Document MMvYKw469J7ro492j1KMkZEQV

Tenneco Chemicals A Tenneco Company P.O. Box 849 Pasadena, Texas 77501 (713)479-3411 Organics & Polymers Division September 3, 1974 Mr. Sam Crowther Texas Air Quality Services 8520 Shoal Creek Blvd. Austin, Texas 78758 Dear Sam: Enclosed with this letter are some data pertaining to VCM emissions from our New Jersey PVC plants which we are submitting for your information. Part A contains descriptions of the suspension and dispersion processes. The suspension process as described is very similar to the process we plan to use at Pasadena. I would like to call two points to your attention in the section headed Operating Efficiency. We have been able to make substantial reductions in monomer losses in the Burlington homopolymer process which we have used as a pilot operation. This has been done at the expense of product quality. The lower quality has resulted in customer complaints at a level which would be a matter of serious concern were it not for the general shortage oj rvu m the market. A second point of particular interest in attempting to extrapolate Burlington experience to the Pasadena plant is the initially high levels of loss at Burlington as compared to those anticipated at Pasadena -- 5.35% vs a maximum of 3%. We certainly anticipate some of the work at Burlington being applicable to Pasadena but we do not now think we can expect the same percentage of improvement at both plants. Part B describes several emission control systems in existence, being installed, or under study. Adsorption by activated carbon is covered in some detail. Even though pilot results to date are not encouraging in regard to carbon life, we are installing two full scale units at Pasadena as stated in our permit application. Tenneco believes the area monitoring systems being installed in all three of its plants will have a beneficial effect on pollution control by giving an early warning of any unusual fugitive emission and so lead to a generally higher standard of maintenance. COLORITE 008309 Mr. Sam Crowther September 3, 1974 Page Two The ambient air monitoring information in Part D is the same that we gave to the E.P.A. during their visit to Burlington on August 22, 1974. For comparison, losses to the air are approximately 15,000 lbs/day at Burlington (plant capacity at 150 million pounds per year) and 4,800 Ihs/day at Flemington (plant capacity at 80 million pounds per year). During the periods covered, Pasadena losses are projected to be about 4,800 lbs/day for comparison. If you have any further questions on these subjects, please do not hesitate to call on us. Yours very truly. TENNECO CHEMICALS, INC. WPA/cj m Enc. W. P. Anderson Director, Environmental Sciences COLORITE 008310 CONTENTS A. PROCESS DESCRIPTIONS - NEW JERSEY PVC PLANTS B. POLLUTION CONTROL DEVICES C. FUGITIVE EMISSION SOURCES D. AMBIENT AIR MONITORING INFORMATION COLORITE 008311 A. PROCESS DESCRIPTIONS NEW JERSEY PV'C PLANTS Tenneco currently manufactures two types of suspension rosin - hompolymer and copolymer - and dispersion resin in its New Jersey plants. A description of Lhese processes is given below: PVC Suspension Resin Suspension resin is manufactured by charging a weighed amount of recovered and virgin VCM into a reactor containing a metered amount of water, suspending agency and a peroxide initiator. In the case of copolymer, vinyl acetate is also added. Under automatic control, the batch is heated to a predetermined tempera ture at which time the exothermic polymerization reaction takes place. The batch temperature is maintained with cooling water until no further exotherm exists and the pressure starts to drop. At this point, the batch is transferred info a stripper vessel and any remaining VCM in the reacLor is drawn into the recovery system until a vacuum of 20 to 22" Hg exists in the reactor. This vacuum is broken with nibrogen and the reactor is washed out with water and made ready for the next batch. In the stripper, the unreacLed monomer is recovered until