Document Qk9zj6d6Zwq1OoY5E3qrQo3ER

(conoco) Interoffice Communication To R. C. Checksfleld, Houston, Texas From L. W. Cresswell, Ponca City, Oklahoma Doi Subject October 2, 1978 Waste Water Treatment Revisions Design - Ethylene feedstock Project Expansion Case - Lake Charles Refinery Attached is a process design for revisions to the existing refinery waste water treatment facilities to accommodate the Ethylene Feedstock Expansion Case. The design calls for a new Intermediate waste water holding tank for high flow rate. Intermittent streams, and a dissolved air flotation unit to remove oil and solids prior to biological treatment. The projected effluent levels for the EPS case Indicate a serious problem with meeting the most lenient of expected NPDES permits without the Instal lation of this pretrestment equipment. The expansion will cause a 35 per cent Increase in hydraulic loading to the activated sludge unit, coupled with an 60 percent increase in raw waste organic loading. The presently oversized activated sludge unit will become fully loaded for the E7S case. Please direct your comments or questions to us by October 9, 1978, or we will assume that the design is accepted as Issued. Lewis W. Cresswell Senior Process Engineer Engineering Services Division Process Engineering Department mdn Encs CC 4- Encs LDWrAJM:CDS:RGG PHS:LAE:TR?:RLG.*VLC G. A. O'Brien, Westlake, Louisiana J. F. Walker, Los Angeles, California R. B. Wodnik, Westlake, Loulslana(3) D. M. Wolfe, Westlake, Louisiana R. J. Kozacka, Houston, Texas T. M. Bohn, Houston, Texas F. E. Rosenberger, St, Louis, Missouri J. L. Young, Alvin, Texas C. H. Lagow, Alvin, Texas C. W. Smelling, Alvin, Texas SHE0000Q0Q72 TABLE OP CONTENTS WASTK WATKK TKJWimNT m-'.VIS IONS ETI1YI,KNB FEEDSTOCK PROJECT - EXPANSION CASK LAKE CHARLES REFINERY List of Tables...................................... .... .................................................................................ii List of Drawings. .................................... Ill Design Basis I. II. III. IV. V. Background................................................ *.................................................................. Projected EFS Raw Waste Levels......................................................................... Projected EFS Case Final Effluent Vs. Discharge Permit. ... New Intermediate Holding Tank.......................................................................... Activated Sludge Feed Pretreataent................................................................ 1 2 2 3 3 Process Description I. Intermediate Holding Tank .........................................................................................12 II. Dissolved Air Flotation Unit.................................................................................... 13 III. CPI Lift Station......................... 15 Work List I. Intermediate Holding Tank......................................................................................... 16 II. Dissolved Air Flotation Unit.................................................................................... 17 III. CPI Lift Station.......................................................... 20 Equipment Specifications............................................................................................... . 21 Piping Schedule...................................................................................... .... ............................ 38 Instrument Specifications ................................................................................................ 41 Drawings i SHE000000074 LIST OF TABLES WASTE WATER TREATMENT REVISIONS ETHYLENE FEEDSTOCK PROJECT - EXPANSION CASE LAKE CHARLES REFINERY Table I -page - Current Waste Water Effluent........................ .... ............................ . 7 Table It - Biological System Feed......................................................... 8 Table III - Projected Future Effluent Values........................ ...... 9 Table IV - Predicted DAF Performance.......................... ......................................... 10 Table V - Projected NPDES Permit for EFS Expansion................................................ - . . . . .............................. 11 ii SHE000000075 LIST OF DRAWINGS WASTE WATER TREATMENT REVISIONS ETHYLENE FEEDSTOCK PROJECT * EXPANSION CASE LAKE CHARLES REFINERY Drawing Number SD-2568-42-116-L SD-2568-42-118-L SD-256B-42-U9-L SD-2568-42-120-L SD-2568-42-121-D SD-2 568-42-122-C SD-2568-83-1-C SD-2568-83-2-B SD-2568-83-3-B SD-2568-89-6-B Title Process Flow Diagram - Wastewater Treatment Facilities - Ethylene Feedstock Project Expansion Case - Lake Charles Refinery Process Flow Diagram - Wastewater Treatment Facilities - Ethylene Feedstock Project Expansion Case - Lake Charles Refinery Plot Flan - Wastewater Treatment Facilities Ethylene Feedstock Project - Expansion Case Lake Charles Refinery P&I Diagram - New Dissolved Air Flotation Unit - Ethylene Feedstock Project - Expansion Case - Lake Charles Refinery P&I Diagram - Tie-Ins for T-2603 - Ethylene Feedstock Project - Expansion Case - Lake Charles Refinery P&I Diagram - CPI Lift Station - Ethylene Feedstock Project - Expansion Case - Lake Charles Refinery S-2601 - Dissolved Air Flotation Feed Sump Ethylene Feedstock Project - Expansion Case Lake Charles Refinery S-2602 - Sludge Sump - Wastewater Treatment Revisions - Ethylene Feedstock Project Expansion Case - Lake Charles Refinery S-2603 - Slop Oil & Solids Sump - Wastewater Treatment Revisions - Ethylene Feedstock Project - Expansion Case - Lake Charles Refinery T-2601 - Flocculation Tank - Wastewater Treatment Revisions - Ethylene Feedstock Project - Expansion Case - Lake Charles Refinery ill SHE000000076 SI>-2568-89-7-B SD-2568-93-3-B SD-2568-95-4-B T-2602 - Polyelectrolyte Dilution Tank Ethylene Feedstock Project - Expansion Case - Lake Charles Refinery T-2603 - Intermediate Holding Tank - Ethylene Feedstock Project - Expansion Case - Lake Charles Refinery T-2603 - Dike Detail - Wastewater Treatment Revisions - Ethylene Feedstock Project Expansion Case - Lake Charles Refinery iv SHE000000077 DESIGN BASIS WASTE WATER TREATMENT REVISIONS ETHYLENE FEEDSTOCK PROJECT - EXPANSION CASE LAKE CHARLES REFINERY Background The Lake Charles Refinery's waste water effluent is currently meeting the limitations specified by Its existing NPDES permit. Table I shows a comparison of refinery monthly average effluent data to existing pcrmLt values for the period of January, 1977 through May, 1978, Even nL the higher 95 percent probable levels, all parameters were in com pliance except for total chromium. Chromium permit levels were exceeded on two occasions due to inadvertent discharges into the sewer. Better housekeeping practices In the future should prevent continued chromium violations. Although the existing discharge permit is being met, the refinery is currently encountering problems in the operation of the waste treatment facilities. The major sources of these problems are: 1) Large flow surges through the treatment system due to various intermittent discharges. 2) High oil concentrations in the Activated Sludge Unit Feed. At present these problems cause the treatment system to experience up sets. Oil builds up In the biological floe of the activated sludge unit, which reduces the treatment efficiency. The high oil level also reduces oxygen transfer and causes solids carryover in the clarifier. Nevertheless, the overall system currently produces a good effluent which easily meets permit values as a result of: 1) The activated sludge unit (ASU) is oversized for the present loading. Therefore, the unit is able to "limp through" upsets caused by high oil levels. 