Aux Une Feed Tank 360 600500 No. 9 Aux Line Feed Tank 360 600500 No. 9 Aux Line Feed Tex* 360 600500 N . 9 Aux Une Feed Tank 360 600500 No. 9 Aik Une Feed Tank 360 600500 No 9 Auk Une Feed Tank 360 600503 Heavies StW Feed Tar* 360 600503 Heavies Still Feed Tar* 360 600503 Heavies StHI Feed Tank 360 600503 Heavies StW Feed Tar* 360 600503 Heavies StW Feed Tar* 360 600503 Heavies Still Feed Tar* 360 600503 Heavies SIM Feed Tar* 360 600503 Heavies StlflFeed Tar* 360 600586 No. 1 PER/TRf Bottoms Tar* 360 600586 No. 1 PEfVTRI Bottoms Tank 360 600586 No. 1 PEfVTRI Bottoms Tar* 360 600586 No. 1 PEfVTRI Bottoms Tar* 360 600566 No. 1 PEFVTRI Bottoms Tar* 360 600586 No. 1 PEfVTRI Bottoms Tar* 360 600586 N . 1 PEFVTRI Bottoms Tar* 360 600566 No. 1 PEfVTRI Bottoms Tar* 360 600651 No. 6 Aux Une Feed Tank 360 600651 No. 8 Aux Une Feed Tank 360 600651 No. 8 Aux Une Feed Tank HAP TCE HCBD HEXA PCBO* PENTA* PER SYM TCE HCBO HEXA PCBO* PENTA* PER SYM TCE HCBD HEXA PC BO* PENTA* PER SYM TCE UNSYM* EDC HCBD HEXA PENTA* PER SYM TCE UNSYM* HCBO HEXA PCBD* Mole Percent Tank Color 0 Inside 1 Diameter (It) V Capacity (0al) H Vapor Specs Haight (ft) Ts Stored Liquid Temp. (oF) N Mv P FP C Number at Molecular Partial Paint Small KN Turnovers Weight Pressure Factor Olameter Turnover par Year (b/b mole) (psia) Factor Factor 2 52 Aqua Green 1.29 Aqua Green 0.71 Aqua Green 0.74 Aqua Green 2.06 Aqua Green 87.16 Aqua Green 5.51 Aqua Green 2.52 Aqua Green 1.29 Aqua Green 0.71 Aqua Green 0.74 Aqua Green 2.06 Aqua Green 67.16 Aqua Green 5.51 Aqua Green 2.52 Aqua Green 2.61 Aqua Green 0.72 Aqua Green 1.13 Aqua Green 1.68 Aqua Green 92.27 Aqua Green 1.01 Aqua Green 0.38 Aqua Green 0.20 Aqua Green 3.44 Lt Beige 5.22 Li Beige 3.59 Lt. Beige 10.10 Lt Beige 41.05 Lt Beige 11.15 U. Beige 15.31 Lt Beige 10.14 Lt Beige 1.29 Aqua Green 0.71 Aqua Green 0.74 Aqua Green 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 f2.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 14700 20000 20000 20000 20000 20000 20000 20000 20000 20000 20000 20000 20000 20000 20000 20000 20000 14700 14700 14700 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 t2.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 70.00 70 00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 150.00 150.00 150.00 150.00 150.00 150.00 150.00 150.00 130.00 130.00 130.00 130.00 130.00 130.00 130.00 130.00 70.00 70.00 70.00 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 0.37 380.53 380.53 360.53 360.53 360.53 360.53 380.53 360.53 461.68 461.88 461.68 461.88 461.88 461.88 461.88 461.88 0.37 0.37 0.37 133.410 260.760 236.760 226.200 202.290 165.620 167.660 133.410 260.760 236.760 226.200 202.290 165.620 167.860 133.410 260.760 236.760 226.200 202.290 165.820 167.860 133.410 167.664 98.970 260.760 236.760 202.290 165.820 167.660 133.410 167.864 260.760 236.760 226.200 0.010 0.000 0.000 0.001 0.001 0.253 0 006 0.010 0000 0.000 0.001 0.001 0.253 0.006 0.010 0.003 0.001 0.009 0.011 2.119 0.010 0.011 0.004 0.167 0.005 0.003 0 040 0.597 0.064 0.262 0.111 0.000 0.000 0.001 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 1.30 0.6046 0.6046 0.6046 0.6046 0.6046 0.6048 0.6046 0.6046 0.6046 0.6046 0.6046 0.6046 0.6048 0.6046 0.6046 0.6048 0.6046 0.6046 0.6046 0.6046 0.6046 0.6046 0.6046 0.6046 0.6046 0.6046 0.6046 0.6046 0.6046 0.6046 0.6046 0.6046 0.6046 0.6046 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 0.25 0.25 0.25 0.25 0.25 0 25 0.25 0.25 0.23 0.23 0.23 0.23 0.23 0.23 0.23 0.23 1.00 1.00 1.00 = NON HAP, Emission is ncrt included as a HAP emission. PPG 05/20/92 SUMMARY OF CALCULATED EMISSIONS FROM FIXED-ROOF STORAGE TANKS ASSOCIATED WITH THE PER / TRI PROCESS UNIT ( PER / TRI) SL 026002 F-1Q EK3 Tar* NO. 10 Tar* Description 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 360 600496 600499 600499 600499 60-0499 600499 600499 600499 600500 600500 600500 600500 600500 600500 600500 600503 600503 600503 600503 600503 600503 600503 600503 600566 600566 600586 600566 600566 600566 600566 600566 600651 600651 600651 No. 6 Auk Lino Peed Tar* No. 10 Auk Line Feed Tar* No. 10 Aux Una Feed Tar* No. 10 Aux Line Feed Tar* No. 10 Aux Una Feed Tar* No. 10 Aux Line Feed Tar* No. 10 Aux Line Feed Tar* No. 10 Aux Una Feed Tar* No. 9 Aux Una Feed Tar* No. 9 Aux Line Feed Tar* No. 9 Aux Line Feed Tar* No. 9 Aux Una Feed Ter* No. 9 Aux Line Feed Tar* No. 9 Aux Line Feed Tar* No. 9 Aux Line Feed Tank Heavies SMI Feed Tar* Heavies Still Feed Tar* Heavies Still Feed Tar* Heavies Still Feed Tar* Heavies Still Feed Tar* Heavies SMI Feed Tar* Heavies SMI Feed Tar* Heavies SMI Feed Tar* No. 1 PER/TRi Bottoms Tar* No. 1 PER/TRI Bottoms Tar* No. 1 PER/TRI Bottoms Tank No. 1 PER/TRI Bottoms Tar* No. 1 PER/TRI Bottoms Tank No. 1 PER/TRI Bottoms Tank No. 1 PER/TRI Bottoms Tar* No. 1 PER/TRI Bottoms Tank No. 8 Aux Line Feed Tank No. 8 Aux Une Feed Tank No. 6 Aim Une Feed Tar* NON HAPS, emission to not included as a HAP amission HAP TCE HCBO HEXA PCBO* PENTA* PER SYM TCE HCBO HEXA PCBO* PENTA* PER SYM TCE HCBO HEXA PCBO* PENTA* PER SYM TCE UNSYM* EDC HCBO HEXA PENTA* PER SYM TCE UNSYM* HCBO HEXA PCBO* LB Breathing Loss (Mfl/yr) 0.00809 0.00028 0.00047 0.00000 0.00000 0.09415 0.00698 0.00809 0 00026 0.00047 0.00000 0.00000 0.09415 0.00698 0.00809 0.00696 0.00296 0.00000 0.00000 0.43906 0.01018 0.00892 0.00000 0.04562 0.01046 0.00564 0.00000 0.17176 0.03714 0.08172 0.00000 0.00028 0.00047 0.00000 LW Working Loss (Mg/yr) 0.00008 0.00000 0.00000 0.00000 0.00000 0.00249 0.00005 0.00006 0.00000 0.00000 0.00000 0.00000 0.00249 0.00005 0.00008 0.01523 0.00453 0.00000 0.00000 7.15460 0.03273 0.03003 0.00000 0.43136 0.03175 0.01411 0.00000 2.30975 0.25073 0.87740 0.00000 0.00000 0.00000 0.00000 LT Total Loss (Mg/yr) Conkol Device 1987 Control Unweighted Efficiency HAP Emissions (%) (Mg/yr) 1987 Weighted HAP Emissions (Mg/yr) 0.00816 0.00028 0.00047 0.00000 0.00000 0.09664 0.00704 0.00816 0.00028 0.00047 0.00000 0.00000 0.09664 0.00704 0.00816 0.02220 0.00749 0.00000 0.00000 7.59368 0.04291 0.03884 0.00000 0.47698 0.04221 0.01995 0.00000 2.48151 0.28787 0.95912 0.00000 0.00028 0.00047 0.00000 Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrtfcber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 0.00775 0.00027 0.00044 0.00000 0.00000 0.09181 0.00669 0.00775 0.00027 0.00044 0.00000 0.00000 0.09181 0.00669 0.00775 0.02109 0.00712 0.00000 0.00000 7.21400 0.04076 0.03899 0.00000 0.45313 0.04010 0.01896 0.00000 2.35744 0.27348 0.91116 0.00000 0.00027 0.00044 0.00000 0.00775 0.00027 0.00044 0.00000 0.00000 0.09181 0.06686 0.00775 0.00027 0.00044 0.00000 0.00000 0.09161 0.06686 0.00775 0.02109 0.00712 0.00000 0.00000 7.21400 0.40781 0.03699 0.00000 0.45313 0.04010 0.01896 0.00000 2.35744 2.73460 0.91116 0.00000 0.00027 0.00044 0.00000 PPG 05/20/92 tC~Or o SUMMARY OF THE CALCULATION INPUTS FOR FIXED-ROOF STORAGE TANKS m ASSOCIATED WITH THE PERCHLOROETHYLENE / TRICHLOROETHYLENE PROCESS UNIT ( PER / TRI) Era Tank NO. 10 Tank Description 360 600651 N . 8 Ai* line Feed Tank 360 600651 No. 6 Aik Une Feed Tank 360 600651 No. 6 Auk Line Feed Tank 360 600651 No. 8 Auk Une Feed Tank 360 60-1663 No. 2 PER/TRI Bottoms Feed Tank 360 60-1683 No. 2 PER/Tfli Bottoms Feed Tank 360 60-1683 No. 2 PEFVTRI Bottoms Feed Tank 360 60-1683 No. 2 PER/TRI Bottoms Feed Tmk 360 60-1683 No. 2 PEFVTRI Bottoms Feed To* 360 60-1683 No. 2 PEFVTRI Bottoms Feed Tank 360 60-1683 No. 2 PEFVTRI Bottoms Feed Tank 360 60-1683 No. 2 PEFVTRI Bottoms Feed Tank 362 60605 PEFVTRI BIM Tank No. 1 363 60647 PEFVTRI BLM Tarfc No. 2 376 60-1865 Dowthsrm "A" Mekong Tank 376 60-1865 Dowthsrm *A* Make-ip Tank 377 60-2173 Dowthsrm Ftecyde H20 Recovery Tank 377 60-2173 Dowthsrm Recycle H20 Recovery Tank 377 800173 Dowthsrm Recycle H20 Recovery Tark HAP Mole Percent Tank Cotar D Inside Diameter UL> V Capacity (9*> H Vapor Space Haight (ft.) Ts Stared Liquid Temp. (oF) N Mv P Tp C Number of Molecular Partial Paint Small KN Ttsnever* Weight Pressure Factor Diameter Tirnover per Year (b/b mole) (peia) Factor Factor PENTA* PER SYM TCE EDO HCBO HEXA PENTA* PER SYM TCE UNSYM* Butylene Ok Butylene Ok BIPHENYL DIPHENYLi BIPHENYL DIPHENYL* H20* 2.08 Aqua Green 87.16 Aqua Green 5.51 Aqua Green 2.52 Aqua Green 3.44 U. Beige 5.22 Lt Beige 3.59 U. Beige 10.10 Lt. Beige 41.05 Lt Beige 11.15 Ll. Beige 15.31 Lt Beige 10.14 U. Beige 100.00 Yellow 100.00 Green 27.00 While 73.00 Whits 0.00 Green 0.00 Green 100.00 Green 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 9.00 900 10.00 to.oo 12.00 12.00 12.00 14700 14700 14700 14700 20000 20000 20000 20000 20000 20000 20000 20000 6000 4100 8700 8700 6768 6768 6768 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 10.00 0.00 6.00 6.00 5.00 5.00 5.00 70.00 70.00 70.00 70.00 130.00 130.00 130.00 130.00 130.00 130.00 130.00 130.00 70.00 70.00 200.00 200.00 200.00 200.00 200.00 0.37 0.37 0.37 0.37 525.00 525.00 525.00 525.00 525.00 525.00 525.00 525.00 4.25 0.00 0.24 0.24 0.31 0.31 0.31 202.290 165.820 167.860 133.4t0 98.970 260.760 236.760 202.290 165.620 167.860 133.410 167.864 72.120 72.120 166.000 166.000 166.000 166.000 18.020 0.001 0.253 0.006 0.010 0.187 0.005 0.003 0.040 0.597 0.064 0.282 0.111 2.708 2.708 0.014 0.037 0.000 0.000 11.380 1,30 0.6046 1.30 0.6046 1.30 0.6048 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.8046 1.30 0.6046 1.30 0.6046 1.30 0.8046 1.30 0.6046 1.30 0.6046 1.30 0.4552 1.30 0.4552 1.00 0.5076 1.00 0.5078 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.00 1.00 1.00 1.00 0.22 0.22 0.22 0.22 0.22 0.22 0.22 0.22 1.00 too 1.00 too 1.00 1.00 1.00 = NON HAP, Emission is not Included as a HAP emission. SL 026004 PPG 05/20*92 SUMMARY OF CALCULATED EMISSIONS FROM FIXED-ROOF STORAGE TANKS ASSOCIATED WITH THE PER/TRI PROCESS UNIT (PER/TRI) EIQ Tank NO. 10 Tank Description 360 600651 No. 8 Aux Una Feed Tank 360 600651 No. 6 Aux Una Faad Tank 360 600661 No. 6 Aux Una Faad Tank 360 600661 No. 8 Aux Una Faad Tank 360 60-1663 No. 2 PER/TRi Bottoms Faad Tank 360 60-1683 No. 2 PER/TRI Bottoms Faad Tank 360 60-1683 No. 2 PER/TRI Bottoms Faad Tank 360 60-1683 No. 2 PER/TRI Bottoms Faad Tank 360 60-1683 No. 2 PER/TRI Bottoms Faad Tank 360 60-1683 No. 2 PER/THI Bottoms Faad Tank 360 60-1683 No. 2 PER/TRI Bottoms Faad Tank 360 60-1683 No. 2 PER/TRI Bottoms Faad Tank 362 80606 PER/TRI BLM Tank No. 1 363 60647 PER/TRI BLM Tank No. 2 376 60-1865 Dowtherm *A* Make-tp Tank 376 60-1866 Oowtherm 'A* Make-up Tank 377 60-2173 Dowtherm Recycle H20 Recovery Tank 377 60-2173 Dowtherm Racyda H20 Recovery Tank 377 602173 Dowtharm Recycle H20 Recovery Tank HAP LB Breathing Loss (Mg/yr) PENTA* PER SYM TCE EDC HCBO HEXA PENTA* PER SYM TCE UNSYM* Butylene Oxide Butylene Oxide BIPHENYL DIPHENYL.OX* BIPHENYL DIPHENYL.OX* H20* 0.00000 0.09415 0.00698 0.00809 0.04562 0.01046 0.00584 0.00000 0.17176 0.03695 0.08172 0.00000 0.09723 0.00000 0.00426 0.00000 0.00000 0.00000 0.00000 LW wUfonnJtri1n--g- Loss (Mg/yr) 0.00000 0.00249 0.00005 0.00008 0.47378 0.03487 0.01560 0.00000 2.53690 0.27332 0.96369 0.00000 0.05430 0.00000 0.00005 0.00000 0.00000 0.00000 0.00000 LT Total Lou (M9/yr) Control Davies 1987 Confcol Unweighted Efficiency HAP Emissions <%> (Mg/yr) 1987 Weighted HAP Emissions (Mg/yr) 0.00000 0.09664 0.00704 0.00616 0.51940 0.04534 0.02134 0.00000 2.70866 0.31028 1.04540 0.00000 0.15153 0.00000 0.00432 0.00000 0.00000 0.00000 0.00000 Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Scrubber Nona Nona Nona Nona Nona Nona Nona 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 5.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00000 0.09181 0.00669 0.00775 0.49343 0.04307 0.02027 0.00000 2.57323 0.29476 0.99313 0.00000 0.15153 0.00000 0.00432 0.00000 0.00000 0.00000 0.00000 0.00000 0.09181 0.06686 0.00775 0.49343 0.04307 0.02027 0.00000 2.57323 2.94764 0.99313 0.00000 0.15153 0.00000 0.00432 0.00000 0.00000 0.00000 0.00000 * NON HAPS, emission is not included as a HAP emission ENSR APPENDIX E-B PER/TRI PROCESS UNIT PROCESS VENT CALCULATION 5510R016.01A SL 026005 E-22 Final 05/27/92 Source: HON subunit(s^ Pgrchloroethvlene/Trichloroethylene Process Units________________ __________________________ HAPs emitted: VinvL_Chlor_ide_fVa . Vinvlidene .Chloride fVDC) . 1.1-Dichloroethane (DCE). Chloroform. Carbon Tetrachloride. Trichloroethylene (TCE1. Ethvl Chloride fEC^ CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: Vinyl Chloride (VC)_______________ Year: 1987 Calculator: Date: April 1992 S.R. Process Vent Identificatioh: 303 (non-routine) Description: __Per/Tri Startup Scrubber__________________________ Process Conditions/Sampling Date of flow measurement 1983 Method of flow measurement Hot Wire Anemometer Date of concentration measurement 1990 Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) Svrinae Sample. GC/TCD Describe any problems encountered during testing None. Identified Production rate during flow determination (lbs/hr) 14.810* Production rate during sampling (lbs/hr) 15.QoJ1 Average production rate during base year (lbs/hr) 20.105 Stream Characteristics Average vent stream flow rate (ft3/min) HAP concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risk weighting factor -222___________ = Q 2.JS.42________ = c 88________ = h 80________ = T 63________ = MW ___U.r 7_______ = P ------10------------ = fhr Control device Scrubber_____________ __ __ __ __ HAP control efficiency (%) _______ 5 = eff Calculations* Uncontrolled Emissions (E0) = (2.54E-09) o C h MW P T + 460 uncontrolled Emissions (Ew) * (2.54E-09)(7921(2.842)(881(631(14.7) _______(80) + 460 0.863 Mg/yr HAP Emissions (E^p) * E0 (1 - eff/100) 1See next page. SL 026006 E-23 Sourc : HON subunit(s) Process Units________________ Perchloroethvlene/Trichloroethylene CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (Eh&p) * 0.863 (1 - 5/100) 0.820 Mg/yr Weighted HAP Emissions EHAP Weighted HAP Emissions = (0.82) fhr (10) 8.197 Mg/yr Total HAP Emissions* = Total Weighted HAP Emissions = 6.759 Mg/yr 30.543 Mg/yr If the conditions during testing are not representative of has year operation, make the appropriate extrapolation below and explain: This is the non-routine scenario of Stack 303. composition data for this vent is available from 1990. The In order to be consistent with operating conditions in 1987, the 1987 stack flow rate was used which was the same as the flow rate measured in 1983. If the flow or concentration were not measured using an epa r ference method, EPA conditional method or validated using Method 301, provide justification and supporting calculations: N/A Expression provided in "Procedures for Establishing Base Year and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. See Attachment I for calculation results for other HAPs emitted. SL 026007 E-24 SL 026008 ATTACHMENT I SUBUNIT: VENT ID: SCENARIO: DESCRIPTION: PERfTRI 303 NON-ROUTINE PEFVTRI 8TARTUP SCRUBBER* YEAR: 1867 Q Average vent stream flow rate (ftSAnin) C HAP Concentration (ppmv) h Annual hours of operation (hrs) T Vent stream discharge temperature (F) MW HAP molecular weight (Ip/lb-mole} P Pressure at point of discharge (psia) FHR HAP high risk weighting factor eff HAP control efficiency (%) EU Uncontrolled emissions (Mg/yr) EU - (2.54E-08xQxCxhxMWxP)/(T + 460) EHAP Controlled emissions (Mgfyr) EHAP EUx(l - (eftrioo)) MI EW Weighted HAP emissions (Mg/yr) ; EW - EHAP x FHR tUo1 COMPONENT Q C h MW P T eff FHR EU EHAP EW VC 792 2,842 88 63 14.7 80 5.00 10 0.863 0.620 8.197 VDC 792 4,105 88 97 14.7 80 5.00 10 1.919 1.823 18.229 DCE 792 947 88 99 14.7 60 5.00 1 0.452 0.429 0.429 CHCL3 792 737 88 119 14.7 60 5.00 1 0.423 0.402 0.402 CCL4 792 947 88 154 14.7 60 . 