the stripper is at a vacuum of 20 to 22" Hg. Heat is applied by injection of live steam and further monomer is recovered. In the case of copolymer, vinyl acetate is removed from the exiLing vapor stream by a condenser before it reaches the compressors. This recovered vinyl acetate is then reused in subsequent batches. When stripping is complete, the batch is transferred inLo a blend tank where it is mixed with other previous batches. It is transferred as a slurry by pump to a solid bowl centrifuge where most of the water is removed. The wet cake drops from the cenLrifuge into a hot air dryer and is air conveyed as dry COLORITE 008312 A-2 resin inLo a eo.llect.or. This dried PVG or copolymer is then screened to remove coarse particles anti lumps and is then sent to bulk storage or to the bagging machines for bagging, palletizing and warehouse storage. The bulk product .is stored in silos until ready for shipment in either rail hopper cars or hopper trucks, PVC Dispersion Resin Dispersion resin is manufactured by first combining a weighed amount of water, emulsifier and recovered and virgin monomer in a batch mix tank which is supported on a scale mechanism. A quantity of peroxide initiator is added and after sufficient mixing Lime, the batch is pumped through a series of high pres sure pumps and orifices into the reactor. An exothermic polymerization reaction occurs and heat is removed over a period of Lwelvo to eighteen hours by circu lating cooling water. When the reaction is complete, as evidenced by a loss of pressure and absence of an exotherm, the batch is transferred to a stripper. Once empty, the reactor is evacuated to the recovery system and mosL of the monomer remaining is recovered. The reactor is then ventilated, opened and cleaned with high pres sure water. In the stripper, the residual vinyl chloride monomer is removed by the recovery system until a vacuum of approximtcly 22" Mg is reached. Further removal of monomer is effected by gradual heating. After stripping, the batch is trans ferred to the blend tank. Water is removed from the PVC by the rotary vacuum filters. The resultant wet cake is then introduced into a hot air stream and is dried to a moisture con tent below 1/. This very fine dry powder is collected in a standard bag-house Lype collector whereupon it is conveyed into a Mikro-Atomizer size reduction machine COLORITE 008313 A- ' Another collector separates this fine product from the air sLream out of the Mikro-Atomizers and delivers it to a blender where small amounts of her mute, are added. This finished product is then bagged, palletized and senL Lo the vji i house for storage and shipping. OPERATING EFFICIENCIES The efficiency of VCM utilization to saleable product varies as a function of the process with the dispersion technology practiced at Burlington being Lhe least efficient. Through the years efficiencies have been improved for all pro cesses, i.e., dispersion, suspension copolymer and homopolymer. Increase! util ization of VCM in suspension hompolymer at Burlington has been improved signi ficantly over 1973 as shown by Table I, attached. Some of this improvement is due to increasing the severity of stripping conditions whereby VCM is recovered and some, perhaps, to a better accounting for product. Equipment to permiL more efficient stripping of homopolymer at Lhe Flemington plant is being installed and is expected to be operational by October of this year. The more severe stripping of copolymer and homopo1ymers over the last months has resulted in a product with a lower VCM content, however, this treatment has had a deleterious effecL on product quality. Up to this point in time, we have had only a small number of shipments rejected by our customers for poor qual ity which is due to the shortage of PVC in the marketplace raLher Lhan product quality itself. Thus, we do not see our current stripping techniques as a long term solution to Lhe problem and significant R&D work to develop better techniques is currently underway. Stripping VCM from the PVC slurry in the dispersion plant has so far been unsuccessful as the latex produced in this process is relatively unstable. COLORITE 008314 TABU- I VCM OPERATING EFFICIENCY BURLINGTON HOMOPOLYMER BURLINGTON COPOLYMER BURLINGTON DISPERSION POLYMER FLEMINGTON HOMOPOLYMER LOSSES AS VCM*-1-* 1973 1974 3.82 2.27 2.61 2.46 3.68 3.39 3.33 - LOSSES AS PVC(1) 1973 1974 1.53 1.38 0.66 0.63 5.08 3.71 TOTAL LOSS 197 3 1974 5.35 3.27 3.65 * 3.OS) 8.26 7.10 1 . 