2) A large partially aerated lagoon followed by a dissolved air flo tation unit downstream of the ASU do a good job of polishing the ASU effluent. The present surges in raw waste flow are caused by intermittent dis charges from three major sources. The coker blowdown pond is periodi cally pumped down at a rate of 200 gpm. Ballast water is also occasionally received from the dock facilities at a rate of 200 gpm, and water draws from the crude tankage in the east and south tank farms can be received at rates of 200 gpm and 160 gpm, respectively. These sources often contain large quantities of oil which can overload the API and CPI separators and end up in the ASU. -1- SHE000000079 Data from the refinery indicates oil concentrations of up to 250 mg/1 can occur in the ASU feed. Generally, 50 mg/1 of oil is considered to be the maximum oil concentration that should be fed to a biological system. At oil concentrations above 50 mg/1 in the waste water, the oil accumulates in the biosludge to a high level which reduces bio efficiency. Oxygen transfer to the waste is also significantly re duced. If insufficient oxygen is transferred to satisfy the require ments for BOD reduction, anaerobic conditions occur. The result is poor effluent quality and increased loading on the final treatment. Theoretically, the existing 4-25 HP surface aerators in the ASU should be able to transfer 210 lbs/hr of oxygen to the waste under normal conditions, this is sufficient oxygen for treatment of the current 95 percent probable BOD loading to the ASU of 3,695 lbs/day. However, current data from the refinery indicates a dissolved oxygen (00) level of zero in the ASU 10 to 15 percent of the time. DO levels approaching zero Indicate Inadequate oxygen supplied for BOD reduction. II. Projected EFS Raw Waste Levels Implementation of the Ethylene Feedstock Project will result in the expansion of the Lake Charles Refinery to include primarily a new 30,000 BPSD FCC, a new 105,000 BPSD crude unit, and a sulfuric acid plant. As a result of the expansion, the average flow to the biological treat ment facilities will increase from 616 gpm to 835 gpra. The predicted raw waste contaminant loadings for the expansion case are shown in Table II, column 1. The large increase In BOD loading is primarily due to additional desalter water from the new crude unit. For the EFS case, the stable operation of the ASU will become more critical to the overall efficiency of the waste water treatment facili ties due to the increased flow and contaminant loadings. Modifications must be made to the system to eliminate the frequent upsets of the ASU seen in the past. The final effluent flotation unit alone will not be able to adequately treat a poor ASU effluent to meet the projected future discharge permit. III. Projected EFS Case Final Effluent Vs. Discharge Permit Table V shows the maximum expected NPDES permit values in column 2 for the case of a direct scale-up of the existing permit based on crude throughput. Since the Lake Charles Refinery discharges to a water quality limited stream, there is a chance that the existing permit will not be changed for the expansion case. However, until Conoco enters into negotiations with the EPA for a new permit, it would be safe to assume that the maximum expected permit values will be the higher values in Table V. -2 - SHE000000080 Predicted EPS case final effluent concentrations without pretreat ment are shown in Table III. The effluent was predicted, assuming no changes were made to the overall treatment scheme. As can be c< 'it, tin- cx|)('i't<'d max f mutii t'Criuenl' perm 11 value's (most li,nl>,nl valm*) cannot be met unless a pretreatment dissolved air notation unit is installed. IV. New Intermediate Holding Tank The most practical method of eliminating the raw waste flow surging problem appears to be the installation of an intermediate holding tank. The new tank would collect water from the coker blowdown pond, the tank farm water draws, and the ballast water tank. Some oil separation would take place in the tank with the water discharging to the API at a controlled rate. A 10,000 bbl capacity tank with an internal floating roof tank has been specified for this service. The floating roof will be required to satisfy State Air Baission requirements for oil water separators. The tank was designed to handle approximately 3,000 bbl of water from the coker blowdown pond and the tank farm water draws. Each source will be received at a rate of ^200 gpm. The additional 7.000 bbl of capacity will be needed to handle ballast water from the dock facilities. Since the dock facilities occasionally have 15.000 bbl of water that must be processed, it will be required in the future to control the rate at which this water is sent Co the holding tank. This can easily be done due to excess capacity of the dock facilities tankage and the fact that ballast water is only received at an average of 15,000 bbl every two weeks. Oil, water, and sludge will be drawn off the new holding tank at various levels by a series of discharge lines spaced at Intervals on the side of the tank. The water will be sent by flow control to the API separator at a normal rate of 80 gpm, while the oil will be periodically drawn off manually and pumped to slop treatment. The slop pump and spare have been specified for a rate of 60 gpm each to allow oil pump down in approximately 3 hours under normal condi tions. V. Activated Sludge Feed Pretreatment A. Introduction The problems of high oil concentrations in the ASU feed and supplying sufficient oxygen to the ASU for BOD removal must both be solved for the expansion caae. The only feasible solution appears to be pretreatment of the ASU feed. - 3- SHEQQ0000081 Tin- 95 piTiiiH. probable HOI) I nail in?', id the ASU .lftor tin- expan sion without Teed pretreatment Is predicted to he 6,556 ibs/day. The oxygen required to process this BOD loading is 350 lbs/day, an increase of 140 lbs/day from the 210 lbs/day presently sup plied. The additional oxygen could be supplied by adding more aeration to the ASU, but this would not eliminate upsets from high oil concentrations. Pretreatment of the feed to a biological system for oil and solids removal is the best method of ensuring stable operation of the system. Pretreatment of the ASU feed with dissolved air flotation would eliminate both the oil and oxygen transfer problems. B. Pilot Tests Dissolved air flotation pilot studies were conducted on the Lake Charles Refinery CPI effluent in the early 1970's. The pilot dis solved air flotation unit yielded a consistently good effluent. Flotation treatment of the ASU feed would greatly Improve the operation of the ASU by removing the oil and suspended solids. This would raise the active fraction of micro-organisms in the ASU mixed liquor. Research studies performed on the ASU in the early 1970's indicated that pretreatment with dissolved air flotation would also greatly improve the oxygen transfer efficiency in the unit. The experi mental data indicated that the alpha value (the ratio of oxygen transfer coefficient in the waste to the that of pure water) would be increased from 0.67 to 0.95 with flotation. This would enable the existing aerators In the ASU to supply 290 lbs/hr of oxygen to the waste. Since a sizeable portion of the suspended BOD will be removed by flotation, the 95 percent probable BOD loading to the ASU will be reduced from 6,556 lbs/day to 4,875 lbs/day. This lower BOD level will require only 260 lbs/hr of oxygen which can easily be transferred by the existing aerators after feed pretreatment. C. Dissolved Air Flotation Unit Design Basis The new dissolved air flotation unit (DAF) will be located vest of the existing CPI and will treat the CPI effluent water. The DAF effluent will then be pumped to the existing equalization section of the ASU. The normal design flow to the new DAF after the expansion will be 495 gpnu The 491 gpm effluent from the DAF will combine with 340 gpm of cooling tower blowdown to give an average flow of 831 gpm to the ASU. By installing the new intermediate holding tank, the flow rate to the new DAF should be relatively constant except during storm conditions. - 4- SHE000000082 Tht* maximum flow during storm conditions to the new DAF will he limited to 1*100 gpm In the expansion cose l>y limiting the feed pump discharge rate. Any excess over 1,100 gpm will back up the sewer to the CPT and switch on the existing storm water diversion pumps, as presently occurs with the existing system. The OAF effluent will combine with 340 gpm of cooling tower blowdown to give 1,440 gpm of feed to the A5U during storm conditions. Currently, the ASU processes approximately 1,200 gpra under maximum storm conditions. The ASU will process the same amount of storm water after the expansion, with the Increase in flow due only to an increase in process water. 1. Flotation Performance The projected feed to the new dissolved air flotation unit was estimated based upon probability plots of contaminant levels from recent plant data (January, 1977 to Hay, 1978) plus predicted effluents for the new units Included in the expansion. The ex pected dissolved air flotation unit performance during normal and storm conditions is summarized in Table IV. Only the critical feed parameters affected by flotation are shown. The perfor mance of the unit was predicted based on dissolved air flota tion pilot tests previously conducted on the CPI effluent. 