5.00 1 0.703 0.668 0.666 TRI 792 4,211 86 131 14.7 80 5.00 1 2.658 2.525 2.525 EC 792 316 88 64 14.7 80 5.00 1 0097 0.093 0.093 FILE: Ml 2 TOTAL 7.115 6.759 30.543 Sourc : HON subunit (si P_erchlQroethvlene/Trichloroethylene Process Units_______________ ________ __ HAPs emitted: Vinvl Chloride fVC). Vinvlidene Chloride fVDCl. l.1-Dichloroethane (DCE). Chloroform. Carbon Tetrachloride. Trichloroethylene fTCEl. Ethvl Chloride (EC) CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: Vinvl Chloride (VC)_______________ Year: 1987 __________________________ Date: April 1992 Calculator: S.R. Process Vent Identification: 303 (startup) Description: Per/Tri Startup Scrubber__________________________ Process Conditions/Samplinq Date of flow measurement Method of flow measurement Hot Wire Anemometer Date of concentration measurement Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) Syringe Sample, Describe any problems encountered during testing None Identified Production rate during flow determination (lbs/hr) Production rate during sampling (lbs/hr) Average production rate during base year (lbs/hr) 1983 1990 GC/TCD 14.810 15.002 20.105 Stream Characteristics Average vent stream flow rate (ft3/min) HAP concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risk weighting factor ___ 5_____ = Q 3*842 =C 74________ = h ____SO - =T 63________ = MW 14.7 =P ------- 12--------------- ~ fhr control Control device Scrubber_______ HAP control efficiency (%) _________5 = eff Calculations* Uncontrolled Emissions (Ew) = (2.54E-09^ o c h MW P T + 460 Uncontrolled Emissions (Ew) = 12-.54E-09) (55.4) (2.842) (74) (63) (14.7) _______ (80) + 460 0.051 Mg/yr HAP Emissions (E^p) = E0 (l - eff/100) SL 026009 E-26 Source: HON subunit(s) Process Units________________ Perchloroethvlene/Trichloroethylene CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (E^p) = 0.051 (1 - 5/100) 0.048 Mg/yr Weighted HAP Emissions Weighted HAP Emissions ehap (0.048) fhr (10) 0.483 Mg/yr Total HAP Emissions** Total Weighted HAP Emissions * 0.398 Mg/yr 1.798 Mg/yr If the conditions during testing are not representative of bas year operation, make the appropriate extrapolation below and explain: This is the startup scenario of Stack 303. Emission concentrations from the source are same as those in non routine scenario. Composition data are available from 1990. If the flow or concentration were not measured using an EPA reference method, EPA conditional method or validated using Method 301, provide justification and supporting calculations: N/A Expression provided in "Procedures for Establishing Base Year and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. *See Attachment I for calculation results for other HAPs emitted. SL 026010 E-27 T r0 9Z0 C/} t-< WI SUBUNIT; VENT fO: SCENARIO: DESCRIPTION: ATTACHMENT I PER/TRI 303 8TARTUP PEfVTRI 8TARTUP SCRUBBER' Q C h T MW P FHR eff EU EHAP EW Average vent stream flow rate (ftSAnin) HAP Concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (Ib/lb-mole) Pressure at point of discharge (peia) HAP high risk weighting factor HAP control efficiency (%) Uncontrolled emissions (Mg/yr) ; Controlled emissions (Mg/yr) ; Weighted HAP emissions (Mg/yr) ; YEAR; 1BB7 EU - (2.S4E-09 xQxCxhx MW x P) / (T + 460} EHAP - EU x (i - (efl/ioo)) EW - EHAP x FHR COMPONENT VC VDC DCE CHCL3 CCL4 TRI EC Q 55.44 55.44 55.44 55.44 55.44 55.44 55.44 C 2,342 4,105 947 737 947 4,211 316 h 74 74 74 74 74 74 74 MW 63 97 99 119 154 131 64 P 14.7 14.7 14.7 14.7 14.7 14.7 14.7 T 60 60 80 60 60 80 60 eff 5.00 5.00 5.00 5.00 5.00 5.00 5.00 FHR 10 10 1 1 1 1 1 EU 0.051 0.113 0.027 0.025 0.041 0.156 0.006 EHAP 0.048 0.107 0.025 0.024 0.039 0.149 0005 EW 0.463 1.073 0.025 0.024 0.039 0.149 0.005 FILE;N12A TOTAL 0.419 0.396 1,798 Source: HON subunitfg)___ Perchloroethvlene/Trichloroethylene Process Units _____ __________________ ___ HAPs emitted: Vinvlidene Chloride (VDC). Carbon Tetrachloride (CCl^ . Trichloroethylene (Tril, Perchloroethvlene fPer) CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: Vinvlidene Chloride (VDC) Year: 1987_____________________________ Date: April 1992 Calculator: S.R. Process Vent Identification: 339 Description: _Fer/Tri Still Line Vent Scrubber________________ Process Conditions/Sampling Date of flow measurement 1987 Method of flow measurement Hot Wire Anemometer Date of concentration measurement 1987 Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) Integrated Baa Sample. GC/TCD or FID Describe any problems encountered during testing None Identified Production rate during flow determination (lbs/hr) 16.372 Production rate during sampling (lbs/hr) 16,372 Average production rate during base year (lbs/hr) 16.372 Str^p charac&erjgtjgff Average vent stream flow rate (ft3/min) HAP concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risJc weighting factor ________16.6 14.737 8.760 ________80 97 ________14.7 10 Coa&rol Control device Scrubber___________________________________________ HAP control efficiency (%) ___________5 * eff Calculations* Uncontrolled Emissions (Ey) = C2.54E-091 o C h MW P T + 460 Uncontrolled Emissions (E0) * (2.54E-09) (16.6) (14.737) f8.760) (97) (14.7) (80) + 460 14.338 Mg/yr HAP Emissions (E^p) = E0 (1 - eff/100) SL 026012 E-29 Source: HON subunit(s) Perchloroethvlene/Trichloroethylene Process Units_______________________ _______________________ _______________________________ CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (E^p) ** 14.338 (1 - 5/100) 13.622 Mg/yr Weighted HAP Emissions E^p F^ Weighted HAP Emissions = (13.622) (10) 136.215 Mg/yr Total HAP Emissions* = Total Weighted HAP Emissions = 67.524 Mg/yr 190.118 Mg/yr If the conditions during testing are not representative of base y ar peration^ make the appropriate extrapolation below and explain: N/A If the flow or concentration were not measured using an EPA refer nee method, EPA conditional method or validated using Method 301/ provide justification and supporting calculations: N/A Expression provided in ''Procedures for Establishing Base Year and PostReduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. *See Attachment I for calculation results for other HAPs emitted. SL 026013 E-30 Cfl )*1 J 26014 SUBUNIT: VENT 10: SCENARIO: DESCRIPTION: ATTACHMENT I PEFVTRI 838 NORMAL PEFf/TRI 8T1LL UNE VENT 8CRUBBER Q C h T MW P FHR eff EU EHAP EW Average vent stream flow rate (ft3Anin) HAP Concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (Ib/lb-mole) Pressure at point of discharge (psia) HAP high risk weighting factor HAP control efficiency (%) Uncontrolled emissions (Mgfyr) Controlled emissions (Mgfyr) Weighted HAP amissions (Mg/yr) ; YEAR; tsar EU - (2.54E-09xQ xC * hxMWx P) / (T + 460) EHAP - EU * (i - (ft/ioo)) EW - EHAP x FHR COMPONENT VDC CCL4 TRI PER Q 16.56 16.56 16.56 16.56 C 14,737 22,105 10,526 5,263 h 6760 6760 6760 6760 MW 97 154 131 166 P 14.7 14.7 14.7 14.7 T 80 60 80 60 eff 5.00 5.00 5.00 5.00 FHR 10 1 1 1 EU 14.336 34.145 13.631 6,763 EHAP 13.622 32.436 13.140 6325 EW 136.215 32.436 13.140 6.325 FILE: N29 TOTAL 71.076 67.524 190.116 Source: ___ subunitfsi P-grchloroethy lene /Tr ichloroethvlene Process Units________________ HAPs emitted: Vinvlidene Chloride fVDCl. Methylene Chloride _fMECl2l . Vinvl Chloride__fVC) .__1. l-Jichloroethane__(DCE) . Carbon Tetrachloride fCCl^. Trichloroethylene fTril . CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: 1.1-Dichloroethane (DCE)________ Year: 1987____________________________ Date: .April 199? Calculator: S.R. Process Vent Identification: 340 (non-routine) Description: Per/Tri DH System Vent Scrubber_________________ Process Conditions/Sampling Date of flow measurement 1987 Method of flow measurement Helium injected as flow tracer Date of concentration measurement 1987 Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) Svrinoe sample. GC/TCD Describe any problems encountered during testing None Identified Production rate during flow determination (lbs/hr) 16.372 Production rate during sampling (lbs/hr) 16.372 Average production rate during base year (lbs/hr) 16.372 Stream Characteristics Average vent stream flow rate (ft3/min) HAP concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risk weighting factor _________3.53 3.789 _________9.75 ________80 99 ________14.7 l figntTPl Control device Incinerator HAP control efficiency (%) ___________5.0 = eff Calculations* Uncontrolled Emissions (E0) = (2.54E-091 o C h MW P T + 460 Uncontrolled Emissions (Ey) * (2.54E--09)(3.531(3.7891(9.751(991(14.71 _______ (80) + 460 0.001 Mg/yr HAP Emissions (E^p) = E0 (1 - eff/100) SL 026015 E-32 Source: HON subunit(s) Process Units________________ Perchloroethvlene/Trichloroethylene CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (E^p) = 0.001 (1 - 5.0/100) 0.001 Mg/yr Weighted HAP Emissions Weighted HAP Emissions ehap (0.001) fhr (1) 0.001 Mg/yr Total HAP Emissions** = Total Weighted HAP Emissions * 0.095 Mg/yr 0.901 Mg/yr If the conditions during testing ere not representative of base year operation, make the appropriate extrapolation below and explain: N/A If the flow or concentration were not measured using an EPA reference method, EPA conditional method or validated using Method 301, provide justification and supporting calculations: N/A Expression provided in "Procedures for Establishing Base Year and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. *See Attachment I for calculation results for other HAPs emitted. SL 026016 E-33 ATTACHMENT I SL 026017 SUBUNIT: VENT ID: SCENARIO: DESCRIPTION: PER/TRI 340 NON-ROUTINE PERfTRI DH 8YSTEM VENT YEAR: 1967 Q C h T MW P FHR ff EU EHAP EW Average vent stream flow rate (ftSAnin) HAP Concentration (ppmv) Annual hours of operation (hrs) Vent strewn discharge temperature (F) HAP molecular weight (Ib/lb-mole) Pressure at point of discharge (peia) HAP high risk weighting factor HAP control efficiency (%) Uncontrolled emissions (Mg/yr) ; Controlled emissions (Mg/yr) Weighted HAP emissions (Mg/yr) ; EU (2.54E-09 nQxCxhx MW x P) / (T + 460) EHAP - EUx(t - (ef^ioo)) EW - EHAP x FHR m 2 COMPONENT Q C h MW P T eff FHR EU EHAP EW VC 3.53 116,342 9.75 63 14.7 60 5.00 10 0.018 0.017 0.166 MECL2 3.53 211 9.75 85 14.7 60 5.00 1 0.000 0.000 0.000 VDC 3.53 332,632 9.75 97 14.7 80 5.00 10 0.077 0.073 0.729 DCE 3.53 3,789 . 9.75 99 14.7 80 5.00 1 0.001 0.001 0.001 CCL4 3.53 10,526 9.75 154 14.7 80 5.00 1 0.004 0.004 0.004 TRI 3.53 2,737 9.75 131 14.7 80 5.00 1 0.001 0.001 0.001 FILE: M30 TOTAL 0,100 0.095 0.901 Source: HON subunit (si Perchloroethvlene/Trichloroethylene Process Units HAPs emitted: Vinvl Chloride (VC) .__vinylidene__Chloride (VDC) . Ethvlene__Dichloride___(EDC) ,___chloroform.___Methyl__Chloroform JMC) . Trichloroethylene_____(Iri.).,____ 1.1.2-Trichloroethane_____(TCE). Perchloroethvlene.(Per) CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: Vinvl Chloride (VC) Year: 1987 Date: April 1992 Calculator: S.R. Process Vent Identification: ?41 Description: Per/Tri Acid JTenlL Scrubber ._ Process Conditions/Sampling Date of flow measurement Method of flow measurement Calculated Date of concentration measurement Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) Svrinae Sample. Describe any problems encountered during testing __None Identified Production rate during flow determination (lbs/hr) Production rate during sampling (lbs/hr) Average production rate during base year (lbs/hr) ----1979 GC/TCD not available not available not availabl Stream Characteristics Average vent stream flow rate (ft3/min) HAP concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (WF) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risk weighting factor _________0.0374 48.254 8.760 ________80 3 ________14.7 10 CQptrfll Control device Scrubber___________________________________ HAP control efficiency (%) __________________ = eff Calculations* Uncontrolled Emissions Uncontrolled Emissions (E0) * (2.54E-09) 0 c h MW P T + 460 (Ew) = .(2r-54E~P9).(01Q3?(AS.25*11$ .2QU.,g3JJ, 14^.7). (80) + 460 0.069 Mg/yr HAP Emissions (E^p) = E0 (1 - eff/100) SL 026018 E-35 Source: units HON subunit(s) Perchloroethvlene/Trichloroethylene Process CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (E^) - 0.069 (1 - 5/100) 0.065 Mg/yr Weighted HAP Emissions - ehap Weighted HAP Emissions - (0.037) fhr (1) 0.654 Mg/yr Total HAP Emissions* * Total Weighted HAPs Emissions ** 1.964 Mg/yr 5.956 Mg/yr If the conditions during testing are not representative of base year peration, melee the appropriate extrapolation below and explain: Composition data are available (from CADY report to Schwarzauer "Acid Pit Vents" 2-22-79) for EIQ 341 (Lift Station No. 2). These are shown on the attached Table 1 in lb/day. (EIQ 341 was excluded from calculation of lift station emissions. See "Lift Station Emission Calculations" in Appendix J.) The mole/hr values were calculated from mass emission rates and are shown on Table 1 below. E-36 SL Source Unit? HON subunit(s) _Perchloroethvlene/Trichloroethylene Process Component MW VC 63 VDC 97 EDC 99 CHCL3 119 MC 133 TRI 131 TCE 133 PER TRANS* CIS* 166 97 97 TOTAL MASS RATE TOTAL MOLES TABLE 1 Mass Emission Rates M (lb/day) 0.41 2.37 2.13 5.19 0.007 0.67 0.84 0.69 2.4 0.007 14.714 (lb/tir) 0.171 0.0988 0.0888 0.2163 0.0003 0.0279 0.0350 0.0287 0.1000 0.0003 0.6131 m (mole/hr) 0.000271 0.001018 0.000896 0.001817 0.000002 0.000213 0.000263 0.000173 0.001031 0.000003 0.005688 C ppmv 48,254 181,161 159,526 323,376 390 37,922 46,829 30,820 183,454 535 Total emissions as shown on Table 1 is 0.0057 mole/hr for the vent. The volumetric emission rate can be calculated as follows (at vent temperature of 80F): 0.0057 mole X hr 359 f3 X mole 88 + 460 = 2.247 ft3 32 + 460 hr or: 2.247 x 1 hr 0.0374 ft3 hr 60 min min SL 026020 E-37 Sourc : HON subunit(s) Perchloroethvlene/Trichloroethvlene Process Units______________________ Similarly for each vent the volumetric flow rate can be calculated using the above procedure, and the concentration of the HAP can be determined. Calculation for VC is shown below. 