59 4.92 - <'1'*All losses as pounds/100 lbs.. monomer charged. * Discrepancy is vinyl acetate loss. COLORITE 008315 B. POLLUTION C'l^'TROL devices There are two basic types of emission control devices used in the PVC manufacturing facilities at Tenneco. One type is installed only for dust control. The device used is a bag filter collector which has an operating efficiency of 99.9+%. The other caLgeory is condensation of VCM vapors via heat exchangers. Three prime factors must be highlighted when dealing with VCM in the PVC manufacturing process. 1. VCM is a compressed reactive gas 2. VCM is highly flammable in air 3. The process uses water as the polymer carrier. Because VCM is a compressed reactive gas, there are temperature and, therefore, pressure limits above which the gas cannot be properly handled without the hazard of reactions in the recovery system. Due to its inflam mability, it must be handled in nonoxygen-containing streams and, therefore, all recovery efforts must be prior to exposure to air. The fact that the pro cess uses water as a carrier tends to set a minimum temperature in the recovery system in order lo prevent freezing the water vapors in the heat exchangers. In order to keep the various streams and vessels from air contact, niLrogen is used as a pad and purge gay. This inert gas is processed through the VCM recovery system and due to its noncondensing characteristics, it musL be bled off in order not to build up excessive recovery system pressure. In the process of bleeding the nitrogen to maintain system pressure and temperature, some of the VCM vapors bleed off concurrently. Thus, we have the misnomer of monomer vent rather than the more accurate inert gas vent. COLORITE 008316 Proposed Techniques for VCH IEmission Reduction Tenncco is planning to install an activated carbon adsorption system in the new Pasadena PVC facility* for recovery of VCM from oxygen-free off-gas streams based on limited tests and data on activated carbon adsorption is given below. Other techniques which have been considered or seem promising for the future are: 1. More efficient stripping of monomer from the slurry, thus reducing VCM emissions from the dryer. 2. Use of condensible gases, such as steam, to purge vessels and piping between batches or prior to opening for maintenance. 3. Use of deep cryogenic condensation to recover VCM by 1iquification after drying. 4. Catalytic destruction or conversion of VCM in dilute streams. 3. CounLer-current scrubbing of VCM from off-gas streams with a low volatility VCM solvating agent. We have made preliminary calculations on the feasibility of removing the VCM contained in a PVC dryer outlet gas via absorption with a lean oil. Although such a system might be practical for oxygen-free streams, it was concluded that for the dryer outlet gas: 1. The system would be quite large and would have to be operated at several atmospheres pressure to allow practical lean oil rates. 2. Operating costs would be relatively high due to compression costs, heating and cooling and lean oil losses. 