2. Chemical Requirements The previous pilot test results indicated that the solids re moval efficiency of a dissolved air flotation unit on the CPI effluent was enhanced with proper chemical treatment. Often both a coagulant (alum) and a flocculant (polyelectrolyte) are used for chemical treatment. However, the pilot test results indicated that 6 ppm of a cationic polyelectrolyte alone gave the best results. Eliminating the alum will bene fit the operation of the unit by simplifying the chemical feed system and also reducing the sludge production associated with the alum solids. The cationic polyelectrolyte (Nalco 603) will be diluted to a 10 weight percent solution in water before addition. The polyelectrolyte dilution tank was specified to provide a 7-day supply of chemical at normal flows. The chemical will be added by proportionating pumps which are controlled by the DAF feed pump flow. The polyelectrolyte will be added to the waste upstream of the flocculation tank. The flocculation tank will provide a reten tion period for the formation of floe. The tank was sized to allow approximately 10 minutes retention time, since pilot tests indicated 5-15 minutes retention Is required for formation of a good floe. Good flocculation will significantly increase the flotablllty of the solids. -5- SHE000000083 3. Flotation Cells I'loL.il Inn ml Is .tr` nn rmal I y sized to give .in overflow r.Ue (Including recycle) .-it normal How of 1.3 to 2.3 g|W*<| I'l. However, due to high oil and solids loading in the feed and the large increase In flow during storm conditions, a slightly more conservative overflow rate has been used for this design. The flotation cell was specified as a 25-foot diameter tank with overflow rates of 1.36 and 3.02 gpm/sq ft at the normal and storm flows. The volume of the tank specified will allow sufficient retention time for the air to contact the solids (floe) and float them to the surface. 4. Recycle Saturation System The recycle saturation system. Included as part of the flota tion cell package, will provide the necessary air to float the solids to the surface of the flotation cell. Air and a portion of the flotation cell effluent will be contacted in the satura tion column at about 65 psig (80 percent saturation efficiency). Air in the recycle stream will be released in the flotation cell by depressurization through a specifically designed back pressure control valve. Excess air (25 percent) will be pro vided to the saturation column to keep the system purged of nitrogen which is less soluble in water than oxygen. The re cycle rate will be maintained at about 35 percent of the feed rate by flow ratio control. 5. Sludge Handling System The floated solids and oil will be skimmed from the flotation cell as an approximately 4 weight percent solution. This high concentration will be achieved due to the large amount of oil and solids in the feed. The float will then gravity flow to the sludge sump where the concentration will be increased by settling to a 5 weight percent solution. The size of the sump was specified to provide 3 days of sludge storage at the normal rate. The 5 weight percent sludge will be removed by vacuum truck for disposal. -6- SHE000000084 TABLE I CURRENT WASTE WATER EFFLUENT LAKE CHARLES REFINERY Parameter BOD5, lb/day COD, lb/day TOC, lb/day TSS, lb/day NIJ'J, lb/day Oil and Crease, lb/day Phenol, lb/day Chromium, lb/day(2) Sulfide, lb/day Monthly(1) Average 50% Probability 130 675 195 185 53 28 0.28 2.1 .047 Monthly(l) Average 95% Probability 275 1,600 325 340 150 72 0.7 6.0 .08 NPDES Permit Dally Average 320.0 2,500.0 760.0 420.0 1.70.0 136.0 2.0 5.0 3.4 NOTES: (1) Based on values reported during the period from January, 1977 through May, 1978 for both the process lagoon and flrepond discharges combined. (2) Compliance has been met 92 percent of the time. Violation of the permit limi tation values occurred on two occasions due to Inadvertent discharges into the process sever. - 7- SHE000000085 TABLE II BIOLOGICAL SYSTEM FEED LAKE CHARLES REFINERY Parameter bod5 , 50% Cli/Day) Probable boo5 , 95% (Lb/Day) Probable Oil, 50% (Lb/Day) Probable Oil, 95% (Lb/Day) Probable TSS, 50% (Lb/Day) Probable COD, 50% (Lb/Day) Probable Flow , (GPM) Current Feed 1,551 3,695 237 1,857 2,811 5,231 616 PROJECTED FUTURE FEED W/0 DAF W/DAF 2,816 6,515 319 2,505 2,010 7,691 835 2,101 4,875 177 295 335 - 831 - 8- SHE000000086 TABLE III PROJECTED FUTURE EFFLUENT VALUES LAKE CHARLES REFINERY Parameter BOD5(3) C0D(3) TSS(4) Oil & Grease(5) Phenolic Compounds(5) Ammonia (as N)(6) Sulfide(5) Total Chromium(7) TOC(3) REFINERY EFFLUENT. 30--DAY AVERAGE LBS/DAY W/0 ASO FEED PRETREATMENT(1) W/ASU FEED PRETREATMENT(2) 502 952 502 952 Probable Probable Probable Probable 311 1,617 237 34 0.34 96 0.06 2.6 467 808 4,697 534 88 0.86 135(8) 0.10 5.9 953 185 946 237 34 0.34 96 0.06 2.6 273 309 1,796 350 88 0.86 150 0.10 3.8 364 NOTES: 1. Projected effluent for the EES case assuming no changes are made to the existing waste treatment scheme. 2. Assumes a new intermediate waste water holding tank Is installed upstream of the API separator for crude tank draws, coker blowdown, and ballast waters with a new dissolved air flotation unit downstream of the existing CPI separator (activated sludge feed pretreatment). 3. BOD5 values for the projected effluents were calculated using computer simula tion of the refinery activated sludge process followed by flotation treat ment. COD and TOC values were calculated from the existing case COD/BOD5 ratios. 4. Effluent TSS values were projected baaed on existing data on the final flota tion unit for higher loadings. 5. These parameters were calculated from a direct scaleup of existing effluent values based only on flow increases. 6. A new 9our water stripper is being designed to allow NH3 compliance with the existing permit for the EES case. 7. Projected 95 percent chromium levels were calculated based on the pounds of suspended solids discharged (assumes housekeeping improvements with re spect to spills, etc.). 8. More of the NH3 is used up as nutrient in the activated sludge unit for the non-pretreatment case due to much higher BOD5 loadings. This assumes that the ASU does not completely fall apart from the much higher loadings. -9 - SHEQ00QQ0087 TABLE IV PREDICTED DAP PERFORMANCE Parameter Flow, gpm Oil, mg/1 Maximum Average Suspended Solids, mg/1 Maximum Average BOD5, mg/1 Maximum Average NORMAL Feed Effluent 495 - 422 50 54 30 600 335 90 50 1,097 467 820 350 Feed STORM Effluent 1,100 - 422 50 54 30 600 335 110 70 _ - 10 - SHEOOOOQOQ88 TABLE V PROJECTED NPDES PERMIT FOR EFS EXPANSION LAKE CHARLES REFINERY Parameter BOD5 COD TSS Oil & Crease Phenolic Compounds Ammonia (asN) Sulfide Total Chromium TOC Existing Permit 320 2,500 420 136 2.0 170 3.4 5.0 760 Calculated EFS Permit Based On Existing Permit Scaleup(l) 616 4,814 809 262 3.9 327 6.6 9.6 1,464 NOTE: (1) A direct scaleup of the existing permit based on crude throughput and the 1.04/0.99 overall multiplier change (Process Factor x Size Factor) in going from the present case to the EFS case. - 11 - SHE000000089 PROCESS DESCRIPTION WASTE WATER TREATMENT REVISIONS ETHYLENE FEEDSTOCK PROJECT EXPANSION CASE LAKE CHARLES REFINERY Intermediate Holding Tank The Intermediate holding tank (T-2603, nominal 10,000 bbl) will be located between the API and CPI oil-water separators. Oily water from the east tank farm crude tanks, south tank farm, ballast water tank, and coker blowdown pond will be transferred to T-2603. Approxi mately 1,500 barrels of water will be pumped from the crude tanks (T-371, 372, and 373) in the east tank farm on an intermittent basis every two days. Bill Last water from the dock, also intermittently, will be dis charged at a rate of 200 gpm into T-2603. Water from the coker blowdown pond will flow continuously into the intermediate holding tank at a normal rate of 50 gpm and a maximum rate of 200 gpm. In addition, water from the south tank farm will be pumped to T-2603 by P-976 at a rate of 180 gpm intermittently. Part of the oil and solids will separate by gravity from the oily waste water in T-2603. The waste water will flow by gravity from T-2603 to the API oil-water separator on flow control (FIC-2603). Under normal conditions, a constant flow to the API separator of 80 gpm will be maintained. A ground reach tank gauge, LI-2601, will be used to aid in manually adjusting FIC-2603 to control the liquid level in T-2603 between a maximum and minimum level for the nor mal 24 hour/day cycle. In this way the level will go through a normal daily cycle, while allowing the flow to the API separator to remain about constant. A board-mounted high, low level alarm, LAHL-2601, located in the reformer control room will alert the operators to protect the tank from overfil ling and prevent the loss of separated oil during low flow conditions. A layer of oil will form underneath the internal floating room (in stalled to prevent hydrocarbon vapor loss) and will be removed as necessary. By using the 1-inch sample draw nozzles, the all layer depth will be determined. The oil layer will be drawn off through one of the three oil