0.000271 x 359 x 88 460 0.10836 -- hr mole 32 + 460 hr 0,10836 ftVhr VC x 1,000,000 - 48,254 ppmv 2.247 ft3lhr total gas If the flow or concentration were not measured using an EPA referenc method, EPA conditional method or validated using Method 301, provide justification and supporting calculations: N/A* * "Expression provided in ''Procedures for Establishing Base Year and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. *See Attachment I for calculation results for other HAPs emitted. S^ E-38 ATTACHMENT I SL 026022 SUBUNIT: VENT ID: SCENARIO: DESCRIPTION: PER/TRI 341 NORMAL PER/mi ACID TANK SCRUBBER YEAR: 1007 Q Average vent stream fkm rate (ft3Anin) C HAP Concentration (ppmv) h Annual hours of operation (hre) T Vent stream discharge temperature (F) MW HAP moiecutar weight (Ib/lb-mote) P Pressure at point of discharge (pels) FHR HAP high risk weighting factor eft HAP control efficiency (%) EU Uncontrolled emissions (Mg/yr) ; EU - p.54E-oexQxC*h*MWxP)/{T + 460) EHAP Controlled emissions (Mg/yr) ; EHAP EUx(f - (aft/ioo)) EW Weighted HAP emissions (Mg/yr) ; EW - EHAP * FHR \CMoIJ COMPONENT Q C tl MW P T eft FHR EU EHAP EW VC 0.0374 43,254 8,760 63 14.7 80 5 10 0.069 0.065 0.654 VDC 0.0374 181,161 8,760 97 14.7 60 5 10 0.396 0.378 3,782 EDC 0.0374 159,526 8,760 09 14.7 60 51 0.356 0.340 0840 CHCL3 0.0374 323,378 8.760 119 14.7 80 5 1 0.872 0828 0.628 MC 0.0374 390 6,760 133 14.7 60 51 0.001 0.001 0.001 TRI 0.0374 37,922 8,760 131 14.7 80 5 1 0.113 0.107 0,107 TCE 0.0374 46,829 8,760 133 14.7 60 5 1 0.141 0.134 0,134 PER 0.0374 30,320 6,760 166 14.7 80 51 0.116 0.110 0.110 FILE: N341A TOTAL 2.067 1.964 5.956 Source: HON subunitPerchloroethvlene/Trichloroethylene Process Units____________________________________________________ HAPs emitted: Perchloroethvlene iPer). Trichloroethylene (Tri) CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: Trichloroethylene (Tri) Year: 198_7 Date: April 1992 Calculator: S.R. Process Vent Identification: 359__ Description: Per/Tri Product Drver Reaeneration Vent Process Conditions/Samplinq Date of flow measurement Method of flow measurement Calculated_______ Date of concentration measurement Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) Calculated Describe any problems encountered during testing N/A_______________ Production rate during flow determination (lbs/hr) Production rate during sampling (lbs/hr) Average production rate during base year (lbs/hr) not measured not measured 16.372 16.372 15,002 Stream Characteristics Average vent stream flow rate (ft^/min) none measured_______ HAP concentration (ppmv) none measured Annual hours of operation (hrs) 24 hr/reoeneration Vent stream discharge temperature (*F) not available_______ HAP molecular weight (lb/lb-mole) ______ lil = MW Pressure at point of discharge (psia) ________14.7__________ HAP high-risk weighting factor _________1 = FHR =Q =C =h =T =P caprol Control device Scrubber HAP control efficiency (%) __________ 5 = eff calculations1 61.46 Mg/yr HAP Emissions (Ehap) " eu f1 " eff/100) 1See next page. SL 026023 E-40 Source: Unite __ HON subunit(s) Perchloroethvlene/Trichloroethvlene Process CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (Eg^) 61.46 (l - 5/100) 58.40 Mg/yr Weighted HAP Emissions = ehap Weighted HAP Emissions (58.40) fhr (1) 58.40 Mg/yr Total HAP Emissions = Total Weighted HAPs Emissions * 87.14 Mg/yr 87.14 Mg/yr If the conditions during testing are not representative of base year peration, make the appropriate extrapolation below and explain: N/A If the flow or concentration were not measured using an EPA referenc method, EPA conditional method or validated using Method 301, pr vide justification and supporting calculations: These are emissions associated with Per and Tri regenerations. Defined by the process are the following: 2722.7 lb/regen. tri 734.3 lb/regen. per 24 hr/regen/ The emissions were calculated from the results of bench scale laboratory experiments. Emissions occur during the regeneration of activated alumina beds. Laboratory experiments were conducted to determine the amount of Per and Tri that could be absorbed by the beds during operation. SL 026024 E-41 Source: Units HON subunit(s) .Egrchloroethvlene/Trichloroethvlene Process Number of regenerations are not available for 1987, these data for 1990 were: = No. of Tri regeneration = 48 Rp * No. of per regeneration =83 Annual emissions are: RT x 2722.7 ---- TRh ---------- ------- - 59 MGJYR 2205 -- (metridj ton ' Rp x 734.3 ---- PER. --------- ----= 27 MGJYR 2205 -- (metric!) ton Production figures for 1987 and 1990 are as follows: TRI: PER: 1990 24245 41552 1987 25254 46551 Scale to 1987 level: PER. 27 x - 30.25 MGJYR 41552 TRh 59 x - 61.46 MGJYR 24245 TOTAL 91.71 MGJYR FHR is one for both TRI and PER. At 5% scrubber efficiency, emissions are: TRI: 58.40 PER: 28.74 TOTAL = 87.14 Expression provided in ''Procedures for Establishing Base Year and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. SL 026025 E-42 ENSR APPENDIX F SHIPPING AND LOADING PROCESS UNIT (S/L) 5S10H016.01 SL 026026 Rni OS/27/92 EK APPENDIX F SHIPPING AND LOADING PROCESS UNIT (S/L) F.l Process Description Finished products, which primarily include ethyl chloride, Tri-Ethane* (methyl chloroform), transdichloroethylene, vinylidene chloride, vinyl chloride, perchloroethylene, trichloroethylene, and ethylene dichloride, are loaded and shipped for distribution via drums, railcars, tank trucks, barges, and ships. The emission losses from loading and shipping were calculated for transfer and handling operations at the point of transfer, and do not include emissions from storage tanks. With the exception of the ethyl chloride loading emissions that are routed to the incinerators, shipping and loading emissions are considered fugitive emissions. F.2 1987 Base-Year Emissions Table F-1 shows the total base-year emissions for the shipping and loading process unit. The total unweighted HAP emissions were 164.4 Mg/yr. Since none of the pollutants emitted are considered high-risk pollutants and subject to multiplication by a weighting factor, the total weighted HAP base-year emissions equal the total unweighted HAP base-year emissions. F.3 Emissions Reduction Strategy Table F-2 shows the control strategy that will be implemented to help achieve a plantwide reduction in emissions for all SOCMI sources at the facility. The general control strategy is as follows: Emissions from tank car and tank truck loading will be routed to the incinerator (99% control): Emissions from drum loading will be routed to a carbon adsorption system (98% control); and Ship and barge loading emissions of EDC (only) will be routed initially to a vent recovery unit comprised of refrigerated condensers (98% control) followed by carbon adsorption (98% control). Emissions from other chemicals will not be controlled. 5S10R016.01A SL 026027 F-1 Final 05/27/92 TABLE F-1 1907 BASE YEAR EMISSIONS SHIPPING AND LOADING OPERATIONS (S/L) UNIT EIQ S/L 300 S/L 390 S/L 391 S/L 392 S/L 393 S/L 394 DESCRIPTION VDCM Tank Car Vent Ships * Barges * Rail Cars Tank Trucks Drums TYPE P F F F F F BASE YEAR CONTROL DEVICE TYPE % CONTROL HAP EMISSIONS UNWEIGHTED WEIGHTED MG/YR MG/YR None 0.00 130.910 130.910 Subtotal Process Vents 130.910 130.910 None 0.00 4.650 4.850 None 0.00 13.760 13.760 None 0.00 8.690 6.890 None 0.00 5.580 5.500 None 0.00 0.412 0.412 Subtotal Fugitive Sources 33.492 33.492 _________________ 1 Total Base Year Emissions | 164.402 * EDC emissions from ships and barges loading operations are controlled at 99.96%, all other compounds are not controlled. 164.402 FILE: SLBASE Crt tr1 too cr> o oto TABLE F--2 EMISSIONS REDUCTIONS STRATEGY AND POST REDUCTIONS EMISSIONS SHIPPING AND LOADING OPERATIONS (S/L) UNIT EIQ S/L 308 S/L 390 S/L 391 S/L 392 S/L 393 S/L 394 DESCRIPTION VDCM Tank Car Vent Ships * Barges * Rail Cars Tank Trucks Drums POST REDUCTION TYPE ADDITIONAL CONTROL 1004 % CONTROL HAP EM SSIONS UNWEIGHTED WEIGHTED MG/YR MG/YR P Incinerate 99.99 0.013 0.013 Subtotal Process Vents 0.013 0.013 F Ref. CondyCatbon Ad. 99.96 4.350 4.350 F Rei. Cond. 99.96 5.263 5.263 F Incinerate 99.99 0.001 0.001 F Incinerate 99.99 0.001 0.001 F Carbon Adsorption 98.00 0.006 0.008 Subtotal Fugitive Sources 9.624 9.624 _________________ 1 Total Post Reduction Emissions ] 9.637 * EDC emissions from ships and barges loading operations are controlled at 99.96%, all other compounds are not controlled. 9.637 RLE: SLPOST Ethyl chloride Is emitted from the only shipping and loading process vent (EIQ 308) during loading of tank trucks and railcars. Nitrogen will be used to pad the tank trucks and tank cars and the pad pressure used to force the emissions into the incinerator header system. F.4 Post-Reduction Emissions Table F-3 shows the total weighted and unweighted HAP emissions for the shipping and loading unit. EDC emissions from barges and ships shipping and loading operations are controlled at 99.96%. The unweighted and weighted total emissions are equal since none of the compounds need to be multiplied by a weighting factor. The total post-reduction emissions of 9.637 Mg/yr represent a 154.765 Mg/yr decrease (94.14% reduction) in base-year emissions. S510W16.01A SL 026030 F*4 Final 05/27/92 SL 026031 TABLE F-3 HAP EMISSIONS SUMMARY SHIPPING AND LOADING OPERATIONS (S/L) Unweighted HAP Emissions Weighted HAP Emissions Post Percent Post Percent Type Base Year Reduction Reduction Base Year Reduction Reduction (Units) P (Mgfri) 130.910 (MftYO 0.013 1%) 99.99 (MftYr) 130.910 (MflM 0.013 (%) 99.99 T F 33.492 9.6236 33.492 9.6236 Total Total Percent Reduction 164.402 9.637 94.14 164.402 9.637 94.14 p-ProcMVm> T-TnfcVntt F-FuqWw Emtoion* 8 / L-8Npping l Looting Timtar Opo*on flooding Np*. bargo*. terfc cars, tank tuck*, drums) APPENDIX F-A SHIPPING AND LOADING UNIT PROCESS VENT CALCULATIONS SL 026032 S510FU16.01A F-6 Final 05/27/92 source: shipping and Leading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: Ethvl Chloride (EC)___________ Year: 1982_________________________________ Date: April 1992______ Calculator: D. Seifert Loading Operation: Rail Car EIQ 3(18___________________________________ Loading Tamneterg Cargo carrier (tank truck, rail car, etc.) Mode of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) Temperature of liquid loaded (F) Weight percent HAP in the loaded material True vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Molecular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor (M co v Tank Car Other 5.452, 70 100 20.37 64.52 Other 1 QanttPl Control device HAP control efficiency (%) None 0.0 Calculation* Uncontrolled Loading Loss Ew* = 76.73 Mg/yr =G SZ T ss P M sS ss fhr eff HAP Emissions (Ehap) " Eu " eff/100) 76.73 (1 - 0/100) 76.73 Mg/yr *See backup calculations on page F-ll. SL 026033 F-7 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS (CONCLUDED) Calculation (continued! Weighted HAP Emissions = E^p FHP = (76.73) (1) 76.73 Mg/yr Calculation worksheet and procedure from "Procedures for Establishing Base Year and Post-reduction HAP Emissions." consistent with AP-42. This procedure is SL 02603* F-8 source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: Ethvl Chloride (EC)___________ Year: 1987________________________ Date: April J-992-------------- Calculator: D. Seifert Loading Operation: Tank Trucks EIQ 3OS__________________________________ Loading. FarapeJfcers cargo carrier (tank truck, rail car, etc.) Mod of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) T mperature of liquid loaded (F) Weight percent HAP in the loaded material True vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Mol cular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor lank.Tracks Other 1.434.393 _____________70___________ 100 20.37 64.52 Other l = SS5 = = HR Control Control device HAP control efficiency (%) None______________________ =i CAlsniatian* Uncontrolled Loading Loss Ey* =* 54.18 Mg/yr HAP Emissions (Ej^) = E0 (1 - eff/100) - 54.18 (1 - 0/100) 54.18 Mg/yr *See backup calculations on page F-12. SL 026035 F-9 CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS (CONCLUDED) Calculation (continued! Weighted HAP Emissions ~ ehap fhp = (54.18) Calculation worksheet and procedure from "Procedures for Establishing Bas Year and Post-reduction HAP Emissions." consistent with AP-42. This procedure is SL 026036 F-10 " ec ! ! i ; ----- * ! ii ll JEtL l--oaeli\*.a. f --i S/n/91 2sfi*rpPPG.-ec J'tr\ :r' zr $/o-ol u 1 ! M ! :1 ! 1 ; !: m ! ,\ ................... M ?~7 psc d LK c\i _ iC^xiow/saii C&cS___ --2?i J2=1.S . | -Jjphn.1___SWifpeeL - ..................... - J -,J2oJ10 . S~.___ lays *>_.Xrvx t s______ ,,5^5i?.n________ ___ Ot^v C^>Ow Vcv', __ \iov___ ^y_e, slavtc. - ^*"7 g. ~lamF ("2AH ^sioT^_ ,__vAAolec-i-4.lov' LM,~L fla/Jb"U*olfc> ... .^yOficlAd____6>v^^>ju_ ~ Qt t'V7_________ ______________ /- OO (jl l Su^e. ~ mnpi(OL ________ ^* ixy"_l--------- /*?!! . Bqc^ Vgflr -------------- De^*;+u -. y. . ^ _______ c^aL 1 :1 7.0 ?20t 5 te* I ZOooil> \ Mai!- 1 L*f . 7Z4 IST.t -Pv-3. Mv ( t*~ 1 7. *n it i 7/WoJL -- 'S'r (S*_JLcadiv^ SS^./t'5 *20 yri^_frJ70*/^ J4X7---20. M S*3c: 1 H^Z- A 7 2-4/3Z.Cpft3. - .4*- yt---( . ^4.53. lb | ^ -- T'l.C.-Jffc' Ife 1- 2Zooit SL 026037 Tfttt _ C "n/ncvi Pwpa ~i or ~ ii Y-ggr~ - -T-a^K . .fvuAiJiS______ A^ ; ______ "! XV*<cJs* V ,K*w^^L (ex>.____ - uHOooQ.1J1_b_WeLs<-. a _^CAoevoQ -> ^ ^ A) pov is . ^3 _ Coiuvc*_W^. _. ~ T ov\V; *fv%A.ols oo 1 u.w^,___ /^j ooo fiovl o^&s pv"ets*>* ec =.-S-.^ .pi{A Xm.h, ^v*p*v ~--gt, 1" ta'Acts /oooo4a( ft* _l , 452-1 ------- * . * *-----------P ] 3 /HH 1 S'JO - ._C-T - S H. 4% .. <U.--t 0^o\ _ C^5uv/'<g o4~ s F-12 r~ t -3 APPENDIX F-B SHIPPING AND LOADING UNIT FUGITIVE EMISSIONS CALCULATIONS SL 026040 5510H01B.01A F-14 Final 05/27/92 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS hap: i.s-Pichlarpetaigne Year: 1987____________ Loading Operation: Drums Date: April 1992 Calculator: D. Seifert Loading Parameters Cargo carrier (tank truck, rail car, etc.) Mode of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) Temperature of liquid loaded (F) Weight percent HAP in the loaded material True vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Molecular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor Drum______________________ submerged: clean 2-l3U1M IL.& 1 p M S cpptrpl Control device HAP control efficiency (%) None Q.o eff calculation* Uncontrolled Loading Loss Ej, = (5.65E-06) s P M G Uncontrolled Loading Loss E0 - T + 460 (5.65E-06) (0.5) (1.32) (70) + 460 (99) (2677) 0.002 Mg/yr HAP Emissions (E^p) * E,, (1 - eff/100) = 0.002 (1 - 0/100) 0.002 Mg/yr SL 026041 F-15 Sourc : Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS (CONCLUDED) calculation (sonfrinuefl) Weighted HAP Emissions = E^p FHR *= (0.002) (1) 0.002 Mg/yr `Calculation worksheet and procedure from ''Procedures for Establishing Base Year and Post-reduction HAP Emissions." consistent with AP-42. This procedure is Si 026042 F-16 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: Methylene Chloride Year: 1987____________________ Loading Operation: Drums Date: April 1992_------------ Calculator: D. Seifert. Loading Parameters Cargo carrier (tank truck, rail car, etc.) Mod of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) T mperature of liquid loaded (F) W ight percent HAP in the loaded material Tru vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Mol cular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor Drum_____________________ submerged: clean 1_29. 