3. It would be a most dangerous operation which is Lhe most powerful argument against it even if it were economical. Although actual organic vapor concentrations would be well below the explosive range, there would always be areas of mist formation which could easily be ignited by static electricity or other ignition sources. *Under construction with expected start-up in late 1974 COLORITE 008317 Tile description oi the commercial activated carbon unit to be ins La I Ltd at Pasadena and its proposed application are presented in Table I. A photo graph of the unit is also attached. Termeeo has operated both laboratory and pilot plant activated carbon units for the recovery of VCM. The experimental results (laboratory) utilizing virgin VCM are attached as Tables II and III, and the results of pilot plant experiments using recovered vinyl chloride from a PVC pilot'plant in Flemington, New Jersey are attached as Table IV. The Tenneco pilot plant was the one referred to by the Calgon representative who testified at the OSHA hearings in Washington, D.C. The information presented in Table 1 shows Lhat 'he commercial application for activated carbon adsorption designed for our Pasadena plant is solely for the purpose of recovering, VCM from two small process streams which vent to the atmos phere and had posed a potential air pollution problem; that these streams have a composition in which air Is not a major constituent and VCM concentration is rela tively high (10-30 percent) and that no system has been designed to collecL am bient air in the Pasadena, or any other plant, and to remove low concentrations of VCM from such ambienL air. The experimental results with virgin VCM, Tables 11 and III, show that tests carried out for 19 to 21 cycles indicate some decrease in bed capacity with time. Preliminary extraction experiments on the used carbon showed no PVC to be present, however, additional chemical tests are underway. Further, data on surface area and pore size are being obtained to determine the extent of physical degradation of the carbon. Experimental results with a recycle VCM stream from Lhe PVC pilot plant containing 29 mol percent VCM for longer periods, 28 cycles, show bed capacity COLORITE 008318 was adversely affected as in the tests with virgin monomer, These data for a limited number of cycles east doubt on the commercial feasibility of using activated eat bon to recover VCM, particularly when a commercial unit must be capable of operating for thousands of cycles to be practical. These data also show that short periods of operation in the laboratory, 15 cycles or less, are not sufficient to demonstrate the long-term efficiency of activated carbon for recovering VCM. Laboratory and pilot plant tests are continuing and iL is hoped that perhaps other types of activated carbon or variations in the adsorption-desorption cycle can be developed which will give acceptable performance. AREA MONITORING SYSTEM Other equipment which is expected to be of great value in minimizing losses of VCM are the sequential area monitoring, systems that are being installed in the RurlingLon and Flemington, New Jersey PVC planL.s and the Pasadena facility. These instruments will provide essentially continuous monitoring of the working atmosphere in these plants. The systems are designed to give an audible alarm if the VCM concent, rat ions increase above a set level, and thus, afford an immediate warning of VCM leakage. This "real Lime" analysis will permit mechanical and operating corrections Lo be made immediately; something that is not possible with the personnel monitoring procedures now used throughout the industry. For the Burlington and FlemingLon plants, the gas chromoLography monitoring systems have been purchased from Bendix. Sampling frequency at any COLORITE 008319 -5- location will bo every 10-15 minutes with an accuracy of j_ 0.5 ppm VCM in the range of 0-50 ppm. Samples arc to be taken at 90 points at the Burlington PVC facility and 35 poinLs at the Flcmington pJanL. Both units are scheduled to be operational by early November. AUTOMATED REACTOR CLEANING SYSTEM The development of an automated reactor cleaning system will measurably reduce emissions of VCM, particularly if such cleaning can be done without having to open the reactor between batches. Currently, Tenneco is evaluating the use of the Goodrich "HRC" high pressure water cleaning, system and sol vent cleaning for use in the New Jersey plants. Prototypes of automated cleaning devices have