withdrawal nozzles. Reciprocating pump, J-2603, or spare, J-2604, will transfer the oil from T-2603 at a rate of 60 gpm to the existing slop oil facilities for further treatment. - 12 - SHEQG0000091 A nozzle located at the bottom of T-2603 will allow the removal of solids or heavy oil. J-2603 or J-2604 will transfer the heavy oil to the slop oil treating facilities. A recycle line from the recipro cating pumps will be used to help suspend the 9olids in the bottom of the tank and aid in solids removal. A sludge sump (S-2603, 4 feet wide by 4 feet long by 5 feet deep) will be used to collect liquid discharged from the sample draw nozzles and can also be used to discharge viscoua solids from the bottom of T-2603. Material from S-2603 will normally be transferred to the slop oil facilities using J-2603 and J-2604. The tank dike around T-2603 will prevent loss of contaminated storm water and will contain oily water which may be released due to tank leaks. When necessary, stormwater will be transferred to the waste water treatment facilities by opening a block valve, which will allow gravity flow to the API outlet basin. If a serious leak occurs, water will flow through a 10-inch overflow line (located approximately 3 feet above grade) through the dike to the API outlet basin. This water will be pumped by P-453 to the stormwater diversion pond for temporary storage. Dissolved Air Flotation Unit Effluent from the CPI oil-water separator will flow through the existing 18-inch sewer to a new sump (S-2601, refer to SD-2568-83-1-C for de tails). The flotation unit feed pumps, P-2601 and P-2602, will be located in S-2601. Pump discharge will be controlled by LC-2601, which obtains Its signal from a float located in S-2601. There will also be a board-mounted flow indicator, FI-2601, on the discharge line of P-2601 and 2602, with a low flow alarm, FAL-2601, in the reformer control room. The level control point will be at the 5-foot level in S-2601. The control range will be 24 inches (12 inches above and below the control point). Normal flow, about 495 gpm, will require the use of only one pump (P-2601 or P-2602 rated at 650 gpm each). Under normal flow condi tions, P-2602 will serve as a complete spare. During storm conditions, the level in the sump will rise, and P-2602 will automatically switch on when the level rises to a height of 6 feet in S-2601. With both pumps In operation, the flotation unit feed pumps will be limited to about 1,100 gpm. Flow will be restricted to about 1,100 gpm by re stricting the travel of the level control valve. During larger magni tude storms, when the flow to S-2601 exceeds 1,100 gpm, P-453 (located in the API separator outlet box) will be actuated by a level controller located in the CPI oil-water separator and the excess storm water will be pumped to the stormwater diversion pond (maximum rate is 2,000 gpm). The dissolved air flotation unit can be bypassed during pump failure or maintenance to the unit by allowing the level in S-2601 to build until the water overflows through the existing outlet sewer down to the existing CPI outlet basin. - 13 - SHE000000092 Waste water will be pumped from S-2601 to Che flocculation tank, T-2601, with polymer addition prior to T-2601. A cationic polyelectrolyte (Nalco 603 recommended) will be used. The polymer injection point should allow the release of polymer into the center of the waste water stream. Polyelectrolyte, as 10 weight percent solution, will be trans ferred to the injection point by polyelectrolyte feed pump, J-2601. The polyelectrolyte feed pump will be equipped with flow ratio control. The pump will receive an air signal (reset) from FT-2601 and will auto matically make adjustments to maintain a constant 6 ppm polyelectrolyte dosage. J-2602 will serve as a spare to J-2601. J-2601 or J-2602 will be automatically shutdown by FSL-2601 when a low liquid flow through sump, S-2601, occurs. Both polyelectrolyte feed pumps will be equipped with simplex screens on their suction lines to remove solid particles and prevent plugging. The polyelectrolyte will be further diluted to 1 weight percent by the addition of recycle water prior to injection in the waste water stream. Adequate mixing of the polyelectrolyte and waste water will occur in the line to the flocculation tank, T-2601. The flocculation tank will provide a period of gentle agitation for the formation of floe (groups of solids particles). T-2601 will provide a 9.5 minute retention time at normal flow conditions and a 4.5 minute retention time at maximum flow. Inlet and outlet baffles will be used to prevent short circuiting. Formation of the solid particles into floe will increase the floatability. Gentle agitation will be accom plished by flocculation mixer, A-2601. A-2601 will be a variable speed mixer. Water containing the flocculated solids will gravity flow from the flocculation tank to the dissolved air flotation cell, AT--2601. This line should be of minimum length (with minimum bends) to reduce shearing of the flocculated material. Recycle will be added to the waste water stream prior to introduction into the flotation cell. Flow will be uniformly distributed throughout the flotation cell by the influent feedwell. The recycle stream will be saturated with air under pressure in the saturation column, D-2601. The release of recycle pressure will cause the formation of many small bubbles which will attach themselves to the flocculated material, and float the solids to the surface of the flotation cell. Float will be skimmed from the surface of AF-2601 by rotating skimmer arms. The float (approximately 4 weight percent solids) will flow by gravity from the float box in AF-2601 to the sludge sump, 5-2602. The float box will have an inclined dewatering beach or ramp to reduce the volume of sludge that must be handled. AF-2601 will be equipped with a center sludge well and bottom scrapers. This will allow removal of non-floatable solids that might settle In the flotation cell. A line from the sludge well to Che sludge sump, S-2602, will allow periodic removal of settled solids. Clarified waste water will flow under a baffle and over a weir to the peripheral launder. Effluent from the dissolved air flotation unit will flow by gravity to the CPI lift station. - 14 - SHE000000093 A portion of the flotation unit overflow will be pumped from the re cycle outlet box by recycle pump, P-2603 (P-2604 spare) to a saturation column, 0-2601. Recycle flow will be controlled by a flow ratio con troller, FRIC-2602, in the common pump discharge line. FRIC-2602 will have a local indicator mounted' on a centrally located control panel In the flotation unit area. In addition, FRIC-2602 will have a boardmounted Indicator, FI-2602, and low flow alarm, FAL-2602, in the re former control room. The flotation recycle pumps will be automatically shutdown by FSL-2601, when a low liquid flow through S-2601 occurs. The recycle stream will be saturated with air at 65 psig in the satura tion column, D-2601. A pressure regulator, FCV-2601, along with a rotameter, FI-2603, will be used to control the air rate to the satura tion column. Excess air will be released by an automatic air vent valve, which also will control the liquid level In 0-2601. Saturation column efficiency will be 80 percent. After exiting from the satura tion column, the recycle stream will pass through a hand-controlled pressure release valve before combining with the flotation feed. Float from the cell will contain 1,817 lbs/day of solids and oil under normal conditions. The float will concentrate to a 5 weight percent solution by settling and will be removed from S-2601 by vacuum truck approximately every 2-3 days. Cationic polyeleccrolyte will be diluted to a 10 weight percent solu tion in dilution tank, T-2602. Mixing requirements will be met by A-2602. The polyelectrolyte (Nalco 603 recommended) will be contained In 55gallon drums. A drum pump will be used to transfer polyelectrolyte to the dilution tank. Dilution water addition will be controlled by a manually operated valve. A target gauge with graduated metering stick will be available for dilution water and polyelectrolyte addition mea surements. Approximately 300 gallons of 10 weight percent polyelectro lyte will be required every 7 days. III. CPI Lift Station Effluent from the dissolved air flotation unit will flow by gravity through an existing 24-inch pipe to the CPI lift station. The acti vated sludge unit feed pumps, P-2605 or P-987, will then transfer the waste water to the equalization section of the activated sludge unit as occurs for the existing system. Pump discharge will be regulated by level control. Under normal flow conditions, only P-2605 will be re quired (P-2605 is rated at 800 gpm). P-987 will serve as a spare for T-2605. During a storm, the sump level will rise, and P-987 will auto matically switch on. With both pumps in operation, the equalization feed from the process sewers will be limited to 1,100 gpm by restricting the travel of the existing level control valve. - 15 - SHE000000094 WORK LIST WASTE WATER TREATMENT REVISIONS ETHYLENE FEEDSTOCK PROJECT - EXPANSION CASE LAKE CHARLES REFINERY Intermediate Holding Tank 1. Install a new internal floating roof tank, T-2603, fabricated as shown in Drawing SD-2568-93-3-B in the area immediately west of the existing API oil-water separator (refer to plot plan SD-2568 -42-119-L). Construct a dike around the new tank (refer to Drawing SD -2568 -93-3-B for a description of the dike) Construct the dike drain line 4-DO-26050-N-A2-3 with block valve and 10-DO-26049-N-A2-3 overflow line as shown in SD-2568-95-4-B. 2. Construct a new concrete sludge sump, S-2603, next to tank T-2603. Sump d imcns i ons arc* to be 4 feet wide by 4 foot long by 5 feet deep. 3. Tie in a new 6-inch C.S. line, 6-DO-26024-N-A2-3, to an existing 6-inch line from the east tank farm at sump in rundown area and install a 6-inch block valve in existing line. Route the new 6inch line to T-2603. Approximately 1,400 feet of pipe will be required. 