100 7.74 84.9 0^ X G T P M S control Control device HAP control efficiency (%) None 0.0 eff Calculation* Uncontrolled Loading Loss E0 * (5.65E-06) S P M G T + 460 Uncontrolled Loading Loss Eu = (5.65E-06) f0.6^ (7.741 (84.91 (70) + 460 (1629^ 0.007 Mg/yr HAP Emissions (Eu&p) *= Eq (1 - eff/100) * 0.007 (1 - 0/100) 0.007 Mg/yr F-17 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS (CONCLUDED) Calculation (continued) Weighted HAP Emissions = EHAP HR (0.007) (1) "Calculation worksheet and procedure from "Procedures for Establishing Base Year and Post-reduction HAP Emissions." consistent with AP-42. This procedure is 0260^4 SL F-18 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: Tefrragfolgxgetfrylepe___________ Year: 1987_________________________________ Date: April 1992 Calculator: D. Seifert Loading Operation: Drums_______________________________________________________________ Cargo carrier (tank truck, rail car, etc.) Mod of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) T mperature of liquid loaded (F) Weight percent HAP in the loaded material True vapor pressure of the HAP loaded (psia) (Note: For mixtures, use the HAP partial pressure] Mol cular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor Clil_______________ sqbmacqedj,.clean _____l-Ou.556 IQ IQO ___________ P.L. 165^5 - __ UP-- Qpntrol Control device HAP control efficiency (%) None 0.0 G T P M S FHR ff Calculation Uncontrolled Loading Loss Eg = (5.65E-06) s P M G T + 460 Uncontrolled Loading Loss E,, = (5.65E-06) (0.5) (0.27)(165.85) (10556) (70) + 460 0.003 Mg/yr HAP Emissions (E^p) - Ej, (1 - eff/100) = 0.003 (1 - 0/100) 0.003 Mg/yr SL 026045 F-19 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS (CONCLUDED) Calculation (continued! Weighted HAP Emissions = EHAP HR = (0.003) (1) Calculation worksheet and procedure from "Procedures for Establishing Base Year and Post-reduction HAP Emissions." consistent with AP-42. This procedure is SL 026046 F-20 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: Trich 1 oroethv 1 ene______________ Year: 1987 _________________________ Date: April 1992 Calculator: D. Seifert Loading Operation: Drums______________________________________________________ lading Earaagt^rs Cargo carrier (tank truck, rail car, etc.) Mode of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) T mperature of liquid loaded (F) W ight percent HAP in the loaded material Tru vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Mol cular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor Drum submerged: clean 58,763 70 100 1.45 131.4 0,5 1 =G sT sP M --S fhr .Control Control device HAP control efficiency (%) None _____________ 0-.0 = eff a^ulaioQa Uncontrolled Loading Loss Eg = (5.65E-06) s P M G Uncontrolled Loading Loss Eg T + 460 (5.65E-06) (0.51(1.451(131.41(587631 (70) + 460 0.06 Mg/yr HAP Emissions CE^p) Ew (1 - eff/100) 0.06 (1 - 0/100) 0.06 Mg/yr SL 26047 F-21 Sourc : Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS ______________FROM LOADING OPERATIONS (CONCLUDED) Calculation (continued) Weighted HAP Emissions =E "Calculation worksheet and procedure from "Procedures for Establishing Bas Year and Post-reduction HAP Emissions." consistent with AP-42. This procedure is SL 026048 F-22 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: 1.1. l-Trichlo_roethane Year: 1987_________________________________ Date: April 1992 Calculator: D. Seifert Loading Operation: Drums_______________________________________________________________ Loading Parameters Cargo carrier (tank truck, rail car, etc.) Mode of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) Temperature of liquid loaded (F) Weight percent HAP in the loaded material True vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Molecular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor Dm________________ submerged;.normal 237.734.7 IQ 1QQ __________3-02 . 1,33._U? ___ 0+5-- l G T P control Control device HAP control efficiency (%) Mi CUQ eff calcgia&iQn* Uncontrolled Loading Loss Ey = (5.65E-06) S P M G Uncontrolled Loading Loss T + 460 5.65E-061 ro.5) f 2.02 W133.415) f237734.7) (70) + 460 .34 Mg/yr HAP Emissions (Ej^) = Ey (l - eff/100) = .34 (1 - 0/100) .34 Mg/yr SL 026049 F-23 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS _______________FROM LOADING OPERATIONS (CONCLUDED) Calculation (continued) Weighted HAP Emissions " ehap = (.34) r HR (1) 0.34 Mg/yr "Calculation worksheet and procedure from "Procedures for Establishing Base Year and Post-reduction HAP Emissions." consistent with AP-42. This procedure is 026050 SL F-24 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: Methylene Chloride_____________ Y ar: 1987________________________________ Date: April 1992 Calculator: D, Seifert Loading Operation: Tank Trucks___________________________________________________ Lpaainq-paraTneters Cargo carrier (tank truck, rail car, etc.) Mode of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) Temperature of liquid loaded (F) Weight percent HAP in the loaded material Tru vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Mol cular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor TaoK T.ruQKs submerged:dedicated normal 145J=?10_______________ = G 70_______________ = T . _ 10,0_______________ ______ Z 2.4 . = P - S4.9 ______ CLJi ,, =M =s _____________1_____________ = F, Control Control device HAP control efficiency (%) _______________None _______________q.q = eff Calculation* Uncontrolled Loading Loss Eg = (5.65E-06) s P m g T + 460 Uncontrolled Loading Loss Eg (5.65E-06) (0.6W7.74W84.9) (70) + 460 fi458ioi 0.61 Mg/yr HAP Emissions (Ej^p) * Ew (1 - eff/100) * 0.002 (1 - 0/100) 0.61 Mg/yr SL 026051 F-25 source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS (CONCLUDED) Calculation (continued! Weighted HAP Emissions = E, Calculation worksheet and procedure from "Procedures for Establishing Base Year and Post-reduction HAP Emissions." consistent with AP-42. This procedure is F-26 SL Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: Y ar: g-PichlOEgeth^ne____________ 1987________________________________ Date: April 1992 Calculator: D. Seifert Loading Operation: Tank Truck_____________________________________________________ Laatoq-EflEame&gra Cargo carrier (tank truck, rail car, etc.) Mod of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) Temperature of liquid loaded (F) Weight percent HAP in the loaded material Tru vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Mol cular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor Pram gqbroeEaedJiftedlcated normal . 2.06 J? 8 3 = G _________ 70 a T 100 1.32 22_____________ = M 0.6___________ = S -1------------------- = *Hr SpnfrrQl Control device HAP control efficiency (%) None_________ o.Q___________ = eff Calculation* Uncontrolled Loading Loss E,, * (5.65E-06) S P M G T + 460 Uncontrolled Loading Loss E*, - (5.65E-06) (0.6) (1.32) f99) (70) + 460 (706883) =P 0.59 Mg/yr HAP Emissions (E^p) = E0 (1 - eff/100) = 0.002 (1 - 0/100) 0.59 Mg/yr O^60^ F-27 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS (CONCLUDED) Caiffiala&i-on .(continue) Weighted HAP Emissions " ehap "Calculation worksheet and procedure from "Procedures for Establishing Base Year and Post-reduction HAP Emissions." consistent with AP-42. This procedure is SL 02605* F-28 Sourc : Shipping: and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: Tetr.achlPr<ag.thYlene___________ Year: 1987~________________________________ Date: .April 1992 Calculator: D. Seifert Loading Operation: Tank Trucks____________________________________________________ Loading Parameters Cargo carrier (tank truck, rail car, etc.) Mod of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) Temperature of liquid loaded (F) Weight percent HAP in the loaded material Tru vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Mol cular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor TanK-IrusK PMfepeEgedj_&edjcat.ed normal 618.706______________ = G 70 = IM_________________ 0.27 -Q.. 6_. -i HR copbrgl Control device HAP control efficiency (%) ______________None _______________o.o = eff Calculation* Uncontrolled Loading Loss Ej, * (5.65E-06) Uncontrolled Loading Loss E0 =(5.65E-06) s PMG T + 460 ro.6)(0.271(165.851(6187061 (70) + 460 T =P 0.18 Mg/yr HAP Emissions (E^p) * E0 (1 - eff/100) = 0.18 (1 - 0/100) 0.18 Mg/yr SL 026055 F-29 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS ______________________________FROM LOADING OPERATIONS (CONCLUDED) Calculation (continued) Weighted HAP Emissions " ehap - (0.18) fhr (1) 0.18 Mg/yr "Calculation worksheet and procedure from "Procedures for Establishing Base Year and Post-reduction HAP Emissions." consistent with AP-42. This procedure is 026056 SL F-30 Source: Shipping _and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: Trichloroethylene______________ Year: 1987_________________________________ Date: _ April 1992 Calculator: D. Seifert Loading Operation: Tank Trucks___________________________________________________ Loading Parameters cargo carrier (tank truck, rail car, etc.) Mode of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) Temperature of liquid loaded (F) Weight percent HAP in the loaded material True vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Molecular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor laafe.Trask submerged;dedicated normal 796.673 70 5= = 100 1.45 . = 131.4 0.6 1 = = control Control device HAP control efficiency (%) Hone_______ 0.0___________ * eff Uncontrolled Loading Loss Eu *= (5.65E-06) Uncontrolled Loading Loss Ey =(5.65E-06) S PMG T + 460 f0.6)(1.451(131.41(7966731 (70) + 460 0.97 Mg/yr HAP Emissions (E^p) * E,, (1 - eff/100) - 0.97 (1 - 0/100) 0.97 Mg/yr SL 026057 F-31 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS __________FROM LOADING OPERATIONS (CONCLUDED) Calculation (continued) Weighted HAP Emissions = E, Calculation worksheet and procedure from "Procedures for Establishing Bas Year and Post-reduction HAP Emissions." consistent with AP-42. This procedure is SL 026058 F-32 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: 1.1.1-Trichloroethane Y ar: 1387_________________________________ Date: April 1992 Calculator: D. Seifert Loading Operation: Tank Truck_____________________________________________________ Loading Parameters Cargo carrier (tank truck, rail car, etc.) Mode of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) Temperature of liquid loaded (F) Weight percent HAP in the loaded material True vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Molecular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor Tank Truck submerged:dedicated normal 1.872.179.9 70 = s 100 2.02 = 133.415 0.6 1 = Qantrgi Control device HAP control efficiency (%) Napeo.o___________ = eff gais,Mlat;ipna Uncontrolled Loading Loss E0 - (5.65E-06) S P M G Uncontrolled Loading Loss Ey = T + 460 (5.65E-06) LSL, 6L(2.02) (133.4151 (1872179.9) (70) + 460 3.23 Mg/yr HAP Emissions (Ejj^p) E0 (1 - eff/100) 3.23 (1 - 0/100) 3.23 Mg/yr SL 026059 F-33 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS (CONCLUDED) Calculation (continued! Weighted HAP Emissions * Emp fhr s 3.23 Mg/yr Calculation worksheet and procedure from "Procedures for Establishing Bas Year and Post-reduction HAP Emissions." consistent with AP-42. This procedur is 026060 5L F-34 Sourc : Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: L,3-J>ighlQE<?S&tame____________ Year: 1987_________________________________ Date: April 1992 Calculator: D. Seifert Loading Operation: Tank Cars_______________________________________________________ Loading Parameters Cargo carrier (tank truck, rail car, etc.) Mode of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) Temperature of liquid loaded (F) Weight percent HAP in the loaded material True vapor pressure of the HAP loaded (psia) (Note: For mixtures, use the HAP partial pressure] Molecular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor TsaafnrJkjgCrgaSrd-LdedjcaSefl normal l-87._686____________ = G 70 ___________ T IPO_______________ ___________L,32 ... , = P _________92_______________ = M _________ Qj_6_________ = S ggnfcJTQl Control device HAP control efficiency (%) None 0.0___________ = eff gfllghlatipn* Uncontrolled Loading Loss Eg * Uncontrolled Loading Loss Eg = (5.65E-06) (5.65E-06) s PMG T + 460 fo.6^ n.321 (991 (1876861 (70) + 460 0.16 Mg/yr HAP Emissions (E^) = E0 (l - eff/100) - 0.16 (1 - 0/100) 0.16 Mg/yr SL 026061 F-35 Sourc : Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS (CONCLUDED) Calculation (continued! Weighted HAP Emissions =E Calculation worksheet and procedure from "Procedures for Establishing Base Year and Post-reduction HAP Emissions." consistent with AP-42. This procedure is SL 026062 F-36 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: Te,fcragMPJ.pethVl.ene___________ Year: 1987_________________________________ Date: April 1992 Calculator: D. Seifert Loading Operation: Tank Cars_______________________________________________________ Loading Parameters Cargo carrier (tank truck, rail car, etc.) Mod of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) T mperature of liquid loaded (F) Weight percent HAP in the loaded material True vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Mol cular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor Tanjc oar submerq&d;ggdisated normal UILJ44 = G 70 = T 100 Q-i-2.7_____________ 1.65.85 0.6 1 CqnfrrQl Control device HAP control efficiency (%) None_________ 0.0___________ = ff Calculation* Uncontrolled Loading Loss E0 = (5.65E-06) S P M G T + 460 Uncontrolled Loading Loss E0 - (5.65E-06) (0.61(0.271(165.851(1170441 ___________________________ (70) + 460 0.61 Mg/yr =P HAP Emissions (E^^p) Eu (1 - eff/100) 0.61- 0/100) 0.61 Mg/yr SL 026063 F-37 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS ________________FROM LOADING OPERATIONS (CONCLUDED) Calculation (continued^ Weighted HAP Emissions "Calculation worksheet and procedure from "Procedures for Establishing Base Year and Post-reduction HAP Emissions." consistent with AP-42. This procedure is 02606* F-38 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: Trichloroethylene______________ Year: 1987________________________________ Date: April 1992 Calculator: D. Seifert Loading Operation: Tank Cars_____________________________________________________ Loading Parameters Cargo carrier (tank truck, rail car, etc.) Mode of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) Temperature of liquid loaded (F) Weight percent HAP in the loaded material True vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Molecular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor Tank Car submerged .-dedicated normal 1.683.653 = G 70 = T 10Q 1.45 121x4___________ - M 0.6___________ = S -Ifi---------------------- = Fhr Control Control device HAP control efficiency (%) _______________None _______________o.o = eff Calculation* Uncontrolled Loading Loss Ew * (5.65E-06) Uncontrolled Loading Loss E0 - (5.65E-06) s Pmg T + 460 fo.61fi-45)fi3i.4)ri683653l (70) + 460 -P 2.05 Mg/yr HAP Emissions (E^p) = E0 (1 - eff/100) * 2.05 (1 - 0/100) 2.05 Mg/yr SL 026065 F-39 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS _____________FROM LOADING OPERATIONS (CONCLUDED) Calculation (continued) Weighted HAP Emissions = E,HAP = (2.05) HR (1) 2.05 Mg/yr Calculation worksheet and procedure from "Procedures for Establishing Base Year and Post--reduction HAP Emissions." consistent with AP-42. This procedure is 02&066 SL F-40 sourc : shiPEi.nq.and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: 1,1, l-TEichlffr<aethflne_______ Year: 1987_________________________________ Date: April 1992 calculator: D. Seifert Loading Operation: Tank Cars_______________________________________________________ Loading Parameters Cargo carrier (tank truck, rail car, etc.) Mode of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) Temperature of liquid loaded (F) Weight percent HAP in the loaded material True vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pr ssure] Molecular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor Bail Tank. submerged;dedicated normal 3.520.965,6 20 =G *T 100 2.02 =P _ 133.415 0,6 1 .