been built and tested at the Pasadena site, however, the effectiveness of this sytem will riot be known until Liu: Texas plant is in operation later this year. COLORITE 008320 TABLE 1 COMMERCIAL ACTIVATED CARBON UNIT DESIGN CONDITIONS The activated carbon unit to be installed in Tenneco Chemicals, Inc. Pasadena Polyvinyl Chloride facility is designed to recover vinyl chloride monomer (VCM) from two small process streams. Data con cerning these streams and proposed conditions of operation of the activated carbon unit are given below: Slurry Tank Vent Design Conditions Flow (SCFM) Pressure (psig^ Temperature ( F) 58.3* 2 60 VCM Condenser Purge 1.1 2 AO Composition (Mol. 7Q VCM Nitrogen Oxygen Water 10.6 75.2 1A.2 28.9 6A. 3 6.6 0.2 *This flow occurs 15 minutes every 2.6 hrs. Operating Cycle Step Adsorption Steam (10 psig 2A0F) Hot Nitrogen Purge (300F) Cold Purge (70F) Time (minutes) 180 60 A0 80 Flow Rate (SCFM) -- 350 800 800 Direction of Flow Down Up Down Down Unit Specifications Two (2) - A ft. I.D. vertical beds witli a packed height of ten feet. Activated carbon to be Pittsburgh Type BPL manufactured by the Calgon Corporation, Pittsburgh, Pennsylvania. Skid mounted adsorption unit manufactured by Chemical, Design, Inc., Lockport, New York. COLORITE 008322 TABLE II ADSORPTION OF VIRGIN VINYL CHLORIDE MONOMER ON ACTIVATED CARBON EQUIPMENT - Steel pipe, 1.61" ID packed with Pittsburgh Type BPL 4 x 10 mesh activated carbon manufactured by the Calgon Corporation, Pittsburgh, Pa. Packed height of bed 5'2". EXPERIMENTAL CONDITIONS - Virgin vinyl chloride (VCM) manufactured by Shell Chemical Company, Houston, Texas mixed with air to give a gas com position of 29 mol percent VCM and 71 mol percent air was fed to the activated carbon bed at a nominal velocity of 29 feet per minute at ambient temperature (70 F) and pressure. Step Adsorption Steam Desorption (20 psig 0.6 Ib/min) Nitrogen Drying (250F)(0.3 CFM) Time (Min.) (2) 20-30 60 60 Direction of Flow Downward Upward Downward Cvcle Number 1 3 Jr 7 9 11 ]3 13 17 19 21 Bed Capacity (lbs VCM/lb Carbon) 17.8 (1) 16.7 (1) 20.0 (1) 18.6 (1) 21.3 21.3 22.0 18.1 19.4 14.9 13.6 ^'^Concentration of VCM and gas velocity varied during first seven cycles. (2) Time varied since adsorption step terminated when VCM breakthrough occurred. Carbon Analysis - After 21 cycles the used carbon was removed from the unit and extracted with THE. The THE extracL gave 0.1] weight percent liquid which on analysis proved lo be a phenolic compound, however, no PVC was found to be present. COLORITE 008323 TABLE HI ADSORPTION OF VIRGIN VINYL CHLORIDE MONOMER ON ACTIVATED CARBON EQUIPMENT - Steel pipe, 1.61" ID packed with Pittsburgh Type BPL 12 x 30 mesh activated carbon manufactured by the Calgon Corporation, Pittsburgh, Pa. Packed height of bed 5'2". EXPERIMENTAL CONDITIONS - Virgin vinyl chloride (VCM) manufactured by Shell Chemical Company, Houston, Texas mixed with air to give a gas composition of 29 mol percent VCM and 71 mol per cent air was fed to the activated carbon bed at a nominal velocity of 29 feet per minute at ambient temperature (70 F) and pressure. Step Time (min.) Adsorption 20 - 30 (2) Steam Desorption (20 psig,0.6 lbs./min.) Nitrogen Drying (250F) (0.3 CIM) 60 60 Direction of Plow Downward Upward Downward Cycle No. 1 3 6 7 9 J1 .13 13 17 19 Bed Capacity (lbs. VCM/Ib. Carbon) 21.9 22.1 19.1 2 A. 1 19.0 20.6 22.2 20.6 16.7 18.2 (1) (1) (1) (1) (1) Concentration of VCM and gas velocity varied during first 7 cycles. (2) Time varied since adsorption step terminated when break through occurred. Carbon Analysis - After .19 cycles, the used carbon was removed from the unit and extracted with THF. The THE exLeacL gave 0.16 weight percent liquid which on analysis proved Lo be a phenolic, compound, however, no PVC was found to be present. COLORITE 008324 TAB IT IV ADSORPTION OF RECOVERED /INYL CHLORIDE MONOMER ON ACTIVATED CARBON EQUIPMENT - Steel pipe, 1.61" ID packed with Pittsburgh Type BPL 4 x 10 mesh activated carbon manufactured by