4. Connect the existing 4-inch C.S. ballast water line from the dock facilities to line 26024 using a new 4-tnch C.S. line (4-D0-26025 -i*-A2-3) and block valve at the API separator. 5. Install a 4-inch C.S. line (26026) and block valve to connect an. existing 6-inch pipe in the pipe rack east of the CPI separator and T-2603 to direct flow from the coker blowdown pond and the south tank farm (P-976) to T-2603. Approximately 120 feet of pipe will be required. 6. Install J-2603 and J-2604 next to sump, S-2603. Tie in all lines and block valves as shown in P&I Diagram SD-2568-42-121-D. All valves are to be operable from the ground level. 7. Install 3-inch discharge lines with check and block valves on J-2603 and J-2604 and route the pipe to an existing 3-inch slop oil line from the API separator located in the pipe rack east of the CPI separator (approximately 120 feet of pipe will be required). Also, tie in the new 3-inch line to an existing 2-inch line as shown in P&ID SD-2568-42-121-D, Provide a 3-inch C.S. line (26036) and block valve to recycle flow from the pumps to T-2603. - 16 - SHE000000095 S. Connect the solids withdrawal nozzle on T-2603 to the sludge pump, S-2fi(n, find In .J-2603, 2604 with row 4-Inch C.S. lino ,-nul block vi I v r; .1:; :;lmwn In I In- I'M IH.ij'l.nu. Al.:n [ilnvliln .1 4-liH`li V.iruillH I Mirk liuNi i iHinrrl Inn. 9. Install 10 1-lnch valves and piping for the sampling system and route to sump S-2603. All valves must be operable from the ground level, 10. Install a ground reach tank gauge, LI-2601, with board-mounted level alarm, LAHL-2601, on T-2603. 1L. Install the 4-inch water drain lines and valves, LO-inch overflow line, segmental orifice, and 3-lnch butterfly control valve as shown in drswing SD-2568-42-121-D. Water will gravity flow through a new 6-inch line (6-DG-2603Q-N-A2-3) to the API inlet box. Approxi mately 200 feet of line will be required. 12. Install FIC-2603 on T-2603 water drain line (4-DO-26027-N-A2-3). New Dissolved Air Flotation Unit (DAF) A. Flotation Feed System 1. Install the flotation feed sump, S-2601, as shown In drawing SD -2568 -83-1-C immediately west of T-115. The existing 21-inch concrete sewer from the CPI should be connected to feed the sump. The sump will overflow to the existing 21-inch con crete sewer to the CPI lift station. 2. Install the flotation feed pumps, P-2601 and 2602, in the new sump, S-2601. 3. P-2601 is to be provided with level switches to turn on and off at 5 feet-0 Inches and 4 feet-0 inches from the sump floor, repsectively. 4. P-2602 is to be provided with level switches to turn on and off at 6 feet-0 inches and 5 feet-0 inches from the sump floor, respectively. 5. Install the board-mounted flow indicator, FI-2601, and low flow alarm, FAL-2601. The instruments will receive an elec trical signal from FT-2601. The instruments are to be included In the package with FI-2601. 6. Install the low flow switch, FSL-2601, to receive an air signal from FT-2601. The flow switch should shut-off Che recycle pumpB and the chemical feed pumps during periods of low flow. - 17 - SHE000000096 7. TnsLulI I.C-2601 in the flotation feed sump, S-2601. A stilling well for Lite ball float mechanism Is Co be provided. The output from LC-2601 will operate the DAF feed flow through a 4-Inch standard pattern continental butterfly valve in line 6-DO-26001N-M2-4. B. Chemical Feed System 1. Install fiberglass polyelectrolyte dilution tank, T-2602, equipped with a target level gauge. The tank should be elec trically traced and insulated. Provide the 1-inch drain line, 1-DO-26022-N-R37-1, to drain to the feed sump, S-2601. 2. Install the top-mounted polyelectrolyte dilution mixer, A-2602, in T-2602. 3. Install the chemical feed pumps, J-2601 and 2602, adjacent to T-2602. Connect the feed lines of both pumps to T-2602. 4. Provide J-2601 and 2602 with low flow shutdown switches. The shutdown switches will receive an electrical signal from the low flow switch, FSL-2601. 5. Tie-in line 1-WU-26016-N-M2-4 to existing service water line at the CPT to provide dilution water for T-2602. Tie-in line 1/2-WU-26015-N-M2-4 to provide further dilution of the chemical pump discharge. 6. Tie-in line 1/2-DC-26019-N-R37-1 to the discharge of J-2601 and 2602 and route to the 6-inch feed pump discharge line, 6-DO-26001-N-M2-4. This connection should be made to allow the introduction of the chemicals into the center of the 6lnch line. 7. Install the flocculation tank, T-2601, with top-mounted floc culation mixer, A--2601. Provide the 2-inch drain line, 2-DO 26021-N-M2-4, to drain to the feed sump, S-2601. 8. Tie-in line 6-DO-26001-N-M2-4 from the feed pumps to T-2601. Route the 10-inch gravity flow discharge line from T-2601, 10DO-26002-N-M2-4, to the flotation tank, AF-2601. The 10-inch line is to have minimum length and number of bends. C. Flotation System 1. Install the dissolved air flotation cell, AF-2601, with the associated equipment listed on the specification sheet. 2. Provide the 12-inch gravity flow line, 12-DO-26004-N-M2-4, from AF-2601 to existing sewer manhole downstream of new DAF feed sump, S-2601. - 18 - SHE000000097 3. Install the saturation column. D-2601, near AF-2601, with all associated equipment listed on the specification sheet. 4. IttsLiiii Liu' 6-inch recycle line, IKJ-26009-N--M2-4, from D-2601 to AF-2601. Install the back pressure value (pressure release mechanism) in 6-inch line as close to AF-2601 as possible. 5. Install the recycle pumps. P-2603 and 2604, and connect the 6-inch discharge line, 6-DQ-26007-N-M2-4, to D-2601. Install the 8-inch suction line, 8-DO-26006-N-M2-4, from AF-2601 to P-2603 and 2604. 6. Install FRTC-2602 in the common discharge line from P-2603 and 2604. The control valve is to be a 4-inch standard pattern continental butterfly valve. FRIC-2602 is to receive an air signal from FT-2602. The package is to Include the boardmounted flow Indicator and low flow alarm, FI-2602 and FAL-2602. 7. Provide P-2603 and 2604 with low flow shutdown switches. The shutdown switches will receive an electrical signal from the low flow switch, FSL-2601. 8. Install the 1-inch line, 1-DO-26013-N-M2-4, from the discharge of P-2603 and 2604 to the top of AF-2601 for wash water. 9. Install the 1/2-inch line, 1/2-DO-26014-N-M2-4, from the dis charge of P-2603 and 2604 to the chemical feed line, 1/2-DC26019-N-R37-1. Install the flow indicator, FI-2604, in the 1/2-inch line from the recycle pump discharge. 10. Provide the 3/4-inch air line, 3/4-AU-26010-N-M2-4, from the existing 2-inch plant air line at the CPI to the saturation column, D-2601. The line should contain the back-pressure regulator, PCV-2601, and flow indicator, FI-2603, which are included with the saturation column package. Sludge Handling System 1. Install the sludge sump, S-2602, near the flotation tank, AF2601, as shown In the sump drawing. 2. Install the 6-inch line from the float withdrawal box on AF-2601, 6-DM-26003-N-M2-4, for gravity flow to the sludge sump. 3. Install the 2-lnch line from the sludge well on AF-2601, 2-DM -26005-N-M2-4, for gravity flow to the sludge sump. 4. Install the 2-inch overflow line, 2-DO-Z6011-N-M2-4, from the sludge sump to the DAF feed sump, S-2601. - 19 - SHE000000098 5, Install the 3-inch sludge withdrawal line, 3-DM-26012-N-M2-4, in the lower end of the sludge sump. Provide a vacuum truck connection on the line for batch sludge withdrawal. III. CPI Lift Station 1. Replace P-986 with a new pump, P-2605, and connect it to the existing 8-inch piping. Retain P-986 as a spare for P-987 and P-2605. 