-M =S - = fhr control Control device HAP control efficiency (%) None 0.0 ________ = eff Calculation* Uncontrolled Loading Loss Eg = (5.65E-06) s P M G Uncontrolled Loading Loss Eg = T + 460 (5.65E-06) XQ_j_6) L2.02.) (133.415) (3520965.61 (70) + 460 6.07 Mg/yr HAP Emissions (E^p) * E0 (1 - eff/100) * 6.07 (1 - 0/100) 6.07 Mg/yr SL 026067 F-41 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS (CONCLUDED) Calculation fcontinued^ Weighted HAP Emissions ^HAP = (6.07) rHR (l) 6.07 Mg/yr Calculation worksheet and procedure from "Procedures for Establishing Base Year and Post-reduction HAP Emissions." consistent with AP-42. This procedure is Oi'-06 F-42 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: 1.2-Dich1 oroethane_____________ Year: 1987_________________________________ Date: April 1992 Calculator: D. Seifert Loading Operation: Barges_____________________________________________________________ Loading,, Paraffafeecs Cargo carrier (tank truck, rail car, etc.) Mode of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) Temperature of liquid loaded (F) Weight percent HAP in the loaded material True vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Mol cular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor Barge submerged_____ 12.219.254 70 ISO 1,32 99 0.5 1 sG sT =p M S s FHR CgntaP.1 Control device HAP control efficiency (%) None ___________ Pi-Q- = eff QalcylafciQn* Uncontrolled Loading Loss Ey * (5.65E-06) Uncontrolled Loading Loss Eu * (5.65E-06) s PMg T + 460 ro.51 (1.321(99)(12.219.254^ (70) + 460 8.5 Mg/yr HAP Emissions (Eo>p) = Eg (1 - eff/100) 8.5 (1 - 0/100) 8.5 Mg/yr SL 26069 F-43 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS ________________FROM LOADING OPERATIONS (CONCLUDED) Calculation (continued! Weighted HAP Emissions ~ ehap = (8.5) 8.5 Mg/yr rHR (1) Calculation worksheet and procedure from ''Procedures for Establishing Bas Year and Post-reduction HAP Emissions." This procedure is consistent with AP-42. SL 026070 F-44 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: Tetrachloroethvlene___________ Year: 1987_________________________________ Date: April 1992 Calculator: D. Seifert Loading Operation: Barges______________________________________________________ Loading Parameters Cargo carrier (tank truck, rail car, etc.) Mode of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) Temperature of liquid loaded (F) Weight percent HAP in the loaded material True vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Molecular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor Barge submerged_____ 2.125.293 _____________70__________ 100 0.2 165.85 0.5 _______________1___________ mm G =T sP as = a Control Control device HAP control efficiency (%) None 0.0 = eff Calculation* Uncontrolled Loading Loss Ew * (5.65E-06) s P M G T + 460 Uncontrolled Loading Loss Ew = (5.65E-06) f0.5)(0.271f!65.85)(21252931 (70) + 460 0.51 Mg/yr HAP Emissions (E^) - Ew (1 - eff/100) =* 0.51 (1 - 0/100) 0.51 Mg/yr SL 026071 F-45 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS (CONCLUDED) Calculation (continued) Weighted HAP Emissions =E "Calculation worksheet and procedure from "Procedures for Establishing Base Year and Post-reduction HAP Emissions." consistent with AP-42. This procedure is 02t>72 F-46 Sourc : gripping, and leading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: Trichloroethylene______________ Year: 1987_________________________________ Date: April 1992 Calculator: D. Seifert Loading Operation: Barges_____________________________________________________________ Loading Parameters Cargo carrier (tank truck, rail car, etc.) Mode of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) Temperature of liquid loaded (F) Weight percent HAP in the loaded material True vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Molecular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor Barae submerged 583.519 70 100 1.45 131.4 0,5 1 tst G sT =P M =S ss fhr CaptCgi Control device HAP control efficiency (%) None _______________P-lIL -- = eff Calculation Uncontrolled Loading Loss Ew = Uncontrolled Loading Loss Eu (5.65E-06) (5.65E-06) S PMG T + 460 fo.5)(1.451(131.4)(5835191 (70) + 460 0.59 Mg/yr HAP Emissions (E^) = E0 (1 - eff/100) - 0.59 (1 - 0/100) 0.59 Mg/yr SL 026073 F-47 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS ________________FROM LOADING OPERATIONS (CONCLUDED) Calculation (continued) Weighted HAP Emissions =E "Calculation worksheet and procedure from "Procedures for Establishing Base Year and Post-reduction HAP Emissions." consistent with AP-42. This procedure is 02601'' SL F-48 Sourc : Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: 1.1.1-Trichloroethane Year: 1987________________________________ Date: April 1992 Calculator: D. Seifert Loading Operation: Barges_____________________________________________________________ Loading Parameters Cargo carrier (tank truck, rail car, etc.) Mode of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) Temperature of liquid loaded (F) Weight percent HAP in the loaded material True vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Molecular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor fiargas submerged: loading 3 , 37,-367,7, _ =G 242 = 100 _____________________ =P U3-.A15 - Qs.5 ____1_______ =M *S = F,HR Cfiptcpl Control device HAP control efficiency (%) None 0.0___________ = eff .Calculation* Uncontrolled Loading Loss Eg = (5.65E-06) S P m g Uncontrolled Loading Loss E^j = T + 460 (5.65E-06)(0.5)(2.02)(133.415)(2897367.7) (70) + 460 t 4.16 Mg/yr HAP Emissions (E^) = E0 (1 - eff/100) - 4.16 (1 - 0/100) 4.16 Mg/yr SL 026075 F-49 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS (CONCLUDED)________________ Calculation (continued) Weighted HAP Emissions = Ej^p FHR = (4.16) (l) 4.16 Mg/yr "Calculation worksheet and procedure from "Procedures for Establishing Bas Year and Post-reduction HAP Emissions." consistent with AP-42. This procedure is SL 026076 F-50 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: 1, Z-Pichloroettone____________ Year: 19B7_________________________________ Date: April 1992 Calculator: D. Seifert Loading Operation: Ships___________________________________________________________ Loading Parameters Cargo carrier (tank truck, rail car, etc.) Mode of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) Temperature of liquid loaded (F) Weight percent HAP in the loaded material True vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Mol cular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor ship submeraed 1.777.361 70 100 1.32 99 0.2 1 SG =T =P M as S = Control Control device HAP control efficiency (%) None _______________S.,0-- = eff Calculation* Uncontrolled Loading Loss Ey = Uncontrolled Loading Loss Ey * (5.65E-06) (5.65E-06) s PMG T + 460 f0.2l (1.32) f99^ (70) + 460 (1777361) 0.50 Mg/yr HAP Emissions (BHAP) Eu (1 - eff/100) 0.50 (1 - 0/100) 0.50 Mg/yr SL 026077 F-51 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS _______________FROM LOADING OPERATIONS (CONCLUDED) Calculation (continued! Weighted HAP Emissions = E, Calculation worksheet and procedure from "Procedures for Establishing Base Year and Post-reduction HAP Emissions." consistent with AP-42. This procedure is SL 026078 F-52 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: Tetrachloroethvlene___________ Year: 1987 ___________________ Date: --April --------------- Calculator: D. Seifert Loading operation: Shins______________________________________________________________ Loading Parameters Cargo carrier (tank truck/ rail car, etc.) Mode of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) Temperature of liquid loaded (F) Weight percent HAP in the loaded material True vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Molecular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor submerged______ 1.994.353 ... _____________20___________ 100 0,27 165.85 0.2 _______________1___________ sG ss T -P = cpnfrrol Control device HAP control efficiency (%) None______________________ 0.0 = eff Calculation* Uncontrolled Loading Loss Eg * (5.65E-06) S P M G T + 460 Uncontrolled Loading Loss E0 = (5.65E-06) fo.2)ro.27)(165.85)(1994353) (70) + 460 0.19 Mg/yr HAP Emissions (.) * Eg (1 - eff/100) - 0.19 (1 - 0/100) 0.19 Mg/yr SL 026079 F--53 Sourc : Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS (CONCLUDED) Calculation (continued) Weighted HAP Emissions - E; `Calculation worksheet and procedure from "Procedures for Establishing Base Year and Post-reduction HAP Emissions." consistent with AP-42. This procedure is SL 026080 F-54 Sourc : ShipBiaq-apd .Lading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: Trichloroethylene______________ Y ar: 198?_________________________________ Date: ___ApfU -19-3.3-------------- Calculator: D. Seifert Loading Operation: Ships_______________________________________________________________ Lpaflipct.Pftrafflefcerg Cargo carrier (tank truck, rail car, etc.) Mod of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) Temperature of liquid loaded (F) W ight percent HAP in the loaded material Tru vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Molecular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor Skips submerged 1.328.619 70 1_Q0 _ _ 1.45 ,, 131.4 _ 0.2 _______________1___________ -- = = = K HR g-anr.al Control device HAP control efficiency (%) None _______________- == eff alul&ispa Uncontrolled Loading Loss Eg = (5.65E-06) Uncontrolled Loading Loss Ey * (5.65E-06) s PMG T + 460 fo.21 (1.451(131.4)(1328619) (70) + 460 0.54 Mg/yr HAP Emissions (Erp) "Eg (1 - eff/100) - 0.54 (1 - 0/100) 0.54 Mg/yr SL 026081 F-55 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS _______________FROM LOADING OPERATIONS (CONCLUDED) Calculation (continued) Weighted HAP Emissions ~ ehap = (0.54) fhr (l) Calculation worksheet and procedure from "Procedures for Establishing Bas Year and Post-reduction HAP Emissions." consistent with AP-42. This procedur is 026082 SL F-56 source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS HAP: 1.1.1-Trichloroethane Year: 1982_________________________________ Date: ___April lg.92-------------- Calculator: D. Seifert Loading Operation: Ships_______________________________________________________________ Loading Parameters Cargo carrier (tank truck, rail car, etc.) Mode of operation (choose from Table 2-16) Annual volume of liquid loaded (gallons) Temperature of liquid loaded (F) Weight percent HAP in the loaded material True vapor pressure of the HAP loaded (psia) [Note: For mixtures, use the HAP partial pressure] Molecular weight of the HAP (lb/lb-mole) Saturation factor (see Table 2-16) HAP high-risk weighting factor ship pmamerqedjoking .......... 70 < IQS 2.02 - UlsAlS. . fit? _ ____1_______ G T P cpntrol Control device HAP control efficiency (%) _______________None _______________q.q = eff Calculation* Uncontrolled Loading Loss Ey * (5.65E-06) s P M G Uncontrolled Loading Loss Ew * T + 460 (5.65E-06) (0.2)(2.021(133.415)(6297957. 21 (70) + 460 3.62 Mg/yr HAP Emissions (E^) 02683 sl 0iuu Ejj (1 - eff/100) 3.62 (1 - 0/100) 3.62 Mg/yr F-57 Source: Shipping and Loading CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM LOADING OPERATIONS (CONCLUDED) Calculation fcontinued! Weighted HAP Emissions " ehap (3.62) `Calculation worksheet and procedure from "Procedures for Establishing Base Year and Post-reduction HAP Emissions." consistent with AP-42. This procedure is 26084 F-58 APPENDIX G TRI-ETHANE* II PROCESS UNIT (TE-II) SL 026085 5510R016.01 Final 05/27/92 APPENDIX G TRI-ETHANE* II PROCESS UNIT (TE-II) G.l Process Description Tri-Ethane* production involves the following: Vinyl chloride Section (VC); 1,1 -Dichloroethane Section (DCE); Methyl chloroform Section (MC); and Oxyhydrochlorination EDC Unit. Methyl chloroform (MC) Is manufactured In the Tri-Ethane* II (TE-II) Unit in three reaction steps. The process begins by cracking ethylene dichloride (EDC) to vinyl chloride (VC) and hydrogen chloride (HCI). VQ and HCI are then recombined to form 1,1-dichloroethane (DCE) which in turn is chlorinated as the final step to form MC and HCI. The TE-II Unit also includes an OHC-EDC section (OHC-II) which converts by-product HCI and ethylene into EDC. Figure G-1 outlines the major production steps that occur in the Tri-Ethane* unit. VQ Section In the VC section, vinyl chloride and HCI are produced as co-products by thermally cracking 1,2EDC at high temperatures in a direct fired natural draft furnace. The chemical reaction occurs as follows: Ethylene Dichloride -- Heat (C2H4Cy Vinyl Chloride (C2H3CI) + Hydrogen Chloride (HCI) Figure G-2 shows the major equipment used in VC section. VC is used as a raw material in the 1,1-DCE section, and is transferred to VCM-II for further processing into VCM product. 5510R016.01A G-1 Final 05/27/92 SL 026086 Figure G-1: Tri-Ethane* II Process Schematic See Volume II Confidential ENSR 5510R016.01A SL 026087 G-2 Final 05/27/92 Figure G-2: TE-II VCM Section See Volume II - Confidential S510R018.01A SL 026088 G-3 Final 05/27/92 P.CE .Section This process uses VC and HCI from the VC section to form 1,1-dichloroethane (DCE). The reaction is catalyzed in a liquid bed reactor. The general chemical reaction for DCE is: Vinyl Chloride + (C2H3CI) Hydrogen -------------------- 1,1-Dichloroethane Chloride Catalyst (HCI) (c2H4cy Figure G-3 shows the major equipment and location of air emissions from the TE-II DCE section. Methvl Chloroform (MCI Section The final chemical reaction step in methyl chloroform production is: 1,1 -Dichloroethane + Chlorine (CVW (Cl2) Methylchioroform + Hydrogen Chloride (CjHjCy (HCI) Figure G-4 shows the major equipment used in the production of MC products from the TE-II unit. Liquid chlorine from Plant A is vaporized and fed to the MC reactor along with liquid DCE. HCI vapor exits the top of the reactor and flows to an absorber system for removal of contaminating organics. This purified HCI is sent to the high pressure HCI system for use in the OHC section. MC, by-products, and unreacted DCE are drawn off the reactor and fed to the DCE Recycle Still. This column separates DCE from the remainder of the mixture. DCE is recycled back to the reactor while MC and other organics are fed to the Product Still. This still separates MC from the heavier by-products. The heavy material is cooled and stored prior to being transferred to the VDCM and Per/Tri units. Pure MC is neutralized to remove HCI and then moved to stabilizing tanks where chemicals are added to make the desired grade of Tri-Ethane* solvent. From here the finished product is pumped to Day Tanks, or Shipping Tanks to await shipment by drum, truck, railcar, barge or ship. S510fl016.01A SL 026089 G-4 Final 05/27/92 Figure G-3: TE-II 1,1-Dichloroethane Section (DCE) See Volume II - Confidential 551(M010.01A SL 026090 G-5 Final 05/27/92 Figure G-4: TE-II Methyl Chloroform (MC) Section See Volume II - Confidential SL 2609j S510H016.01A G*6 Final 05/27/92 Oxvhvdrochlorination (OHC1 -EDC Section EDC is produced in a vapor phase reaction of MCI and Ethylene in the presence of a catalyst. This process is known as oxyhydrochlorination. The chemical reaction is as follows: Ethylene + 2HCI + V402 EDC + Catalyst (CW (C2H4CIj) H20 Figure G-5 shows a flow diagram of the OHC-EDC production process. The OHC-EDC section of TE-II is an independent process capable of running while TE-II is down. Likewise TE-II can operate without OHC-II because EDC can be obtained from other units (EDC, VCM-II). HCI generated by the MC section is discharged into the HCI distribution system. Figure G-6 outlines the major steps and equipment used in OHC-EDC production. In the OHC-EDC section, EDC is made by the oxyhydrochlorination process. Oxygen, hydrogen chloride, and ethylene