Lhe Calgon Corporation, Pittsburgh, Pa. Packed height of bed 5'2". EXPERIMENTAL CONDITIONS - Vinyl Chloride Monomer recovered from a pilot plant polymerization reactor in Flemington, New Jersey having, a gas com position of 29 mol percent VCM and 71 mol percent air was fed to the activated carbon bed at a nominal velocity of 29 feet per minute at ambient temperature (70 F) and pressure. Step Adsorption Steam Desorption (20 psig 0.6 Ib/inin) Nitrogen Drying (250F), (0.3 CFM) Time (Min.) 20 - 30 (1) 45 - 120 60 Cycle Number Bed Capacity (lbs. VCM/lb. Carbon) 1 19.4 3 15.1 5 18.7 7 15.1 9 18.7 11 18.0 13 17. 3 15 18.4 17 14.4 19 18.0 21 12.2 23 11.2 25 9.8 27 b. 1 28 8.3 Direction of Flow Downwa rd Upward Downward Steam Desorption Step (min.) 45 45 70 45 75 /5 75 75 100 100 1 10 120 120 120 120 Time varied since adsorption step terminated when VCM breakthrough occurred. Carbon Analysis - After 28 cycles the used carbon was removed from the unit and examined. There! was no visible evidence of PVC on the carbon or change, in carbon color. The carbon was extracted with THE and the extract gave 0.06 weight percent liquid which on analysis proved to be a phenolic compound, however, no PVC was found to be present. Unused carbon extracted with THE yields 0.06 weight percent of liquid of simi lar type as the used carbon. COLORITE 008325 C._FUCri'_lVF FM_[SS10N S0I1RCFS The1 iugitive (.'`missions from the I'V'C' jo 1 111_arc exl rrau' I y diflrcult to estimate since a sufficiently accurate material balance, has not as yet boon developed. The potential poinLs of fugitive emissions, however, are in the main known and a number of Lhese have been chocked at the New Jersey plants to determine the general extent of leakage. These potential points and operations are connecting and disconnecting of VCM tank cars, opening, of Liu reactors and strippers beLween batches, leakage at compressor packing and pump seals, and leakage at valve stems. Other areas whore leakage can occur are at safety valves and flanged -joints and during sampling and Lank level gauging. Periodic chocks at valves and flanges with a Cenlurv Flame Ionization Detection unit capable' erf detecting levels of VCM oi 2 ppm has shown that .id e.quaLe 1 y maintained valves and flanged .joints show no detectable leakage. Flanges near pumps and other vibratory equipment, however, need attention to maintain a no-leakage condition. Compressor seal leakage, opening of reactu and sLrippers and operations associated with unloading VCM tank cars are be 1 ieve.d to be the major causes oi iugitive emissions. Cost Aspects of Pollut ion Control Devices A review of the construction cost of the New Jersey PVC facilities was made to determine the cost of installed pollution control devices. At the Flemington plant, built in 1 957 , $448,000 was spent at that time for bag, lurut other dost control equipment and a monomer vent condenser. Tn 1973, a fluid bed dryer was installed at this site and associated bag collectors, cyclones, etc. required an investment of $48,000. COLORITE 008326 c; i The cuyo ] vincr plant at Burlington was constructed in 1962 nl wtiicii Lima $610,000 of the total plant investment was spent in Llie area o! dust control and VCM recovery, In 1964 the plant was expanded with the equipment installed then currently in suspension homopo 1 ymer production. Cost of omis sion control items installed at that Lime was $895,000. Investment in pol lution control equipment installed in the dispersion planL at Burlington in 1964 was $719,000. An ex pension in 1969 of the dispersion plant required $1,100,000 lor such equipment. As indicated in an earlier section of this report, it is planned to install an activated carbon adsorption unit at the 240 million pound per vent PVC plant now being constructed at Pasadena, Texas. The cost of tills unit installed is projected at $300,000, however, actual operating costs arc not available as vet.. Preliminary and very rough estimates of capital requirements ior sub stantial reduction of