2. Field check existing level control valve and limit travel to that necessary to restrict flow to a maximum of 1,100 gpm. - 20 - SHE000000099 totooooooaHs - TZ - jexjH uof^nTm aaXtoaaoax^!^^ aaxfK 5iufx uoT3tnooo-[i C09Z-I moxj tBAouiaa spnS P" TTO edumj paa^ asXxoaqoaxa^xoa duma paai QSV A3N sdtnnj ax^asg jva ednma paaj IVd tramxoo aoj^ejiruBs ax3^33H dVd 5JUFJ 3UTPTH 5BTP"^S5WI 3iubi uoxjnxTa 33X^oa3oaxa^XOd *ubi uoxsaxnoooxa iva XX0 U0X3B30X3 3XWI JVQ aH dams aSpnxs C09Z-I dmns a8pnxs dams paej dVQ Z09Z-V T09Z-Y SJDXXW *09Z-r pup eo9Z-f Z09Z-C puu T09Z-f S09Z**d 909Z-d PUB e09Z-d Z09Z-d pue 1092-d sdoina T09Z-a SIIMUIl C09Z-I Z09Z-I T09Z-I S^UBX I09Z-dV bxxD uoj^e^oxi 09Z-S Z09Z-S T09Z-S sdumg S3TOTHD TOVl asvo MoiSNVJxa - iraroM SDOisaaaa anaiAHia SN01S1AMH XNiJWXVilHJ. Mil J.VM TfXSVM isn LdaHJinbH AIR FLOTATION TANK SPECIFICATIONS WASTE WATER TREATMENT REVISIONS ETHYLENE FEEDSTOCK PROJECT - EXPANSION CASE LAKE CHARLES REFINERY Item No. Location Service Fluid Influent Flow, GPM Oil, mg/1 Maximum Average Suspended Solids, mg/1 Maximum Average pH, Range Temperature.Range, F Chemical Feed, GPU Cationic Polymer, 10 wt7. AF-2601 (1) Dissolved Air Flotation Unit Removal of Oil and Suspended Solids from ASU Feed Refinery Wastewater Normal 493 Storm 1,100 4^2 54 600 335 6-9 120-150 422 54 600 335 6-9 90-120 1.8 4.0 Effluent (2) Oil, mg/1 . Maximum Average Suspended Solids, mg/1 Maximum Average Float (Average) Flow, GPM Oil, lbs/day Suspended Solids,lbs/day 50 30 90 50 4 140 1,700 50 30 110 70 7 315 3,500 Operating Conditions New Flotation Area, sqft Overflow Rate, GPM/sq ft (3) (recycle Included) Normal Flow Maximum Flow Retention Time, Minutes (recycle Included) Normal Flow Maximum Flow Recycle Rate, GPM Normal Flow Maximum Flow Recycle Saturation Pressure, psig Saturation Efficiency, 7. - 22 - 491 1.36 3.02 50 22 173 400 65 80 SHE000000102 AIR FLOTATION TANK SPECIFICATIONS WASTE WATER TREATMENT REVISIONS ETHYLENE FEEDSTOCK PROJECT - EXPANSION CASE LAKE CHARLES REFINERY Operating Conditions (Cont'd) Flotation Tank Dimensions Diameter Depth, Water Total Freeboard Material of Construction Corrosion Allowance 9'-0" 91-6" 6" C.S. 1/8" (4) NOTES 1. Vendor will supply a detailed drawing of the flotation cell. 2. Effluent concentrations are predicted valves based upon Conoco pilot tests. 3. Flow ratio control on the recycle stream will maintain the recycle flow at 35 percent of the flotation feed. After startup, the recycle rate can be adjusted for optimum performance. 4. Not including bottom slope to central sludge cone. 5. The unit will Include the following: a. A walkway with hand rails extending to center of tank (center drive mechanism). b. A sludge rake and float scraper driving mechanism with built in auto matic torque overload indication, alarm contact and cut off switches, and including a 3/4 HP variable speed explosion-proof driver. c. A float removal assembly consisting of a float box and two surface scrapers with neoprene wipers. d. An influent diffusion feed well to uniformly distribute the alr-watersolids mixture across the tank area. e. The sludge raking arms with blades and adjustable squeegees. f. A peripheral underflow baffle for the flotation compartment. g. An adjustable V-notched peripheral velr. h. A peripheral launder with two discharge boxes (effluent and recycle). i. Saturation column and associated equipment (see D-2601 specifications). 6. The flotation cell Interior is to be coated with Carbolinea Carbomastic 14 or equivalent for corrosion protection. - 23 - SHE0000QQ103 RECYCLE SATURATION COLUMN SPECIFICATIONS WASTE WATER TREATMENT REVISIONS ETHYLENE FEEDSTOCK PROJECT - EXPANSION CASE LAKE CHARLES REFINERY Item No. Location Service FI uid Liquid Rate(2) Normal Flow, gpra Maximum Flow, gpm Vapor Rate(3) Normal Flow, lb/hr Maximum FLow, Ib/hr Operating Pressure, psig Saturation Efficiency, % Design Conditions Liquid, pH Liquid Temperature Range, F Atmospheric Temperature, F Winter Design, Min. Summer Design, Max. Atmospheric Pressure, psia Design Pressure, spgi D-2601C1) Dissolved Air Flotation Unit Saturation of DAF Recycle With Air Treated Wastewater 173 400 11.6 26.1 65 80 6-9 90-150 26 100 14.7 100 NOTES: 1. Vendor will furnish a detailed drawing of recycle saturation system. 2. Liquid rate (recycle) stream will be maintained at 35 percent recycle by flow ratio control. 3. Based on 25 percent excess air at maximum flow to maintain continuous purg ing of the saturation column. 4. The following will be included with D-2601: a. Inlet and outlet nozzles, sight glass, pressure gauge, pressure release valve, automatic air vent valve, and all tower internals. b. Specifically designed back pressure release assembly with pressure re lief valve adjusted by manual hand wheel. c. Compressed air control panel consisting of pressure gauge, flow indica tor, solenoid valve, flow control valve, and air regulator. - 24 - SHE000000104 TANK SPECIFICATIONS WASTE WATER TREATMENT REVISIONS ETHYLENE FEEDSTOCK PROJECT - EXPANSION CASE LAKE CHARLES REFINERY Item No. Location Service Fluid Dimensions, Ft Diameter Height Total Normal Liquid Capacity, Gallons Total Normal Liquid ' Retention Time, Minutes at Normal Rate at Maximum Rate Design Conditions Operating Pressure, psig Design Pressure, psig Operating Temperature, F Design Temperature, F Material of Construction Corrosion Allowance Type T-2601 Dissolved Air Flotation Unit Flocculation of Suspended Solids in Refinery Waste Water Refinery Waste Water 9 13 10 6,200 4,700 9.5 4.5 0 0 120-150 150 C.S.(6) 1/8-Inch Open top, vertical cylindrical tank. NOTES: 1. The centerline of outlet nozzle is to be 36 Inches below top of sidewall and the same elevation as the flotation cell overflow weir* 2. Pipe connection between T-2601 and AF-2601 is to have the minimum length and number of bends. 3. An 1/4 HP variable speed mixer (A-2601) is to be top-mounted to meet mix ing requirements. 4. A walkway with handrails to the center of the tank will be provided. 5. Four antlvortexing baffles and inlet and outlat baffles will be provided. 6. The tank interior will be coated with Carbolines Carbomastlc 14 or company approved equal. - 25 - SHE000000105 TANK SPECIFICATIONS WASTE WATER TREATMENT REVISIONS ETHYLENE FEEDSTOCK PROJECT - EXPANSION CASK LAKE CHARLES REFINERY Item No. Locat Lon Service Fluid Dimensions, Ft. Diameter Height Total Normal Liquid Capacity, Gal. Run Time Between Mixes, Days Design Conditions Operating Pressure, psig Design Pressure, psig Operating Temperature, F Design Temperature, F Material of Construction Corrosion Allowance Type T--2602 Dissolved Air Flotation Unit PolyelectTolyte Dilution and Storage Tank 10 weight percent solution of cationic polyelectrolyte. 4 5 3.5 300 7 0 0 40-100 110 Fiberglass None Vertical Cylindrical NOTES: 1. A 1/4-HP propeller-type mixer (A-2602) is to be top-mounted to meet mixing requirements. 2. Tank, is to be equipped with a target level gauge. The graduated meter ing stick will allow proper dilution water addition. 3. A 1-inch service water line is to be supplied to the top of T-2602 for dilution water addition. 4. Tank is to be provided with fiberglass top and observation hatch. 5. Entire chemical addition area to be surrounded by curbing or small re taining wall to contain spills. 6. Tank is to be electrically traced and insulated. - 26 - SHE000000106 TANK SPECIFICATIONS WASTE WATER TREATMENT REVISIONS KTMYI,KNI^KKKI>STO('K PHtUKCT - KX^ANSION CASI-: LAKE CHARLES REFINERY Item Location Service Fluid Dimensions, Ft. Diameter Height Capacity Barrels Design Conditions Operating Pressure, psig Design Pressure, psig Operating Temperature, "F Design Temperature, *F Material of Construction Corrosion Allowance Type T-2603 Vest of API 011-Water Separator Intermediate Holding Tank Oily Water 43'-0" 40*-0" 10,000 0 0 40^90 90 C.S. l/8-tnch Internal Floating Roof NOTES: 1. Internal floating roof support legs are to be constructed of galvanized steel. 2. Tank is to be equipped with a ground reach tank gauge. 3. T-2603 is to be enclosed by an earthen dike. Dike will have approxi mate dimensions of 85 feet long by 50 feet vide by 6 feet high. - 27 - SHE000000107 MIXER SPECIFICATIONS WASTE WATER TREATMENT REVISIONS ETHYLENE FEEDSTOCK PROJECT - EXPANSION CASE LAKE CHARLES REFINERY Item No. Location Service Tank Dimensions, Ft Diameter Height Total Normal Liquid Liquid Volume, gal Retention Time, Minutes Fluid Temperature, *F Viscosity, cp Sp Gr pH Mixer(1) Type HP Entry Position Material of Construction A-2601 Dissolved Air Flotation Unit Flocculation Tank T-2601 Provide Gentle Agitation for Flocculation 9 13 10 4,700 9.5 (495 gpm) 4.5 (1,100 gpm) Refinery wastewater with cationic polymer added to aid in flocculation. 