are fed to a fluid bed reactor and form EDC and water. A small purge from the condenser is removed and incinerated to eliminate impurities. Following condensation, the EDC and water are phase separated. The EDC is chemically purified, dried and furth r processed in a lights still. This still removes light impurities, which are sent to the Per/Tri Unit. EDC is drawn from the bottom of the lights still and stored. Use of OHC-EDC is limited to internal usage since the EDC is not pure enough for shipment. G.2 1987 Base-Year Emissions Table G-1 shows the total base-year emissions for the TE-II process unit. The total unweighted HAP emissions were 46.266 Mg/yr. Emissions from storage tank EIQ 353 required using weighting factors. The total base-year weighted HAP emissions for the TE-II unit were 48.187 Mg/yr. 5510R016.01A G-7 Final 05/27/92 Figure G-6: TE-II OHC Section (EDC Production) See Volume II - Confidential SL 026094 5510R016.01A G-9 Rnal 05/27/92 SL 026095 TABLE G-t 1987 BASE YEAR EMISSIONS TRIETHANE PROCESS UNIT (TE-II) BASE YEAR UNIT EIQ TE-II 305 TE-II 306 TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II 310 315 316 317 318 319 320 321 322 323 324 325 326 353 355 358 DESCRIPTION MC/DCE Startup Scrubber No.2 OHC Startup Scrubber DCE Tank Vents EDC Crude and Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Dock Storage TE Shipping Tank TCE/Tetra Tank No.1 BLM Storage Tank TBl/MC Tank TYPE P P T T T T T T T T T T T T T T T T CONTROL DEVICE HAP EMISSIONS TYPE % UNWEIGHTED WEIGHTED CONTROL* MG/YR MG/YR Scrubber 5.00 3.004 3.004 Scrubber 5.00 3.935 3.935 Subtotal Process Vents 6.939 6.939 Ref. Cond 88.10 6.045 6.045 Ref. Cond. 68.00 4.065 4.065 None 0.00 0.298 0.298 None 0.00 0.759 0.759 None 0.00 0.759 0.759 None 0.00 3.042 3.042 None 0.00 3.038 3.038 None 0.00 0.913 0.913 None 0.00 1.941 1.941 None 0.00 2.062 2.062 Ref. Cond. 84.00 7.113 7.113 Ref. Cond. 88.40 4.748 4.748 None 0.00 2.610 2.610 Scrubber 5.00 1.529 3.450 None 0.00 0.097 0.097 None 0.00 0.288 0.288 Subtotal Tank Vents 39.3273 41.2483 1 * Control afflciancfaa lor acrubbarc tapraaant afficlanciaa far hyckooarbona. Ihaaa acrubbara bava 99% afffciancy far HCI. Total Base Year Emissions 46.266 48.187 FILE: TEBASE G-3 Emissions Reduction Strategy Table G-2 shows the control strategy for the TE-II unit that will be implemented to help achieve a plantwide reduction in emissions for ail SOCMI sources at the facility. The general control strategy is as follows: Emissions from ten storage tanks, EIQ 316 through EIQ 323, EIQ 326, and EIQ 358 will be incinerated. With the inclusion of these controls, the total overall control level for the TE-ll unit is estimated to be equal to or greater than 34.00% for unweighted HAPs and 32.64% for weighted HAPs. G-4 Post-Reduction Emissions Table G-3 shows the total unweighted and weighted HAP emissions for the TE-ll process unit. The total post-reduction unweighted emissions of 30.5 Mg/yr represent a 15.7 Mg/yr decrease (34.00% reduction) in unweighted HAP base-year emissions. The total post-reduction weighted emissions of 32.5 Mg/yr represent a 15.7 Mg/yr decrease (32.64% reduction) in weighted HAP base-year emissions. s5ionoie.oiA 02&096 Sl G-11 Final 05/27/92 026097 TABLE G-2 EMISSIONS REDUCTIONS STRATEGY AND POST REDUCTION EMISSIONS TRIETHANE PROCESS UNIT (TE-II) POST REDUCTION UNIT EIQ TE-II 305 TE-II 306 TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II TE-II 310 315 316 317 318 319 320 321 322 323 324 325 326 353 355 358 DESCRIPTION MC/DCE Startup Scrubber No.2 OHC Startup Scrubber DCE Tank Vents EDC Crude and Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Process Storage MC Dock Storage TE Shipping Tank TCE/Tetra Tank No. 1 BLM Storage Tank TBL/MC Tank TYPE P P T T T T T T T T T T T T T T T T HAP EMISSIONS ADDITIONAL CONTROL 1994 UNWEIGHTED WEIGHTED % CONTROL* MG/YR MG/YR None 5.00 3.004 3.004 None 5.00 3.935 3.935 Subtotal Process Vents 6.939 6.939 None 88.10 6.045 6.045 None 88.00 4.065 4.065 Incinerator 99.99 0.000 0.000 Incinerator 99.99 0.000 0.000 Incinerator 99.99 0.000 0.000 Incinerator 99.99 0.000 0.000 Incinerator 99.99 0.000 0.000 Incinerator 99.99 0.000 0.000 Incinerator 99.99 0.000 0.000 Incinerator 99.99 0.000 0.000 None 64.00 7.113 7.113 None 88.40 4.748 4.748 Incinerator 99.99 0.000 0.000 None 5.00 1.529 3.450 None 0.00 0.097 0.097 Incinerator 99.99 0.000 0.000 Subtotal Tank Vents 23.5973 25.5183 ______________________________________ 1 * Control afffcIwwlM tor scrubber* r*prM*nt fflcienciM for hytSocarbon*. Ihw* scrubber* hew 99% efficiency tor HCI. Total Post Reduction Emissions j 30.536 32.457 FILE: TEPOST TABLE G-3 HAP EMISSIONS SUMMARY TRI-ETHANE PROCESS UNIT (TE-II) Unweighted HAP Emissions Weighted HAP Emissions Post Percent Post Percent Type Base Year Reduction Reduction Base Year Reduction Reduction (Units) (Mgiyi) (Mg/YO <%> (Mfttyr) (MflYrJ <%> P 6.939 6.939 0.00 6.939 6.939 0.00 T 39.327 23.597 40.00 41.248 25.518 38.14 F Total Total Percent Reduction ______ m______ P-Proem Vonti T-Tar* F-FuqWv* Errtiwlorw 46.266 30.536 34.00 48.187 32.457 32.64 APPENDIX G-A TRI-ETHANE* II PROCESS UNIT STORAGE. TANK CALCULATIONS ssionoie.oiA SL 026099 G-14 Final 05/27/92 Sourc : HON subunit(s) Tri~Ethane (TE-II^ CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM FIXED ROOF STORAGE TANKS (SAMPLE) HAP: 1.1-Dichloroethane (DCE)________ Year: 1987____________ Date: 05/13/92 Calculator: J. Greer Tank Designation: EIO 310. No. 1 DCE Storage Tank (60-1467^ Product: 1.1-Dichloroethane___________________ ____________________________ Tank., charagterirstieg Inside diameter, (ft) Height, (ft) Capacity, (gal) * ir P2h* 4** *7.48 gal. 4 ft1 * if not known Roof color White Shell color __HkUfi Vapor space height, (ft)a Ambient Qffin&tjpns Average atmospheric pressure (psia) (defaults 14.7 psia) Average ambient diurnal temperature (F)b Average annual ambient temperature (oF) Bulk_ Liquid -Characteristics Stored liquid temperature (WF)C Total throughput per year (gal) Number of turnovers per yeard Molecular weight of HAP (lb/lb mole) Mole percent of HAP Partial pressure of the HAP at liquid conditions (psia) _______26 _______36 144.000 D Ht V ________18 H ________14.7 = PA ________18_______ dT ________70_______ - TA 70 * Ts 8.339.470 = An :_________$1^385 = N 2JLj.9_Z- * Mv 10Q______________ = % 3.670 *P Adjustment Factors Paint factor Small diameter tank factor Turnover factorf Product factor9 1,0.... _ Mm 0.655 1^0____ - Fp -c = Kn = Kc SL 026100 Source: HON subunit(s) TE-II CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM FIXED ROOF STORAGE TANKS (SAMPLE)*(CONTINUED) Baseline Control Control device Refrigerator Condenser HAP control efficiency (%) 88.10 calculationsh eff Breathing Loss (Mg/yr) = *>. LB * 1.02E-05 (Mv) ja (^1-73(^0.61(</7).50(^(C)(/g (Pa) ' (P) J* 1.02E-05 (98.97) 3.67 (26)173(18)061(18)050(1 )(0.9924)(1.0) 14.7 - 3.67 2.46 Mg/yr Working Loss (Mg/yr) = L,, = 1.09E-08 MvPVNKnKc = 1.09E-08(98.97)(3.67)(144,000)(61.385)(0.655)(1) 22.94 Mg/yr Total Loss (Mg/yr) ** TL * Lb + I* = (2.46) + (22.94) If a control device is employed. HAP Emissions (E^p) SL 026101 " Total Loss (1 - eff/100) = 25.4 (1 - 88.1/100) 3.02 Mg/yr Source: HON subunit(s) TE-II CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM FIXED ROOF STORAGE TANKS (SAMPLE) (CONTINUED) Calculation (Continued) 3.02 Mg/yr aIf vapor space height is unknown for shell, assume H equals one half tank height. If tank has a cone roof, adjust vapor space height by adding 1/3 of height of cone. bIf average ambient diurnal temperature change is unknown assume 20F. cStored liquid temperature may be approximated from average annual ambient temperature. dN = AN where V N * number of turnovers per year AN = total throughput per year (gal) V = tank capacity (gal) eFor D 30ft, C-l; For 6 S D < 30 ft, C * 0.0771D-0.0013D2-0.1334. fFor turnovers > 36, K,, = (180 + N)/(6 * N) where KM - turnover factor (dimensionless) N = number of turnovers per year For turnovers s 36, KN 1 9Kc = 1.0 for volatile organic liquids Expression for computing HAP emissions are from "Procedures for Establishing Base Year and Post-Reduction HAP Emissions." The calculation procedure is consistent with AP-42. Eor emissions of other HAPs from this EIQ, see summary of calculated emissions from fixed roof storage tanks. SL 026102 G-17 PPG 05/20/92 SL 026103 SUMMARY OF THE CALCULATION INPUTS FOR FIXED-ROOF STORAGE TANKS ASSOCIATED WITH THE TRI ETHANE-II PROCESS UNIT (TE-II) EIQ Tank Tank NO. ID Deacription 310 60-1467 No. 1 DCE Storage Tark 310 60-1468 No. 2 DCE Storage Tor* 315 60-1482 No. 1 OHC Product Tar* 315 60-1463 No. 2 OHC Product Tar* 315 60-1464 N . 1 OHC Crude Storeqe Tank 315 60-1465 No. 2 OHC Crude Storage Tank 316 600396 Spec. Tank No. 12 316 600396 Spec. Tank No 12 316 600396 Spec. Tank No. 12 317 600539 Spec. Tank No. 6 317 600539 Spec. T ark No. 6 318 600540 Spec. Tank No. 7 316 600540 Spec. Tar* No. 7 319 60-1026 Spec. Tank No. 8 319 60-1028 Spec. Tank No. 8 319 60-1028 Spec. Tark No. 6 319 60-1028 Spec. Tank No. 8 319 60-1028 Spec. Tank No. 6 320 60-1029 Spec. T ank No. 9 320 60-1029 Spec. Tank No. 9 320 60-1029 Spec. Tank No. 9 320 60-1029 Spec. Tank No. 9 320 60-1029 Spec. Tank No. 9 321 60-1030 Spec. Tank No. fO 321 60-1030 Spec. Tank No. 10 321 60-1030 Spec. Tank No. 10 321 60-1030 Spec. Tank No. 10 321 60-1030 Spec.Tank No. 10 321 60-1030 Spec. Tar* No. 10 321 60-1030 Spec. Tark No. 10 321 60-1030 Spec. Tw* No. 10 322 60-1031 Spec. Tank No. 11 322 60-1031 Spec. Tar* No. 11 322 60-1031 Spec.Tank No. 11 HAP DCE DCE EDC EDC EDC EDC BLM MC NTE MC NTE MC NTE BLM OME* MC NTE TBL* BLM DME* MC NTE TBL* BLM BTE* DOL* MC NRE NTE TBL* TLE BLM BTE* DOL* Mole Percent 100.00 10000 100.00 100.00 100.00 100.00 0.11 99.29 0.60 99.40 0.60 99.40 0.60 0.90 2.46 93.94 0.56 2.11 0.90 2.46 93.94 0.58 2.11 0.53 1.13 2.75 89.36 3.33 0.57 1.37 0.97 0.53 1.13 2.75 Tar* Color While While White White While White Beige Beige Beige Bejge DVyV Dwgv Beige While White White While White While White While White White White White White While White While White White White White White 0 Inside Diameter (ft.) V Capacity <fl*) H Vapor Space Height (ft.) Ta Stored Liquid Temp. (oF) N Mv P Fp C Number of Molecular Partial Paint Small KN Tirnever* Weight Pressire Factor Diameter Tirnever per Year (b/b mole) (psia) Factor Factor 26.00 26.00 24.00 24.00 24.00 24.00 12.00 12.00 12.00 14.00 14.00 14.00 14.00 18.00 16.00 18.00 18.00 18.00 18.00 16.00 18.00 18.00 18.00 18.00 18.00 16.00 18.00 18.00 18.00 18.00 16.00 18.00 18.00 18.00 144000 144000 101500 101500 101500 101500 13500 13500 13500 19000 18000 18000 18000 42000 42000 42000 42000 42000 42000 42000 42000 42000 42000 42000 42000 42000 42000 42000 42000 42000 42000 42000 42000 42000 16.00 18.00 15.00 15.00 15.00 15.00 7.00 7.00 7.00 12.00 12.00 12.00 12.00 10.00 10.00 10.00 10.00 10.00 10.00 10.00 10.00 10.00 10.00 10.00 10.00 10.00 10.00 10.00 10.00 10.00 10.00 10.00 10.00 10.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 61.39 61.39 140.18 140.18 128.58 128.56 1.00 1.00 1.00 4.78 4.78 4.78 4,78 20.75 20.75 20.75 20.75 20.75 20.75 20.75 20.75 20.75 20.75 2.56 2.56 2.56 2.56 2.56 2.56 2.56 2.56 11.56 11.56 11.56 96.970 98.970 98.970 98.970 98.970 98.970 72.100 133.420 89.090 133.420 89.090 133.420 69.090 72.100 90.100 133.420 89.090 74.120 72.100 90.100 133.420 89.090 74.120 72.100 90.000 74.080 133.420 61.040 89.090 74.120 92.130 72.100 90.000 74.080 3.670 3.670 1.330 1.330 1.330 1.330 0.003 2.007 0.002 2.009 0.002 2.009 0.002 0.026 0.157 1.899 0.001 0.013 0.026 0.157 1.899 0.001 0.013 0.015 0.022 0.037 1.806 0.018 0.001 0.009 0.005 0.015 0.022 0.037 1.00 0.9924 1.00 0.9924 1.00 0.9682 1.00 0.9682 1.00 0.9682 1.00 0.9682 1.30 0.6046 1.30 0.6046 1.30 0.6046 1.30 0.6912 1.30 0.6912 1.30 0.6912 1.30 0.6912 1.00 0.6332 1.00 0.6332 1.00 0.8332 1.00 0.8332 1.00 0.8332 1.00 0.8332 1.00 0.8332 1.00 0.8332 1.00 0.8332 1.00 0.8332 1.00 0.8332 1.00 0.8332 1.00 0.8332 1.00 0.8332 1.00 0.B332 1.00 0.8332 1.00 0.8332 1.00 0.6332 1.00 08332 1.00 0.8332 1.00 0.8332 0.66 0.66 0.38 0.38 0.40 0.40 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 too 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 * = NON HAP, Emission ia ncrt included aa a HAP emission. PPG 05/20/92 SUMMARY OF CALCULATED EMISSIONS FROM FIXED-ROOF STORAGE TANKS ASSOCIATED WITH THE TRIETHANE-II PROCESS UNIT (TE-II) SL 026104 EIQ Tank NO. ID Tank Description 310 60-1467 No. 1 OCE Storage Tank 310 60-1466 No. 2DCE Storage Tank 3t5 60-1462 No. 1 OHC Product Tank 315 60-1483 No. 2 OHC Product Tar* 315 60-1464 No. 1 OHC Crude Storage Tank 315 60-1485 No. 2 OHC Crude Storage Tank 316 600396 Spec. Tank No. 12 3t6 600396 Spec. Tank No. 12 316 600396 Spec. Tank No. 12 317 600539 Spec. Tank No. 6 317 600539 Spec. Tank No. 6 316 600540 Spec. Tank No. 7 318 600540 Spec. Tank No. 7 319 60-1028 Spec. Tank No. 6 319 60-1028 Spec. Tank No. 8 319 60-1028 Spec. Tank No. 6 319 60-1028 Spec. Tank No. 6 319 60-1028 Spec. Tank No. 8 320 60-1029 Spec. Tank No. 9 320 60-1029 Spec. Tank No. 9 320 60-1029 Spec. Tank No. 9 320 60-1029 Spec. Tank No. 9 320 60-1029 Spec. Tank No. 9 321 60-1030 Spec. Tank No. 10 321 60-1030 Spec. Tank No. 10 321 60-1090 Spec. Tank No. 10 321 60-1090 Spec. Tank No. 10 321 60-1030 Spec. Tank No. 10 321 60-1090 Spec. Tank No. 10 321 60-1090 Spec. Tank No. 10 321 60-1030 Spec. Tank No. 10 322 60-1031 Spec. Tank No. 11 322 60-1031 Spec. Tank No. 11 322 60-1091 Spec. Tank No. 11 = NON HAPS, emission is notinciuded as aHAP emission HAP DCE DCE EDC EDO EDC EDC BLM MC NTE MC NTE MC NTE BLM DME* MC NTE TBL* BLM DME* MC NTE TBL* BLM BTE* DOL* MC NRE NTE TBL* TLE BLM BTE* DOL* LB Breathing Loss (Mg/yr) 2.46344 2.46344 0.63883 0.83893 0.83893 0.83893 0.00157 0.25710 0.00116 0.50561 0.00229 0.50561 0.00229 0.01678 0.00000 0.83129 0.00294 0.00000 0.01676 0.00000 0.63129 0.00000 0.00000 0.01165 0.00000 0.00000 0.60717 0.01104 0.00289 0.00000 0.00667 0.01165 0.00000 0.00000 LW Working Loss (Mg/yr) 22.93602 22.93602 7.77118 7.77118 7.48961 7.48961 0.00003 0.03940 0.00002 0.25140 0.00013 0.25140 0.00013 0.01776 0.00000 2.40679 0.00124 0.00000 0.01776 0.00000 2.40679 0.00000 0.00000 0.00128 0.00000 0.00000 0.28289 0.00128 0.00015 0.00000 0.00050 0.00579 0.00000 0.00000 LT Total Loss (Mg/yr) Contd Device 1987 Control Unweighted Efficiency HAP Emissions {%) (Mg/yr) 1987 Weighted HAP Emissions (Mg/yr) 25.39945 25.39945 6.61011 8.61011 6.32864 6.32854 0.00160 0.29650 0.00118 0.75701 0.00242 0.75701 0.00242 0.03454 0.00000 3.03808 0.00416 0.00000 0.03454 0.00000 3.03808 0.00000 0.00000 0.01293 0.00000 0.00000 0.89006 0.01232 0.00304 0.00000 0.00718 0.01744 0.00000 0.00000 RVR RVR RVR RVR RVR RVR None None None None None None None None None None None None None None None None None None None None None None None None None None None None 88.10 88.10 88.00 88.00 88.00 88.