emissions beyond the reductions already accomplished oi demonstrated are in the mu 1t i-mi 11ion dollar range. hstim.itcs are subject to variation based on technical feasibility and requirements of other agencies, such as those of OSHA. COLORITE 008327 AMJi I_Fr1N'L_AT_R _M0N_1 TORINC l NF(J KM\T_I ON A". cacn ui Lhe two polymer plants a sc r i us ot samp ! i up, poinLs .iroun.i the plant perimeter were selected and sets ot grab samples were taken at these points startin'', in early April. Date for the period April 2 through August, lb are present! ed in the following Lables: Al the initiation of Lhe sampling program, the gas ehromoLograpliit: method used for VCM analysis was felt to be sensitive to 0.5 ppm V/V basis. However, with experience and refinement of Lhe technique, it is now believed sensitivity is 0,1 ppm V/V basis. Tn approximately ninety percent, of the samples, the VCM coneent rat i on teas below Lhe detectable level. AtLaehed tire the (ol lowing: 1) Plot plan of the Burlington plant; 2) Tabulation of the data at the Burlington plant; 3) Plot plan of the Fleming,ton plant; and 4) Tabulation of the data at the Fl.eming.ton plant. Additional in 1 o rma t i on on '1 enncco sampling, and analvt ieal methods is given below: All samples were grab samples taken in a standard glass 500 ml. gas burette fitted with a septum. Samples were collected bv drawing, air at 2 I,/min. through the burette tor 5 minutes, then closing, the stop cocks. Samples tor analyst's were withdrawn through the septum using, a syringe. Analyses were carried out using a liewlel L-Packard Model 810 (las Chroma tograph or equivalent with a hydrogen 1 lame ionixaLion detector. The chroma tographs were fitted with 1/4" x 2M columns [lacked with 15% V-Con 550X-LB on Anakrom ABS, 60-8 mesh. Columns were held at ambient temperatures. Flame hydrogen flow at 10 psig pressure was 30 m]/min. Helium carrier gas flow was 60 ml/min. at 50 psig. Sample size, was 5.0 ml. COLORITE 008328 COLORITE 008329 COLORITE 008330 SAMPLING POTXT VIXD DIRECTION1 1. Office Parking Lot 2. Catalyst weigh Shack 3. North Gate 4. Railroad Gate 5. Fence Near CPD, Plant 6. CPD. Plant Gate 2. in Gate SIT.lTXGTPX PLANT SITL CICO - PPM 5 'll 5 /22 Stj .5/2. sw 5/28 XX 5/30 5/31 a 6/_3 5 J 4,0 XD 0.5 XD XD XD 3.0 XD XD XD 0.8 XD CD XD 1.9 XD XD 1.0 4.7 xd t:d XD XD XD XD XD xd ;;d XD XD XD 0.5 XD ::d xd XD ND XD XD XD xn 0.5 XD XD XD 0.5 XD TXCTZD ( 0.5 P?X) 6/6/74 F.W.K. COLORITE 00833 --1. . ? -ki ad r 10 4 ire *1: Office Parking Lot 0.2 ' e i-M . t Oiite c .I Railroad Oate icr.co- Near I'-pd. pit. M ate 1 i0 -ii-' 1 ,e 1 If i '" or' ' 1-t 3 0,1 2-5 5 2-i n 0-1 5 2.: 1.3 0.2 0.1* \tj nd o.T i.2 1*7 \d \|j \r - M' " C1.-. \[. 1 * '.2 Kl 0.4 rt.`r 1.0 2.2 0.2 Mi Mj M 1.2 - 1. 3 1.' CM 1.1 0.7 2.2 0.3 Mi M M :'.'J 0.4 0,3 \p 0.2 M: 0.3 1.4 Ml Mj Ml _l^__ +vt~ ~ * - tD Mi Mj . J 11 - 'i.l,' 2*0 1. 0 ;. 1 0. 'J ,11 Mi ' [' ' rf ci, ' 2.o 1.M 0.1 1.3 0.1 O.o o.l .!' ,0 iion i-;j>ro\ed .ce last report * ~ ;T>r T ~ J" i r6 i V . I r~i I y <s' ( i * i Fv L A c T0c PV V. Sui LOl O > a > T a r< r. A A C m \ S V OJ^AG C ' > ^ K `j COLORITE 008332 ------- p: e'~7T:tt^ t tj Lu 1 .C P ~Di N . __________________________________ Fl E H i O C. T 0 0 pc {_ / i, -i ft P L 0 ). SITE PL- P f tK(JcCO CnEh: -- 1; L tJ C . Ja /,< SAMPLING POINT l'-T IN D DIR C C 710 N V'CM IN AMBIENT AIR - FLI!MTNGTON PLANT SITE V'CM PL TECTED - PPM A/2 -1 ) `1 5/8 5/22 5/23 5/24 5/30 6/1 ~6~ /3 1. R & D Parking Lot, South Corner 2. R & D Parking Lot, North Corner 3. Rail Car Unloading Area 4. Fence Behind Reactor Bldg. 5. Fence Near Settling Ponds 6. Bushkill Creek Behind Catalyst Freezer Bldg. 7. Area Behind Storage Pjldg, 8. Fence In Front of Prod. Office 0.5 NO NO ND ND ND ND ND ND -- -- -- ND ND ND ND ND ND 3.0 0.8 ND 1.1 ND ND -- NT) ND NO ND ND ND ND ND ND ND 1.4 ITT. ND -- ND ND ND ND !-J ND 1.0 ND -- ND ND ND 0.5 ND ND NO VT> ND ND ND ND -- -- -- 00 -- -- ND ND _ _ ND ND nd = nine detected (<0.5 ppm) COLORITE 008333 6/6/74 F.v; ,K. . L'J COLOR!TE 008334