120-150 1 1.0 6-9 Turbine 1/4 (variable speed 15-45 rpo) Top Type 304 S.S. Shaft and Blades NOTES: 1. A-2601 is to provide a uniform energy distribution in tank T-2601. The drive for A-2601 has been specified as variable speed to allow for adjust ment to maximize floe formation without floe shear. - 28 - SHE000000108 MIXER SPECIFICATIONS WASTE WATER TREATMENT REVISIONS ETHYLENE FEEDSTOCK PROJECT - EXPANSION CASE LAKE CHARLES REFINERY Item No. Location Service Tank Dimensions, ft Diameter Height Total Normal Liquid Liquid Volume, Gal. Fluids Volume, gal Temperature, F Viscosity cp at 60"F Sp Gr pH Mixer Type HP Entry Position Material of Construction A-2602 Dissolved Air Flotation Unit Polyelectrolyte Tank T-2602 Batch Mixing of Polyelectrolyte with Dilution Water 4 5 3.5 330 Water 300 40-100 1.0 1.0 6-9 Polyelectrolyte 30 40-100 100 1.16 6-7 Propeller 1/4 (350 rpm) Top Type 304 S.S. Shaft and Blades - 29 - SHE000000109 SUMP SPECIFICATIONS WASTE WATER TREATMENT REVISIONS ETHYLENE FEEDSTOCK PROJECT -EXPANSION CASE LAKE CHARLES REFINERY Item Location Service Fluid Dimensions Length Width Depth, Total Normal Liquid Maximum Liquid Retention Time, Minutes Normal Rate Maximum Rate Design Conditions Operating Pressure, spig Design Pressure, psig Operating Temperature, "F Design Temperature, Material of Construction S-2601 Air Flotation Unit Area Air Flotation Feed Sump Oily Water lO'-O" 5'-0" 11 6'- " 5T-0" 6r-0" 3.S 2.0 0 0 90-150 150 Concrete - 30 - SHE000000110 SUMP SPECIFICATIONS WASTE WATER TREATMENT REVISIONS ETHYLENE FEEDSTOCK PROJECT - EXPANSION CASE LAKE CHARLES REFINERY Item Location Service Fluid Dimensions Length Width Depth, Total Normal Liquid Capacity, Gallons Retention Time, Hours Normal Rate Maximum Rate Design Conditions Operating Pressure, pslg Design Pressure, pslg Operating Temperature, *F Design Temperature, *F Material of Construction S-2602 Air Flotation Unit Area Collection of Float From Air Flotation Unit Float (4X solids) in Waste Water 18'-0" 13*-0" 7,-6"(4) 7*-0M(4) 11,400 47 27 0 0 90-150 150 Concrete NOTES: 1. A 3-inch vacuum truck connactlon will be provided for removal of bottoma sludge. 2. A 2-inch line will be provided for overflow to the new DAF feed sump. 3. The sump will be sloped one foot towards the point of sludge withdrawal. 4. Dimensions at overflow end of sump. 5. The sump will be provided with a redwood cover and baffle. - 31 - SHEQQ00Q0111 SUMP SPECIFICATIONS WASTE WATER TREATMENT REVISIONS ETHYLENE FEEDSTOCK PROJECT - EXPANSION CASE LAKE CHARLES REFINERY Item Location Service Fluid Dimensions Length Width Depth Material of Construction S-2603 T-2603 Intermediate Holding Tank Slop Oil and Solids Draw Slop Oil-Water-Solids 4'-0" 4*-0M s'-o" Concrete - 32 - SHE000000112 ENGINEERING CENTER PONCA CITY, OKLAHOMA SPECIFICATION SHEET , CCNTtlPUOM PUMPS P> ant LOCATION l.C. ftC-4-mfcX^ _ PROJECT _liiXLfcKlV. A.F.E NO. ____ _______ DATS 8/^-7 3 MAOC BY ac. APP'O BY b m no. -- W .O . NO INQ. NO. REG. NO. P.O.NO .CKgajMSiflFj ^flSE. 7ffTlCA5r?7y^ST?MAT^rr^URCHrBE " g-* gfegs service pitto.,y ed . B v< F. 10+0*4 ion MOTOR DRIVE TURBINE I 1 uouip '^j'a,V4,r PT F SPGRitPT OA VAP PRESS. at PT. p*a 3 / OPERATING CONDITIONS U S. gp* M PT-NOR OISCH PRESS.. Df -- SUCT PRESS., p*MAX QIFF PRESS.. pH Dlff HEAO. ft RATED ISS RATED JCL aVIS t PT. Sm CORR/EROS CMJMtiby NPSH AVAIL.. N CONSTRUCTION CASING MOUNTING (CENTERLINE ) (FOOT ) IBRACKET ) (VERTICAL SPLIT type" (AXIAL I (RAOtAL (SINGLE VOLUTE 1 IOOUBLE VOLUTE (DIFFUSER TAPPED OPENINGS (VENT ) (DRAIN I (GAGE CONNS. N02ZLES SIZE ASA RATING FACING POSITION SUCTION OISCHARGE MATERIAL COPE-EXTERNAL CASINO I CAST IRON INTERNALS COOK a-BRONZE IMPELLER $-STEEL INNER CASE PARTS C- tM3%Cf SLEEVE (PACKED! A ALLOY SLEEVE (SEAL) h-HARO&NED WEAR PARTS I- FACED SHAFT x wi res ivr INTERNAL PARTE 1B c SPECIAL MTL.COOE 1 8sc 11 sc Cr a Af Af CCc c 1 8 0 Cr s s sS MOTOR ORIVER BY TURBINE ORIVER EY ITEM NO.____ MTDBY _H> RPM FRAME MFR OR COMPANY APPVO, EQUAL ITEM NO. HP PPM MFR and TYPE INLET STEAM, ptiq MTD BY MATL TEMP F TYPE INSUL ENC F^q, PfC. TEMP RISE C~ VOLTS/P"HXAsSE/CYCLES EXHAUST STEAM RATE, ft BEARINGS Ib/BHP/HR LUBE BEARINGS FULL LOAO AMPS LUBE NOZZLES SIZE ASA RATING INLET EXHAUST FACING POSITION REMARKS: S.PEM 3M.PSlUEft L1 )t V- PUfwR B6.A A (LE- TC e>fe _g_i^U^j\5.^_U>_IT_lL eIsLOvC~.oAY\>^. PUMP IS TO BE MANUFACTURED IN ACCORDANCE WITH THE FOLLOWING 8TANOAR08. API-610 I ) INOICATES ITEM CHANGED ON LATEST REVISION. ~1 NOTE: THE SOUND LEVELS GENERATED BY THE PUMP AND ORIVER SHALL BE WITHIN THE LIMITS OF THE ATTACHEO SPECIFICATION. VENDOR MANUFACTURER SIZE ANO TYPE STAGES RFM ROTATION FACING CPUS. EFF. HYO. H.P. RATED 8.H.F. RATED HP ORIVER DIA. IMP. MAX. OIA. IMPELLER N.F.S.H. AEOD. IN FT FLUIOPUMPEO MFRS. BEARING No. RADIAL THRUST PACKING OR SEAL FLUSHING, GPM MATERIAL EXCEPTIONS BY VCNOOR WATER COOLING BEARINGS STUFF. BOX' PEOE5TAL GLAND TOTAL CW. REOD. COUPLING MFR. COUPLING, TYPE GUARD MECH. SEAL, MFR. MECH. SEAL. TYPE PACKING DELIVERY. WEEKS PUMP PRICE ORIVER PRICE EST. FREIGHT TOTAL PRICE 4-4M-S QUOTATION WILL NOT BE CONSIDERED IF SUPPLIER DOES NOT COMPLETE RIGHT HANO COLUMN, 33 _ B-1S-7J SHEET. .OF REV. SHEOOOOOOU3 LANT i n^tTiQM /AML ENGINEERING CENTER PONCA CITY. OKLAHOMA SPECIFICATION SHEET CENTRIFUGAL PUMPS tCr h *,rpRnjCT Aft NO ..... OAT fc VM/7 1. MAOE BBYY PP APP 0 BY a m no X ?/ pA ej . VV O NO----------------INO NO ------- -- BEQ NO._________ P 0 NO _ t- _ 1 APPLICABLE TO ESTIMATE (VI PURCHASE 1 I t P- 2G o ?. A Ksa 5L b O i SERVICE ft.fceyct.e_ 1 * ^PMPfc. 3 MOTOR ORIVE 1 y\ TURBINE 1 1 > . i OPERATING CONDITIONS /, i i LIQUID tuA-Tfc*- US gpm PT, NOR ./.7.3 RATED A CC 0 PT f \ <,> DISCH PRESS. pug rt SUCT PRESS.. pwgMAX 'I RATED 0 11 SPGRatPT /.C 12 VAP PRESS. PT. p*. 3.7 13 VISatPT.BM 4p O-1* 14 CORR/EROS uuHd by DIFF PRESS., pi OIFF HEAO, H .. NPSH AVAIL, H 75 1 7.5 T O 4* IB CONSTRUCTION 8 CASING MOUNTING (CENTERLINE I (FOOT ) (BRACKET 7 SPLIT IAXIAL | (RAOIAL 1 8 TYPE (SINGLE VOLUTE ) (DOUBLE VOLUTE (VERTICAL I t (OIFFUS6R ) 9 TAPPED OPENINGS (VENT ) IORAIN 1 (GAGE CONNS. 1 0 NOZZLES SIZE ASA RATING FACING POSITION 1 SUCTION 12 DISCHARGE 23 MATERIAL CODE-EXTERNAL CASING !4 I CAST IRON INTERNALS COOE !5 B- BRONZE IMPELLER 28 S STEEL INNER CASE PARTS NTERNAlPARTS x______ 1 B8 C SPECIAL MTL COOE 1 BSc 1 sc 27 C-1l-13%Cr 28 A ALLOY 29 n-HAROENEO 30 FACED 31 x u: - SLEEVE (PACKEDI SLEEVE (SEAL! WEAR PARTS SHAFT Cf Cr At At CCCc 1 8 Cr Cr s S SS 32 motor driver by ITEM NO. MTQ BY HP RPM FRAME as MFR 3? OR COMPANY APPV'O. EQUAL TURBINE DRIVER by ITEM NO. HP RPM MPR r>d TYPE INLET STEAM. * MTO BY MAT'L TEMPP TYPE INSUL 39 EMC jcfi. PfcR, TEMP R|$E C EXHAUST STEAM RATE. FL Ito/BHP/HR VOLTS/PHASE/CYCLES BEARINGS LUBE BEARINGS 2 FULL LOAO AMPS 43 LUBE NOZZLES SIZE ASA RATING INLET EXHAUST FACING POSITION 44 REMARKS 4& 48 47 PUMP IS TO BE MANUFACTURED IN ACCORDANCE WITH THE FOLLOWING STANDARDS API410 I INDICATES ITEM CHANGED ON LATEST REVISION. - NOTE: THE SOUND LEVE IS GENERATED BY THE PUMP ANDORlVER SHALL BE WITHIN THE LIMITS OF THE ATTACHED SPECIFICATION. o) FLO MJ a+\b *1 A L LAT4 U'U.U f^.6. V f Ptr / >C>ri T 3&tCi Ptc i.A-7 vdAl >+i pvi "1 PUMPS TC Ttfc. L..,,* lb L v.-.iK ISLUAH L/^klSb Pl4WT ^ATtA. QUOTATION WILL NOT BE CONSIDERED IF SUPPLIER DOES NOT COMPLETE RIGHT HAND COLUMN. - 34 - 5/'STCtVk SHEET. VENDOR MANUFACTURER SIZE ANO TYPE STAGES RPM ROTATION FACING CPLG EFF HYD. H P. RATED B HP. RATED HP DRIVER DIA IMP MAX DIA IMPELLER N.PSH. REQO IN FT F LUID PUMPED ( ' ! ' ) MF AS BEARING No RAOIAL THRUST i ( PACKING OR SEAL FLUSHING. GPM MATERIAL EXCEPTIONS BY VENOOR * WATER COOLING BEARINGS STUFF BOX PEDESTAL GLANO TOTAL C.W REOD COUPLING, MFR COUPLING! TYPE ~GUAH0_______ _____ mech.sealTmfr MECH. SEAL. TYPE "PACKING DELIVERY. WEEKS PUMP PRICE DRIVER PRICE _ EST_FRI_GHT `totalprice ! i OF REV. SHE000000114 PLANT LOCATION ^ ENGINEERING CENTER PONCA CITY, OKLAHOMA SPECIFICATION SHEET , CCNIttfUOAl PUMPS V > <Z\ PROJECT A.Fi NO. . DATE____ & MADE BY 72 APP'OBY B.M NO. 'Cue. ___iT.c eAi W. o NO. . INQ.NOREQ. NO. P 0 NO APPLICABLE TO: ESTIMATE <SQ PURCHASE ( I SERVICE _____ jfiT^ T L*fcL ................ Si MOTOR DRIVE ) TURBINE l I iv - UFT OPERATING CONDITIONS uoH!?r*Vsi iVtsA pj f U.S.SP*tPT,NOR. OtSCH PRESS.. pM JkSL SUCT PRESS.. p*t MAX <? RATED flQQ RATED y*C SP GR *t PT VAPPRESS. M PT. pit a k OIPP PRESS.. pm DlfF HEAP, It VIS it PT.SMgp T NPSH AVAIL.. l CORW/EROS ew* by SAhhOj 3/tJ T~ SO CONSTRUCTION CASING MOUNTING ICENTERLINE I (FOOT I(BRACKET I (VERTICAL JPUT_ (AXIAL (RADIAL TYPE (SINGLE VOLUTE TAPPED OPENINGS (VENT ) IOOUBLE VOLUTE (DIFFUSER (DRAIN ) IGAGE CONNS. NOZZLES SIZE ASA RATING FACING POSITION SUCTION DISCHARGE I CAST IRON B- BRONZE S STEEL C 11 !3%Cr A ALLOY h:HARDENED i'faceo INTERNALS CODE IMPELLER INNER CASE PARTS SLEEVE (PACKED) SLEEVE [SEAL) WEAR PARTS SHAFT X KJ, - (Lfetivr MOTOR DRIVER 0V ITEM NO. MTD BY HP RPM FRAME MFR OR COMPANY APRV'D, EQUAL TYPE INSUL "6NC g^P. Pg. TEMPR)SEC~ VOLTS/PHASE/CYCLES BEARINGS LUBE FULL LOAD AMPS REMARKS: QPgM 1BSc 1 Bsc 1( $c Cr Cr Af Af C CC c 1 B Cr Cr S S SS SPECIAL MTL. COOC TURBINE DRIVER BY ITEM NO. MTD BY HP RPM MAT*L MFR ana TYPE INLET STEAM. pw9 TEMP P EXHAUST STEAM RATE. FL NUBHP/HR SEARINGS LUBE NOZZLES SIZE ASA RATING FACING POSITION INLET EXHAUST \)6ftTlC.