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 3.02254 3.02254 1.03321 1.03321 0.99942 0.99942 0.00160 0.29650 0.00116 0.75701 0.00242 0.75701 0.00242 0.03454 0.00000 3.03808 0.00418 0.00000 0.03454 0.00000 3.03808 0.00000 0.00000 0.01293 0.00000 0.00000 0.89006 0.01232 0.00304 0.00000 0.00718 0.01744 0.00000 0.00000 3.02254 3.02254 1.03321 1.03321 0.99942 0.99942 0.00160 0.29650 0.00118 0.75701 0.00242 0.75701 0.00242 0.03454 0.00000 3.03808 0.00418 0.00000 0.03454 0.00000 3.03808 0.00000 0.00000 0.01293 0.00000 0.00000 0.89006 0.01232 0.00304 0.00000 0.00716 0.01744 0.00000 0.00000 PPG 05/20/92 yi ^ SUMMARY OF THE CALCULATION INPUTS FOR FIXED-ROOF STORAGE TANKS o ASSOCIATED WITH THE TRI ETHANE-II PROCESS UNIT (TE-II) O' ------------------------------------ -------------- - ----__________________________________________ __ _________________________________________ m EIQ NO. Tank ID Tank Description 322 60-1031 Spec. Tark No. 11 322 60-1031 Spec. Tank No. 11 322 80-1031 Spec. Tark No. 11 322 60-1031 Spec. Tank No. 11 322 60-1001 Spec. Tark No. 11 323 60-1166 Spec. Tark No. 12 323 60-1166 Spec. Tank No. 12 324 60-1470 No. 1 DOL/SBLTark 324 60-1470 No. 1 DOl/SBL Tank 324 60-1471 No 2 DOL/SBLTark 324 60-1471 No. 2 DOL/SBLTark 324 60-1472 No. 2 BLM Storage Tank 324 60-1473 DOL/DOX SBL Tark 324 60-1473 DOL/DOX SBL Tank 324 60-1475 S-4 Tark 324 60-1475 S-4 Tark 324 60-1475 S-4 Tark 324 60-1475 S-4 Tar* 324 60-1475 S-4 Tark 324 60-1475 S-4 Tark 324 60-1476 S-3Tark 324 60-1476 S-3Tark 324 60-1476 S-3 Tark 324 60-1476 BO Tank 324 60-1476 S-3 Tank 324 60-1476 S-3 Tank 324 60-1477 S-2 Tank 324 60-1477 S-2 Tank 324 60-1477 S-2 Tark 324 60-1477 S-2 Tar* 324 60-1477 S-2 Tar* 324 60-1477 S-2 Tar* 324 60-1478 No. 3 Day Tank 324 60-1478 No. 3 Day Tank HAP Mote Percent Tank Color D Iraida Diameter (It) V Capacity (9*-) Vapor Spue Height (M Stared Liquid Temp. (oF) N Mv P PP C Number of Molecular Partial Paint Small KN Turnovers Weight Pressire Factor Diameter Turnover per Year (b/b mole) (Pta) Factor Factor MC NRE NTE TBL* TLE MC NTE DOX SBL* DOX SBL* Butylene Ox DOL* DOX OOL* DOX MC NRE NTE SBL* DOL* DOX MC NRE NTE SBL* DOL* DOX MC NRE NTE SBL* MC NTE 69.36 While 3.33 White 0.57 While 1.37 While 0.97 White 99.40 While 0.60 While 67.65 Beige 32.15 67.65 wOBeM-ti-gp-Ve 32.15 Beige 100.00 Tan 54.32 45.66 Bome-lig-gm-e 1.75 Aqua Green 1.47 Aqua Green 93.45 Aqua Green 1.06 Aqua Green 0.51 Aqua Green 1.75 Aqua Green 1.75 Aqua Green 1.47 Aqua Green 93.45 Aqua Green 1.06 Aqua Green 0.51 Aqua Green 1.75 Aqua Green 1.75 Aqua Green 1.47 Aqua Green 93.45 Aqua Green 1.06 Aqua Green 0.51 Aqua Green 1.75 Aqua Green 99.47 White 0.53 White 16.00 16.00 16.00 16.00 16.00 18.00 18.00 13.00 13.00 13.00 13.00 13.00 16.00 16.00 24.00 24.00 24.00 24.00 24.00 24.00 24 00 24.00 24.00 24.00 24.00 24.00 24.00 24.00 24.00 24.00 24.00 24.00 24.00 24.00 42000 42000 42000 42000 42000 42000 42000 19000 19000 19000 19000 17600 28600 28600 101500 101500 10t500 101500 101500 101500 101500 101500 101500 101500 101500 101500 101500 101500 101500 101500 10f500 101500 101500 101500 10.00 10.00 10.00 10.00 10.00 10.00 10.00 9.00 9.00 9.00 9.00 9.00 9.00 9.00 15.00 15.00 15.00 15.00 15.00 15.00 15.00 15.00 15.00 15.00 15.00 15.00 12.00 12.00 12.00 12.00 12.00 12.00 15.00 15.00 70.00 70.00 70.00 70.00 7000 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 7000 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 11.56 11.56 11.56 11.56 11.56 11.56 11.56 0.74 0.74 0.49 0.49 1.57 10.80 10.80 28.51 28.51 28.51 28.51 26.5t 28.51 28.51 28.51 28.51 28.51 28.51 28.51 28.51 28.51 28.51 28.51 28.51 28.51 3.19 3.19 133.420 61.040 89.090 74.120 92.130 133.420 69.090 88.100 74.120 68.100 74.120 72.120 74.060 68.100 74.080 88.100 133.420 61.040 89.090 74.120 74.080 88.100 133.420 61.040 89.090 74.120 74.080 88.100 133.420 61.040 69.090 74.120 133.420 89.090 1.806 0.018 0.001 0.009 0.005 2.009 0.002 0.373 0.062 0.373 0.062 2.708 0.735 0.251 0.024 0.008 1.889 0.006 0.001 0.003 0.024 0.008 1.889 0.006 0.001 0.003 0.024 0.006 1.889 0.006 0.001 0.003 2.010 0.001 1.00 0.8332 1.00 0.8332 1.00 0.8332 1.00 0.8332 1.00 0.8332 1.00 0.8332 1.00 0.8332 1.30 0.6492 1.30 0.6492 1.30 0.6492 1.30 0.6492 1.30 0.6492 1.30 0.7674 1.30 0,7674 1.30 0.9682 1.30 0.9662 1.30 0.9682 1.30 0.9682 1.30 0.9682 1.30 0.9682 1.30 0.9682 1.30 0.9682 1.30 0.9682 1.30 0.9682 1.30 0.9682 1.30 0.9682 1.30 0.9682 1.30 0.9682 1.30 0.9682 1.30 0.9682 1.30 0.9682 1.30 0.9662 1.00 0.9662 1.00 0.9682 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 too 1.00 1.00 1.00 1.00 = NON HAP, Emission is not included as a HAP emission. PPG 05/2Q/92 SUMMARY OF CALCULATED EMISSIONS FROM FIXED-ROOF STORAGE TANKS ASSOCIATED WITH THE TRIETHANE-II PROCESS UNIT (TE-II) SL 026106 EIQ Tank NO. ID Tank Description 322 60-1031 Spec. Tank No. 11 322 60-1081 Spec. Tank No. 11 322 60-1031 Spec. Tank No. 11 322 60-1031 Spec. Tank No. 11 322 60-1031 Spec. Tank No. 11 323 60-1166 Spec. Tank No. 12 323 604166 Spec. Tank No. 12 324 60-1470 No. 1 DOL/SBL Tank 324 60-1470 No. 1 DOLTSBl Tank 324 60-1471 No. 2 DOL/SBL Tank 324 60-1471 No. 2 DOL/SBL Tank 324 604472 No. 2 BLM Storage Tank 324 60-1473 DOLflJOX SBL Tank 324 60-1473 OOLjOOX SBL Tank 324 60-1475 S-4 Tank 324 60-1475 04 Tank 324 60-1475 0-4 Tank 324 60-1475 0-4 Tank 324 60-1475 04 Tank 324 60-1475 0-4 Tank 324 604476 03 Tank 324 601476 0-3 Tank 324 601476 08 Tank 324 601476 08 Tank 324 601476 08 Tank 324 601476 08 Tank 324 601477 S-2 Tank 324 601477 08 Tank 324 601477 S-2 Tank 324 601477 S-2 Tank 324 601477 S-2 Tank 324 601477 S-2 Tank 324 601478 No. 3 Day Tank 324 601478 No. 3 Day Tank = NON HAPS, emission Is not included as a HAP emission HAP MC NRE NTE TBL* TLE MC NTE BOX SBL* DOX SBL* Butylene Oxide DOL* DOX DOL* oox MC NRE NTE SBL* DOL* DOX MC NRE NTE SBL* DOL* DOX MC NRE NTE SBL* MC NTE LB Breathing Loss (Mg/yr) 0.60717 0.01104 0.00289 000000 0.00667 0.65986 0.00299 0.06963 0.00000 0.06983 0.00000 0.24627 0.00000 0.08961 0.00000 0.02839 1.92105 0.01561 0.00619 0.00000 0.00000 0.02839 1.92105 0.01561 0.00819 0.00000 0.00000 0.02533 1.71441 0.01384 0.00731 0.00000 1.55194 0.00643 LW Working Loss (Mg/yr) 1.27529 0.00579 0.00066 0.00000 0.00228 1.41863 0.00071 0.00501 0.00000 0.00334 0.00000 0.05964 0.00000 0.07451 0.00000 0.02253 7.94661 0.01101 0.00360 0.00000 0.00000 0.02253 7.94861 0.01101 0.00360 0.00000 0.00000 0.02253 7.94661 0.01101 0.00360 0.00000 0.94647 0.00042 LT Total Loss (Mg/yr) Confrol Device 1987 Confrol Unweighted Efficiency HAP Emissions (%) (Mg/yr) 1967 Weighted HAP Emissions (Mg/yr) 1.66246 0.01683 0.00367 0.00000 0.00895 2.07849 0.00370 0.07464 000000 0.07317 0.00000 0.30791 0.00000 0.16432 0.00000 0.05091 9.86766 0.02653 0.01179 0.00000 0.00000 0.05091 9.66766 0.02653 0.01179 0.00000 0.00000 0.04786 9.66102 0.02486 0.01091 0.00000 2.49841 0.00665 None None None None None None None RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR 0.00 0.00 0.00 0.00 0.00 0.00 0.00 84.00 84.00 84.00 84.00 64.00 84.00 64.00 84.00 64.00 64.00 84.00 84.00 64.00 84.00 84.00 84.00 64.00 84.00 84.00 84.00 64.00 84.00 84.00 84.00 84.00 64 00 84.00 1.88246 0.01683 0.00367 0.00000 0.00895 2.07849 0.00370 0.01197 0.00000 0.01171 0.00000 0.04927 0.00000 0.02629 0.00000 0.00815 1.57863 0.00424 0.00189 0.00000 0.00000 0.00815 1.57683 0.00424 0.00189 0.00000 0.00000 0.00766 1.54576 0.00398 0.00175 0.00000 0.39975 0.00110 1.68246 0.01683 0.00357 0.00000 0.00895 2.07649 0.00370 0.01197 0.00000 0.01171 0.00000 0.04927 0.00000 0.02629 0.00000 0.00815 1.57883 0.00424 0.00189 0.00000 0.00000 0.00815 1.57883 0.00424 0.00189 0.00000 0.00000 0.00766 1.54576 0.00398 0.00175 0.00000 0.39975 0.00110 PPG 05/20/92 SL 026107 SUMMARY OF THE CALCULATION INPUTS FOR FIXED-ROOF STORAGE TANKS ASSOCIATED WITH THE TRI ETHANE-II PROCESS UNIT (TE-II) EIO Tank NO. ID Tank Description 324 60-1479 No. 2 Day Tank 324 60-1479 No. 2 Day Tank 324 60-1460 No. 1 Oay Tank 324 60-1460 No. 1 Day Tank 324 60-1481 S-1 Tar* 324 60-1461 S-1 Tar* 324 60-1481 S-1 Tar* 324 60-1481 S-1 Tank 324 60-1481 S-1 Tank 324 60-1481 S-1 Tar* 324 60-1896 No. 4 NRE Tank 324 60-1696 No. 4 NRE Tank 325 600413 No. 2 Trtelhane Dock Storage Tank 325 600413 No. 2 Trtelhane Dock Storage Tank 325 600413 No. 2 Triethane Dock Storage Tank 325 600413 No. 2 Trtelhane Dock Storage Tar* 325 600413 No. 2 Trtelhane Dock Storage Tank 325 600413 No. 2 Trtelhane Dock Storage Tar* 325 600530 No. 1 Triethane Dock Storage Tank 325 600530 No. 1 Trtelhane Dock Storage Tar* 325 600530 No. 1 Triothane Dock Storage Tank 325 600530 No. 1 Trtelhane Dock Storage Tar* 325 600530 No. 1 Triethane Dock Storage Tank 325 600530 No. 1 Trtelhane Dock Storage Tar* 325 601465 No. 3 Trtelhane Dock Storage Tank 325 601465 No. 3 Trtelhane Dock Storage Tank 325 601465 No. 3 Triothane Dock Storage Tar* 325 601465 No. 3 Trtelhane Dock Storage Tank 325 601465 No. 3 Triethane Dock Storage Tank 325 601465 No. 3 Trtelhane Dock Storage Tank 326 601133 TE-II Shipping Tar* 326 601133 TE-II Shipping Tar* 326 601133 TE-II Shipping Tar* 326 601133 TE-II Shipping Tar* HAP MC NTE MC NTE DOL* DOX MC NRE NTE SBL* MC NRE DOL* DOX MC NRE NTE SBL* DOL* DOX MC NRE NTE SBL* DOL* DOX MC NRE NTE SBL* DOL* DOX MC NRE Mote Percent Tank Color D Iraki* Diameter (It) V Capacity (9*) H Vapor Space Height (ft) Ta Stared Liquid Temp. (oF) N Mv P Fp C Number of Molecular Partial Paint Small KN Turnovers Weight Pressire Factor Diameter Tianover par Tear (to/to mole) (paia) Factor Factor 99.47 White 0.53 White 99.47 White 0.53 White 1.75 Aqua Green 1.47 Aqua Green 93.45 Aqua Green 1.06 Aqua Green 0.51 Aqua Green 1.75 Aqua Green 31.39 Beige 68.61 Beige 1.75 While 1.47 White 93.18 White 1.27 While 0.56 White 1.75 White 1.75 White 1.47 While 93.18 White 1.27 White 0.56 White 1.75 White 1.75 White 1.47 White 93.18 White 1.27 White 0.58 White 1.75 While 1.75 White 1.47 White 93.45 White 1.06 White 24.00 24.00 24.00 24.00 18.00 16.00 18.00 16.00 16.00 16.00 21.00 21.00 32.00 32.00 32.00 32.00 32.00 32.00 32.00 32.00 32.00 32.00 32.00 32.00 80.00 60.00 60.00 60.00 60.00 60.00 12.00 12.00 12.00 12.00 101500 101500 101500 101500 46660 46660 46660 46660 46660 46660 62200 62200 420000 420000 420000 420000 420000 420000 420000 420000 420000 420000 420000 420000 1006000 1008000 1006000 1006000 1006000 1006000 25200 25200 25200 25200 15.00 15.00 15.00 15.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 12.00 24.00 24.00 24.00 24.00 24.00 24.00 24.00 24.00 24.00 24.00 24.00 24.00 24.00 24.00 24.00 24.00 24.00 24.00 17.00 17.00 17.00 17.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 3.19 3.19 3.19 3.19 62.01 62.01 62.01 62.01 62.01 62.01 1.43 1.43 7.11 7.11 7.11 7.11 7.11 7.11 7.11 7.11 7.11 7.11 7.11 7.11 2.96 2.96 2.96 2.96 2.96 2.96 33.15 33.15 33.15 33.15 133.420 69.090 133.420 69.090 74.060 68.100 133.420 61.040 89.090 74.120 133.420 61.040 74.060 68.100 133.420 61.040 69.090 74.120 74.080 80.100 133.420 61.040 89.090 74.120 74.080 68.100 133.420 61.040 89.090 74.120 74.060 88.100 133.420 61.040 2.010 0.001 2.010 0.001 0.024 0.006 1.689 0.006 0.001 0.003 0.634 0.369 0.024 0.006 1.883 0.007 0.001 0.003 0.024 0.006 1.883 0.007 0.001 0.003 0.024 0.006 1.883 0,007 0.001 0.003 0.024 0.008 1.689 0.006 1.00 0.9662 1.00 0.9662 1.00 0.9662 1.00 0.9682 1.30 0.8332 1.30 0.8332 1.30 0.8332 1.30 0.8332 1.30 0.6332 1.30 0.8332 1.30 0.9124 1.30 0.9124 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 1.0000 1.00 t.0000 1.00 1.0000 1.00 0.6046 1.00 0.6046 1.00 0.6046 1.00 0.6046 1.00 1.00 1.00 1.00 0.65 0.65 0.65 0.65 0.65 0.65 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 too 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 * *= NON HAP, Emission is not included as a HAP emission. PPG 05/20/92 SUMMARY OF CALCULATED EMISSIONS FROM FIXED-ROOF STORAGE TANKS ASSOCIATED WITH THE TRIETHANE-II PROCESS UNIT (TE-II) 026108 EIO Tank NO. to Tank Description 324 60-1479 No. 2 Day Tank 324 60-1479 No. 2 Day Tank 324 60-1460 No. 1 Day Tank 324 60-1480 No. 1 Day Tank 324 60-1461 0-1 Tank 324 60-1461 S-1 Tank 324 60-1481 0-1 Tank 324 60-1461 S-1 Tank 324 60-1461 S-1 Tank 324 60-1461 S-1 Tank 324 60-1806 No. 4 NRE Tank 324 60-1606 No. 4 NRE Tank 325 60-0413 No. 2 Triethane Dock Storage Tank 325 600413 No. 2 Trfelhane Dock Storage Tank 325 600413 No. 2 Trieftane Dock Storage Tank 325 600413 No. 2 Triethane Dock Storage Tank 325 600413 No. 2 Triethane Dock Storage Tank 325 600413 No. 2 Triethane Dock Storage Tank 325 600530 No. 1 Triethane Dock Storage Tank 325 600530 No. 1 Trietfwne Dock Storage Tank 325 600530 No. 1 Triethane Dock Storage Tank 325 600530 No. 1 Triethane Dock Storage Tank 325 600530 No. 1 Triethane Dock Storage Tank 325 600530 No. 1 Triethane Dock Storage Tank 325 60-1465 No. 3 Triethane Dock Storage Tank 325 60-1465 No. 3 Triethane Dock Storage Tank 325 60-1465 No. 3 Trieftane Dock Storage Tank 325 60-1465 No. 3 Triethane Dock Storage Tank 325 60-1465 No. 3 Triethane Dock Storage Tank 325 60-1465 No. 3 Triethane Dock Storage Tank 326 60-1133 TE-II Shipping Tank 326 60-1133 TE-II Shipping Tank 326 60-1133 TE-II Shipping Tank 326 60-1133 TE-II Shipping Tank = NON HAPS, mission is not included as a HAP mission HAP MC NTE MC NTE DOL* DOX MC NRE NTE SBL* MC NRE DOL* DOX MC NRE NTE SSL* DOL* DOX MC NRE NTE SBL* DOL* DOX MC NRE NTE SBL* DOL* DOX MC NRE LB Breathing Loss (Mg/yr) 1.55194 0.00643 1.55194 0.00643 0.00000 0.01325 0.69692 0.00724 0.00362 0.00000 0.57314 0.17906 0.00000 0.04706 3.16363 0.02911 0.01486 0.00000 0.00000 0.04706 3.16353 0.02911 0.01486 0.00000 0.00000 0.13961 9.44500 0.08637 0.04409 0.00000 0.00000 0.00436 0.29651 0.00239 LW Working Loss (Mg/yr) 0.94647 0.00042 0.94647 0.00042 0.00000 0.01465 5.16696 0.00716 0.00234 0.00000 0.06210 0.02164 0.00000 0.02319 8.16106 0.01360 0.00424 0.00000 0.00000 0.02319 6.18106 0.01360 0.00424 0.00000 0.00000 0.02319 8.16106 0.01360 0.00424 0.00000 0.00000 0.00651 2.29469 0.00318 LT Total Loss (Mg/yr) Control Device 1987 Contol Unweighted Efficiency HAP Emissions <%) (Mg/yr) 1987 W Ightsd HAP Emissions (Mg/yr) 2.49641 0.00665 2.49641 0.00685 0.00000 0.02791 6.06568 0.01441 0.00616 0.00000 0.65523 0.20092 0.00000 0.07025 11.36460 0.04272 0.01910 0.00000 0.00000 0.07025 11.36460 0.04272 0.01910 0.00000 0.00000 0.16260 17.62606 0.09997 0.04832 0.00000 0.00000 0.01089 2.59120 0.00557 RVR RVfi RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR RVR None None None None 84.00 84.00 84.00 84.00 84.00 84.00 84.00 84.00 84.00 64.00 84.00 84.00 68.40 68.40 88.40 88.40 88.40 88.40 88.40 88.40 86.40 68.40 86.40 86.40 88.40 86.40 88.40 88.40 88.40 88.40 0.00 0.00 0.00 0.00 0.39975 0.00110 0.39975 0.00110 0.00000 0.00447 0.97064 0.00230 0.00099 0.00000 0.10484 0.03215 0.00000 0.00815 1.31629 0.00496 0.00222 0.00000 0.00000 0.00815 1.31629 0.00496 0.00222 0.00000 0.00000 0.01889 2.04462 0.01160 0.00561 0.00000 0.00000 0.01089 2.59120 0.00557 0.39975 0.00110 0.39975 0.00110 0.00000 0.00447 0.97054 0.00230 0.00099 0.00000 0.10464 0.03215 0.00000 0.00815 1.31829 0.00498 0.00222 0.00000 0.00000 0.00615 1.31829 0.00496 0.00222 0.00000 0.00000 0.01889 2.04462 0.01160 0.00561 0.00000 0.00000 0.01069 2.59120 0.00557 W PPG 05/20/92 026109 SUMMARY OF THE CALCULATION INPUTS FOR FIXEO-ROOF STORAGE TANKS ASSOCIATED WITH THE TRI ETHANE-II PROCESS UNIT (TE-II) EtQ Tank Tank NO. 10 Deaeration 326 60-1133 TE-II Shaping Tank 326 60-1133 TE-II Shipping Tank 353 60-1469 TCE-Teta Storage Tank 353 60-1469 TCE-Tetia Storage Tank 353 60-1469 TCE-Tete Storage Tank 353 60-1469 TCE-Te*a Storage Tank 355 60403 No. 1 BLM Storage Tank 358 60-1032 TBL/MC Storage Tank 356 60-1032 TBL/MC Storage Tank ) } HAP Mole Percent NTE SSL* PENTA* SYM TCE UNSYM* Butylene Ck MC TBL* 0.51 1.75 4.16 12.47 60.16 23.22 100.00 35.71 64.29 Tank Color 0 Inside Olametor () V Capacity (gai) H Vapor Space 1nletijintii (.) Ta Starad Liquid Temp. (oF) N Mv P Fp C Number of Molectiar Partial Point Sinai KN Turnovers Weight Pressure factor Diameter Turnover par Year (b/b mole) (Pla) factor factor White White Green Green Green Green White White While 12.00 12.00 42.00 42.00 42.00 42.00 8.00 1200 12.00 25200 25200 435300 435300 435300 435300 4115 15000 15000 17.00 17.00 21.00 21.00 21.00 21.00 5.00 10.00 10.00 70.00 70.00 70.00 70.00 70.00 70.00 70.00 100.00 100.00 33.15 33.15 0.11 0.11 0.11 0.11 6.61 8.17 3.17 89.090 74.120 202.290 167.864 133.410 167.664 72.120 133.420 74.120 0.001 0.003 0.003 0.012 0.229 0.050 2.700 1.466 0.771 1.00 0.6046 1.00 0.6046 1.30 1.0000 1.30 1.0000 1.30 1.0000 1.30 1.0000 1.00 0.4002 1.00 0.6046 1.00 0.6046 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 1.00 = NON HAP, Emission is not included as a HAP emission. PPG 05/2CV92 U1 r* oto O' v* EIQ NO. Tank ID SUMMARY OF CALCULATED EMISSIONS FROM FIXED-ROOF STORAGE TANKS ASSOCIATED WITH THE TRIETHANE-II PROCESS UNIT (TE-II) Tar* Description HAP LB Breathing Loss (Mg/yr) LW Working Loss (Mg/yr) LT Total Loss (Mg/yr) Control Device 1987 Contol Unweighted Efficiency HAP Emissions <%) (Mg/yr) 1987 Weighted HAP Emissions (Mg/yr) 326 60-1133 TE-II Shipping Tar* 326 60-1133 TE-II Shipping Tar* 353 60-1469 TCE-Tets Storage Tar* 353 60-1469 TCE-Tefea Storage Tar* 353 60-1469 TCE-Tets Storage Tank 353 60-1469 TCE-Teta Storage Tar* 355 60-403 No. 1 BLM Storage Tar* 358 60-1032 TBLA4C Storage Tor* 358 60-1032 TBt/MC Storage Tank NTE SBL* PENTA* SYM TCE UNSYM* Butylene Oxide MC TBL* 0.00126 0.00000 0.00000 0.23402 1.35813 0.00000 0.03786 0.18630 0.00000 0.00104 0.00000 0.00000 0.00112 0.01639 0.00000 0.05964 0.10155 0.00000 0.00230 0.00000 0.00000 0.23515 1.37452 0.00000 0.09730 0.28785 0.00000 None None Scrubber Scrubber Scrubber Scrubber None None None 0.00 0.00 5.00 5.00 5.00 5.00 0.00 0.00 0.00 0.00230 0.00000 0.00000 0.22339 1.30579 0.00000 0.09730 0.28785 0.00000 0.00230 0.00000 0.00000 2.23391 1.30579 0.00000 0.09730 0.28785 0.00000 NON HAPS. emission is not included as a HAP amission APPENDIX G-B TRI-ETHANE* II PROCESS UNIT PROCESS VENT CALCULATIONS SL 0261H 5510R016.01A G-26 Final 05/27/92 Source: HQM-JSUfeUnitlsj *13.13?.-IL.PgggW .UhiL HAPs emitted: !,.I.-OighiaEaPtliang-CPQ)^.ilgthYl Chl<?XfgER.fMC) , HC1 CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: None Date: Year: 1987 Calculator: April 1992 S.R, Process Vent Identification: 305 (non-routine) Description: MC/DCE startup Scrubber-------------------------------------------- Process Conditions/Sampling Date of flow measurement Method of flow measurement N/A____________________ Date of concentration measurement Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) N/A___________________ Describe any problems encountered during testing N/A________________ Production rate during flow determination (lbs/hr) Production rate during sampling (lbs/hr) Average production rate during base year (lbs/hr) stream _phar cis_t jgs Average vent stream flow rate (ftJ/min) HAP concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risk weighting factor -----------------______ -----------------_______ ------ ______ ---------------- Control Control device ____________________________________________ HAP control efficiency (%) ______ CalGhlflUQDg* Uncontrolled Emissions (E0) = (2.54E-09) 0 C h MW P T + 460 Uncontrolled Emissions (Ey) = f2.54E-09)(0)(0)(0)(0) (0) + 460 1 Q C h T MW P FHR = eff 0 Mg/yr HAP Emissions (Chap) " (1 " eff/100) -OQQ ^There were no non-routine releases in 1987, 1988 and 1989. SL 026112 G-27 Sourc : HON subunit(s) Tri-Ethane II Process Unit CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (E^p) * o (l - o/ioo) 0 Mg/yr Weighted HAP Emissions = E^p FHR Weighted HAP Emissions = (o) (-- ) 0 Mg/yr If the conditions during testing are not representative of has year operation, make the appropriate extrapolation below and xplain: N/A If the flow or concentration were not measured using an EPA reference method, EPA conditional method or validated using Method 301, provide justification and supporting calculations: N/A Expression provided in "Procedures for Establishing Base Year and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. SL 026113 G-28 Source: HON subunit(s) Tri-Ethane XI Process Unit HAPs emitted: 1.1-Dichloroethane (DCE1. Methvl Chloroform (MC) . Hydrochloric Acid (HC1) ____________ CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: 1,1-Dichloroethane (DCE)________ Year: 1987 Calculator: Date: April 1992 _ S.R^ Process Vent Identification: 305 (startup) Description: MC/_DCE Startup Scrubber.____________________________ Process Conditions/Sampling Date of flow measurement Method of flow measurement Calculated Date of concentration measurement Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) Calculated1 __zrz_ Describe any problems encountered during testing N/A Production rate during flow determination (lbs/hr) Production rate during sampling (lbs/hr) Average production rate during base year (lbs/hr) 19,086 19.086 19.086 stream cfrarast_gri;_Eigs Average vent stream flow rate (ft^/min) HAP concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risk weighting factor 3*519 21*221 4 99 14-tl 1 =Q = MW Control Control device Sgrufrbgr HAP control efficiency (%) 99% for HC1 * eff 5% for hydrocarbons Calculations* Uncontrolled Emissions (Ey) = (2.54E-091 0 C h MW p T + 460 Uncontrolled Emissions (Ev) = _(2.54E-09) (3^619) (22.227) (4) (99) (14.7) ________(80) + 460 2.205 Mg/yr HAP Emissions (E^p) * Ey (1 " eff/100) xs e next pag . 0261lA G-29 Source: HON subunit(s) Tri-Ethane II Process Unit CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (E^) = 2.205 (1 - 5/100) 1.948 Mg/yr Weighted HAP Emissions = E^^p F^ Weighted HAP Emissions * (1.948 ) (1) 1.948 Mg/yr Total HAPs Emissions* * Total Weighted HAPs Emissions = 3.004 Mg/yr 3.004 Mg/yr If the conditions during testing are not representative of base year operation, make the appropriate extrapolation below and explain: N/A If the flow or concentration were not measured using an EPA reference method, EPA conditional method or validated using M th d 301, provide justification and supporting calculations: During startup the following emissions will occur: Component DCE MC HQ lb/lb-mole 99 133 36 lb/hr 2,556 1,179 18,620 22,355 % wt 11.4 5.3 83.3 100 mole 25.82 8.865 517.23 551.915 % mole 4.7 1.6 93.7 100 Avg. Ib/lb-mole 4.653 2.128 33.732 40.513 SL 026115 G-30 Source: HON subunit(s) Tri-Ethane IT Process Unit These rates are determined for a production of 450 tpd in 1987. The production was 214 tpd at 0.5 hr/startup, 1987 emissions = 22,355 x 0.5 & x 214 = 5315.53 lb/su su 450 - 5315.53 x = 42524.24 Ib/yr yr - ^25^'24 - 10631.1 ibfyr 4 DCE emissions = 10631.1 IbfhrxH^. 1212 Ibfhr 100 MC emissions = 10631.1 Ibfhr x -- = 563.45 Ibfhr 100 HCI emissions - 10631.1 ibfhrx ^2. * 8855.7 Ibfhr Stack gas flow rate - 22355 lfe x lb-mole x 379 ft3 x 540 R hr 40.513 lb lb-mole 520 R - 217,175 ft3/hr * 3,619 ft3/min Concentration calculation of DCE; DCE emission 1212 lb/hr (uncontrolled) Flow Rate 3619 ft3/min - 217,175 ft3/hr amount of DCE in vent, 1212 lb x lb-mole = hr 99 lb 12.24 lb-mole hr - 12.24 lb-roole/hr - 0.000056 lb-mole 217,175 ftJ/hr ft3 st ol6Ub G-31 Source: HON subunit(s) Tri-Ethane II Process Unit DCE concentration, C = (0.000056 Ib-molefft3) (0.7302 ft3 atnilb-mole R) ,(80.460)- flx1(). atm . 22227 ppm MC concentrations, emissions = 563.45 Ibfhr (uncontrolled) r _ (563.45) (0.7302) (80 + 460) 1Q, (133) (217,175) 7692 ppm HCI concentrations HCI emissions - 8855.7 Ibfhr (uncontrolled) C g855-7) <-7302) (80 - 460) 10a , (38) (217,175) ^ aExpression provided in "Procedures for Establishing Base Year and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. See Attachment I for calculation. 0^ G-32 ATTACHMENT I SUBUNIT: VENT ID: SCENARIO: DESCRIPTION: TE-II 305 STARTUP MCyDCE STARTUP SCRUBBER YEAR: 1987 8X1920 ^ Q C h T MW P FHR eff EU EHAP EW Average vent stream flow rate (ftsihnln) HAP Concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (Ib/lb-mole) Pressure at point of discharge (peia) HAP high risk weighting factor HAP control efficiency (%) Uncontrolled emissions (Mgfyr) Controlled emissions (Mg/yr) Weighted HAP emissions (Mg/yr) ; EU - (2.54E-09 xQ xC x h* MWx P) / (T + 460) EHAP - EU * (i - (aft/ioo)) EW - EHAP x FHR 0 u1> w COMPONENT Q C h MW P T eff FHR EU EHAP EW DCE 3619 22,227 4.00 99 14.7 120 5.00 1 2.051 1.946 1.948 MC 3619 7,692 4.00 133 14.7 120 5.00 1 0.953 0.906 0,906 HCL 3619 446,626 4.00 36 14.7 120 99.00 1 14.964 0.150 0.150 FILE: N16 TOTAL 17.988 8.004 3.004 Source: HON subunit(s) Tri-Ethane II Process Unit HAPs emitted: Ethylene Dichloride (EDC1. Hydrochloric Acid fHCl^ CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: Ethylene Dichloride (EDC) year: 1987 Calculator: _ S,R. Date: April-1992, Process Vent Identification: 306 (non-routine) Description: No. 2 OHC Startup .Scrubber_________________________ Process Conditions/Sampling Date of flow measurement Method of flow measurement Calculated1 Date of concentration measurement Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) Syringe Sample. Describe any problems encountered during testing None Identified Production rate during flow determination (lbs/hr) Production rate during sampling (lbs/hr) Average production rate during base year (lbs/hr) 1987 1987 GC/TCD 19.QSS. . I9.,t-Q86. Stream Characteristics Average vent stream flow rate (ft3/min) HAP concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risk weighting factor ________17.4 996.384 __________7.42 80 99 ________14.7 1 -Q -C *h =T = MW P CgPtafll Control device Scrubber HAP control efficiency (%) 99% for HC1 * eff Calculations* 5% EDC Uncontrolled Emissions (Ey) = (2.54B-09) Q C h MW P T + 460 Uncontrolled Emissions (Ey) = (2.54E-09) (17.4) (996.384H7,42) L99) (14^7) ________(80) + 460 0.881 Mg/yr HAP Emissions (Ey^) = Ey (1 - eff/100) SL 026119 G-34 Source: HON subunit(s) Tri-Ethane II Process Unit CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (Ej^p) = 0.881 (1 - 5/100) 0.837 Mg/yr Weighted HAP Emissions = E^p Weighted HAP Emissions = (0.837) FHR (1) 0.837 Mg/yr Total HAPs Emissions* Total Weighted HAPs Emissions 0.837 Mg/yr 0.837 Mg/yr If the conditions during testing ere not representative of base year operation, make the appropriate extrapolation below and explain: N/A If the flow or concentration were not measured using an EPA reference method, SPA conditional method or validated using M thod 301, provide justification and supporting calculations: Concentration of gas was determined using a gas chromatograph with a thermal conductivity detector. Sample was taken from the vent into a syringe. The flow rate of the gas can be calculated as follows: gQfflPPnentg EDC HCL Uncontrolled Concentrations MPle/Jir PPMV 2.64 .0069 996,384 2,604 G-35 Source: HON subunit (s) Hri^Ethane II Process Unit. 1044 fP hr 17.4 JL min Vent temperature is 80F. "Expression provided in "Procedures for Establishing Base Year and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. See Attachment I for calculation. SL 026121 G-36 SUBUNIT: VENT 10: SCENARIO: DESCRIPTION: ATTACHMENT I TE-II 306 NON-ROUTINE NO. 2 OHC 8TARTUP SCRUBBER Q C h T MW P FHfl eft EU EHAP EW Average vent stream flow rate (ft3Anin) HAP Concentration (ppmv) Annual hours of operation (hrs) Vent stream discharge temperature (F) HAP molecular weight (Ib/lb-mole) Pressure at point of discharge (psia) HAP high risk weighting factor HAP control efficiency (%) Uncontrolled emissions (Mg/yr) Controlled emissions (Mg/yr) Weighted HAP emissions (Mg/yr) ; YEAR: 1987 EU - (2.54E-09xQxCxhxMWxP)/(T + 460) EHAP- EUx(1 - (fl/100)} EW - EHAPxFHR COMPONENT EDC HCL O 17.4 17.4 C 996,384 2604 h 7.42 7.42 MW 99 36 P 14.7 14.7 T 60 60 eff 5.00 99.00 FHR 1 1 EU 0.881 0.001 EHAP 0.837 0.000 EW 0.837 0.000 FILE: N17 TOTAL 0.881 0.837 0.837 Source: HOW subunit(s) Tri-Ethane II Process Unit_------------------------HAPs emitted: Ethvlene_ Dichloride (EPC1. Hydrochloric Acid (WgL) CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) HAP: Ethvlene Bichloride. _LED)----------- Year: 1987______________________________ Date: ftprU -11^- Calculator: S.R. Process Vent Identification: 306 _ (startup) Description: No. 2 OHC startup Scrubbed----------------------------------- Prgcess,-goaditi<2ng lag Date of flow measurement Method of flow measurement calculated1 Date of concentration measurement Method of concentration measurement (if not an EPA Method give a brief description and attach protocol) Svrinae Sample. Describe any problems encountered during testing None Identified Production rate during flow determination (lbs/hr) Production rate during sampling (lbs/hr) Average production rate during base year (lbs/hr) 1987 198?_ GC/TC 19.086 19.086 19.086 strain. charapfeeEistiss , Average vent stream flow rate . (ftJ/min) HAP concentration (ppmv) Annual hours of operation (hrs) vent stream discharge temperature (F) HAP molecular weight (lb/lb-mole) Pressure at point of discharge (psia) HAP high-risk weighting factor ________60.7 999.578_ __________5 5 ________80 ________99 ________14.7 __________1 _ Q C h T MW P FHR Coatcgl Control device Scrubber HAP control efficiency (%) 99% for _HC1_ _ - eff 5% EDC Calculations* Uncontrolled Emissions (Eu) = (2.54E-Q9) Q C h MW P T + 460 Uncontrolled Emissions (Ev) * (2.54E-091 (60.7J (999.578) 15.5) (99) QUA ________(80) + 460 2.283 Mg/yr HAP Emissions (E^) = Ew (1 - eff/100) 1See next page. SL 026123 G-38 Source: HON subunit(s) Tri-Ethane II Process Unit CALCULATION WORKSHEET FOR ESTABLISHING HAP EMISSIONS FROM PROCESS VENTS (SAMPLE) (CONCLUDED) HAP Emissions (Eh^) = 2.283 (1 - 5/100) 2.169 Mg/yr Weighted HAP Emissions = ehap Weighted HAP Emissions * (2.169) fhr (1) 2.169 Mg/yr Total HAPs Emissions* Total Weighted HAPs Emissions ** 2.169 Mg/yr 2.169 Mg/yr If ths conditions during testing are not representative of base year operation, make the appropriate extrapolation below and explain: N/A If the flow or oonoentration were not measured using an EPA referenoe method, EPA conditional method or validated using M tbod 301, provide justification and supporting calculations: Concentration of gas was determined using a gas chromatograph with a thermal conductivity detector. Sample was taken from the vent into a syringe. Flow rate of the vent can be calculated as follows: components EDC HCL Uncontrolled______________ REMV 9.23 .012 998,859 1,299 SL 026124 G-39 Source: HON subunit(s) Tri^Ethane II Process Unit 9.24 x (3S9 f54?^ ( hr ) { mole) V492 R 3641 hr 60.7 JL min Vent temperature is 80F.* * "Expression provided in "Procedures for Establishing Base Vear and Post-Reduction HAP Emission" to convert flow and concentration into an annual mass rate; the 2.54E-09 constant is based on the ideal gas law. *See Attachment I for calculation. G-40 ATTACHMENT I SL 026126 SUBUNIT: VENT ID: 8CENARIO: DESCRIPTION: TIE-11 SOS STARTUP NO. 2 OHC STARTUP SCRUBBER YEAR:1987 Q Average vent stream flow rate (ft3Anin) C HAP Concentration (ppmv) h Annual hours of operation (hrs) T Vent stream discharge temperature (F) MW HAP molecular weight (Ib/lb-mole) P Pressure at point of discharge (psia) FHR HAP high risk weighting factor ff HAP control efficiency (%) EU Uncontrolled emissions (Mg/yr) ; EU - (2.ME-09xQ xCxhx MWx P)/(T + 460) EHAP Controlled emissions (Mgfyr) EHAP - EU x (1 - (*11/100)) 0 EW Weighted HAP emissions (Mg/yr) ; EW - EHAP x FHR 1 COMPONENT EDC HCL o 60.7 60.7 C 996,859 1,299 h 5.50 5.50 MW 99 36 P 14.7 14.7 T 60 60 eff 5.00 99.00 FHR 1 1 EU 2.263 0.001 EHAP 2.169 0.000 EW 2.169 0.000 FILE: N18 TOTAL 2.284 2.169 2.169