\L. feOMl VENDOR MANUFACTURER SIZE AND TYPE STAGES RPM ROTATION FACING CPLG. EFf. HYO, H.P. RATED B.H.P. RATED HP DRIVER DIA. IMP. MAX. DIA. IMPELLER N.P.S.H. REQO. IN FTFLUIO PUMPEO MFRS. BEARING Na. RADIAL THRUST PACKING OR SEAL FLUSHING. GPM MATIRIAL EXCEPTIONS BY VCNOOR~~| WATER COOLING BEARINGS STUFF. SOX PEOESTAL GLAND TOTAL C.W. REQO. COUPLING. MFR. COUPLING. TYPE GUARO MECH. SEAL. MFR. MECH. SEAL. TYPE PACKING PUMP IS TO BE MANUFACTURED IN ACCORDANCE WITH THE FOLLOWING STANDAROS. API-810 l I INDICATES ITEM CHANGEO ON LATEST REVISION. NOTE: THE SOUND LEVELS GENERATED BY THE PUMP AND DRIVER SHALL BE WITHIN THE LIMITS OF THE ATTACHED SPECIFICATION. DELIVERY. WEEKS PUMP PRICE DRIVER PRICE 6ST. FREIGHT TOTAL PRICE ----- 1 QUOTATION WILL NOT BE CONSiOEREO IF SUPPLIER DOCS NOT COMPLETE RIGHT HANO COLUMN. 35 S-IB-72 SHEET. OF REV. SSS000000115 ' PI AWT /A#". ENGINEERING CENTER PONCA CITY. OKLAHOMA SPECIFICATION SHEET PROPORTIONATING PUMPS ttcntil/ proifot a.f.e.no-------------------------------------------------------0Are .VO^J WO.NO---------------------- -- MAOE BV_ ('(*INQ NO. ______ APP0 8Y REO NO. B m no p.O no-------------------------- ^Vrjftcr- i SERVICE h9Lv tiUTHO'-yT. H A . Vt >') 2 4>J& T. A fe. 3 OPERATING CONDITIONS 4 LIQUID |0 UJT *7. 6. IM U'A4e_ 5 PUMPING TEMPERATURE, F /OO <*>*>, 6 SPECIFIC GRAVITY # P.T. 7 VAPOR PRESSURE 9 P.T. B VISCOSITY P.T..-8 <*.- r /) Q 9 CORR/6ROS CAUSED BY: tCwy aUKliuA pW- ?.0 10 U. s. SO* GPH AT PT. NORM. 1. % DES. OES. 4,. 0 11 SUCT. PRESS., pcifl. MAX. 0 DES. C J2J OISCH. PRESS., 13 OIFF. HEAD, tl 14 NPSH AVAIL., h MAX. Zll -ZC +- OES. jcC 15 16 CONSTRUCTION 17 CASE MAT'L. HEQ'D. 7 Vf>. v/6 CS t- 4 ***.> P*18 UOUIO END MAT'L. REQ'D. r^ O / HA -CPU r> 19 STROKE ADJUSTMENT: YES MM 20 MANUAL 21 AUTOMATIC 22 NUMBER OF CYLINDERS 23 BASEPLATE REQUIRED Cii,TAl>- 24 COUPLING REQUIRED 25 COUPLING GUARO REQUIRED 26 MOTOR DRIVER BY 27 ITEM NO. 28 ""hp rpm MTO BY FRAME 29 MFR 30 OR COMPANY APPV'D EQUAL 31 TYPE tNSUL. 32 ENC /P. fififi, TgMP, RISE C 33 VOLTS/PHASE/CYCLES 34 SEARINGS LUBE 35 FULL LOAD AMPS 36 37 ITEM NO, J- ZfcOf MANUFACTURER SIZE DESIGN SPEED, SPM MAX. RECOMMENCED SPEED, SPM MAX. PISTON SPEED, ft/MIN STROKE LENGTH, IN BORE.IN SUCTION NOZZLE size class DISCHARGE NOZZLE SIZE CLASS BRAKE HORSEPOWER VOLUMETRIC EFFEClENCV NPSH REQUIRED LIQUID END-MAT^ DIAPHRAGM MAT'L. COVER PLATE MAT'L. LIQUID END GASKET BALL CHECK VALVES - MAT'L BALL SEAT MATERIAL PLUNGER GLAND LANTERN RING PACKING TYPE COUPLING MANUFACTURER SPEED REDUCER MANUFACTURER F TYPE OELIVERY, WEEKS SHIPPING WT. PUMP PRICE MOTOR PRICE E5T. FREIGHT COST TOTAL PRICE face FACE 38 39 40 41 42 43 44 45 46 47 48 49 50 __5l' NOTES: (>) 7>)h T ntne/^rcn /c/euJ ('4i4cr I.t.1 Aw'frtttA'tYc PtJrthO tU Z n+.&*?*+ L. tUfcUf AN)D Ac.l_ PULti^ftt fntfL u>t*L u/v'ti li<u 1. 1 /* . I.1 fc. A- 4i '4/eW Alt- r.Cifc.^r, v* f , *-Lo\*3 TA f S < 4 1<* . >?*/-. s:- 1 3 c QUOTATION WILL NOT BE CONSIOCREO IF SUPPLIER OOES NOT COMPLETE RIGHT HAIYO COLUMN. - 36 - SHEET OF REV 1-432-: SHE000Q00116 m-m SaEElB o. amt !. . 1- ENGINEERING CENTER PONCA city, OKLAHOMA SPECIFICATION SHEET PROPORTIONATING PUMPS project &THVLiA/l. DATE MAOE BY APP'n BY '.Ifm W. O. NO--------------------------- INO. NO -------------------------AEQ. NO. b m no . p o.no--------------------. +-E.fU}.';7nU'- EAffMSfoO UKf stuvici KLUDGE RND OIL. KMD2iIL_ ? ^v. n't- x- (io3 3 OPERATING CONDITIONS LIOUIO 6o++orO ^rvlirK Of Cj inn fit 1 5 PUMPING TEMPERATURE, F " SPECIFIC GRAVITY P.T |, mlmno 0- b03 1 2fe04- MANUFACTURER SI2E TYPE DESIGN SPEED. SPM MAX RECOMMENDED SPEED. SPM max mmon r.pfrn. h/min 7 1 fl VAPOR PRESSURE 9 P.l . VISCOSITY P.T..-SSU 'p r>. ) Si SI ROM. LKNGTH, IN BORE.IN 9 CORR/EROSCAUSED BY: SUSpfJDD SA/JD 4" SOUtt 101 U.S. GPM.-GEHJkT PT, NORM. OES. OES. n SUCT. PRESS., psi#. MAX. DES. O SUCTION NOZZLE SIZE DISCHARGE NOZZLE CLASS FACE 12 DISCH. PRESS., psig. MAX. / f "7 DES. 13 DIFF. HEAD; ft l| 14 NPSH AVAIL., ft / S' 70 SIZE CLASS BRAKE HORSEPOWER VOLUMETRIC EFFICIENCY FACE IS 16 CONSTRUCTION iT CAUL MAT'L. REO'D. IB LIQUID END MAT'L. REO'D. 19 STROKE ADJUSTMENT: YES OR NO (&') NPSH REQUIRED LIQUID END MAT'L. DIAPHRAGM MAT'L. COVER PLATE MAT'L. LIOUID END GASKET 20 MANUAL 21 AUTOMATIC 7? NUMBER OP CYLINDERS 23 BASEPLATE REQUIRED 24 COUPLING REQUIRED BALL CHECK VALVES BALL SEAT MATERIAL PLUNGER MAT'L GLANO LANTERN RING 25 COUPLING GUARD REQUIRED PACKING TYPE 26 MOTOR DRIVER BY 27 ITEM NO. 28 HP RPM MTD BY FRAME COUPLING MANUFACTURER SPEEO REDUCER MANUFACTURER 29 MFR 30 OR COMPANY APPV'D EQUAL 31 TYPE INSUL. DELIVERY, WEEKS 3? ENC gjLp. fT F. TEMP. RISE OC 33 VOLTS'PHASE/CYCLES 34 BEARINGS LUBF SHIPPING WT. PUMP PRICE MOTOR PRICE ~~3b FULL LOAD AMPS r^r- 37 EST FREIGHT COST TOTAL PRICE 38 39 NOTES: an ~'i . ' * t ir: ? . .diiv 42 43 T M r. ;ll^. i'i x.\ fee. '*'+ A 44 r t t- | ( C'-S'.irfii 4b - . U>. < -* l ij v i.e-r, `S'.' ' < l v \ iOA-rrs 4G 47 4- 4b -> A . J C 1-4 n + i _______________________________ ________________ .. -9 r v r* l +0 to < C. - y v #* ' ' 0 * - ' ' < v, lYni.'/r 1 r<- 49 . f\w 4 at c Ar * S'*4f - so' - Ta m y \ 'L ^ 15 i 5. j ij> 9 \ td VJ: * ,JQpai'' <? ^ O 51 * Cr ftfi Sfrn ke 52 PutfP\C> M_SO REQUIRED J Tft LIPT LlU/n OUT OP A SUMP 53 Six FEET eLoW SRftDt. 54 U1 QUOTATION WILL NOT BE CONSIDERED IF SUPPLIER DOES NOT COMPLETE RIGHT HAND COLUMN. _ 37 ^ SHEET OF RFV -432- SHE000000117 ccr: *&.** Vel ft/s e c P ro je c t CA __ LJ M a d e B y -- C L z P re s s D rop PSIG / 100* P la n t JLdfc D ate 4 r P u t p\AiH-kc. PROCESS P IP IN G SCHEDULE PROCESS ENG INEERING DEPARTMENT F low L in e S e rv ic e Rate D e sig n a tio n R em arks 3 '-t $ Is 8s $ 3 5j G44. % T X 15 Kl N. Q cs *$ 3 <5f v > ft 0 "S N 3 < r S is 4 -4 ~iUos s? s h O V 3Q-J s X rS -S <5 so wNm to 3 '1V- h U. *\ 4\ 3? *iA I V 19 N v^ X. 'o N V 4 5^ li i Li N "oh Lfvj u CN c AJ in rJ V <4 * 4 VI ri "V* vS >9 -*$ VI f T IN r 'T *r < Q / s5 1 o & s ii k li rJ r< o a N f 4 * ts. aJ to i v T O l t> o N 0` d 4> V 1 <4 d. k 1i 0. u (0 0. *co H > U D a \S> >S k si l 4i v> sS 4J (4 o >s oo d 1 1 4 sB >a dd d fi -&a sS -a 3 Q d d <3 fc- Cun u V ffl a. < J^ NS V. s' \ vs v* v *v S3 si v> V) d 'C 1 Qo 0 00 1 sy ri vS <si <4 AJ Al -> vS A1 N VS o HV 10 U5 fO <4 0i 0 o oO O >> c u u l ti S3 V O 0 0 ft 0 fftt o0 EC o Z 0, ab o *0 C u & s. 0 to o 'vi Ooo 8 0 k< & N V1 Q O oSj t) c o<3 Qft o q oft Li 3(/) S CL > Js 5 >J 0 B Li Cm s0 f<t5 f0ot 0 Oi 0 oft ft* o Uj <1 in M1 to \ 0 0Q oQ fiJ 0 0o Moo 0 o0 0 0g s9 ao QO' fj 0 .i 0 O in 0 0 \n -4 j >4 J Ji -J 0 4 4 'x j -J 4 o si zV o <0 tJ 0 -fi fO 1 u V< rJ 0 St N 1 fP d It) 3 U) v 0 4> ri i V) v00 3o fi rsl t lO f C s D rSJ0 0 v <N Ma a 0 4) i4 V* 4a mt40n-i V 0 N <4 t u. t i. w4 A\t \ c *5j* A4 >5 X? 4 a a4 .u O 9 tf d. c 9 fJ i h o -a 4 U 0 a A) 4. cs fi u < o A** j. (* 0 -S rJ a 40 3 fi a i < 4 4 i t. -5 n a fj 0 -9 f) V 0 J a! t A jt h s* 4- %fst Mi4on d. sc> ft 9 s3i 4 1 *1 f i1 X f H f f 4 A fj \ NT s 5 *s* 4 + + V- * i 2 A s? JT ro0v i-41 2i * A 0 < * 8 4 Ml s in l C 4 8 >c r &. r Q o o O r4 3 - ft Q Q ti ri 2 i 0 j N % i Tjl A o 44 4 i i * o -a <sl G sA N i! k c cQ 5 *5 0 -i Ct "^e 0 O saO > a 4J 3 >9 1 * <V nn 1 0 o T 0 0 T 0 0 vr 8 t 4 j J 4 TT /J G 4) A) l ri n rJ 0 9 rii 4 % c i Nj O Psfi C fl- 1V 8 (> 1JL4 i V j ri 0 43 h iJ 00 S \oj s ri -1 J 0 -1 h* i < kr r, c> c t. 7 \ iV 1 t00 r Ac| J 5 5 J S 4 N A> 2 1 O V j Ci Q c> si V - 39 - R w -I dem otes 5HE000000118 PROCESS PIPING SCHEDULE PROCESS ENGINEERING DEPARTMENT Date Hade By _____ Project 1 f. L. *' r.. . ;i Plant i ry.i_^v.hw. * s <*?r -:7- K1 Si (C OJ 3 ,ci cJ > SHE000000119 Line Designation Service Frau TO Plow V Rate L Lb/Hr (Hot BPSD) Normal At T and P L B/CF Vise *F PS1G (SP G* CP Press Drop PSIG/ 100* Vel ft/se c 2-to- 7.<.or - n - m\-4-K h no - Zi>CTL l-*v- JB 37-1 r-ztew r- t4oi- i-7,fcC/ L *S ' 2.4># L -- - /50 /to O 0 - - - -- -- - y- 0-7>7vn-mi*4 y-- T iVk-rt-rti; SorAP tto fi*-On-?kA84-M`A?>3 ROtfDOWN fiftlA P-24<4 T-etoS t- 7*0. *pO /r* 0 ^A/ L foo1rvoo 70 _> 0./27 0.^5 0-/3 2. SC* Z. 22. 4 - f)r\4-DO-2bOSb'D-A^3 t-fao-z<o24-it2>3 L ^*Li ne. ___T-2fr03___ L lorkj/vyi 70 so ^2.3 i2dL 0-^ *Qry700 $0 feg O-IS 0. 7SF 5-04- 4- bo-?fcoM-W*-3 V- EboS L 46 ,000 0 IC-tJC.-ffcAM-ttf-'X 4-t-2fe27-^hl*? L 4QjOQQ 0 4* c- ?'rte>2R-U A2-3 ro* oo- ZbON- t* U-T-3 b-0o-Zbo30'itt*3 L ^OOOO Vet ttiir L 3%oOO Uqo o T'WM- ^feOll-M-AbS t- SbO'S *'* L no o 4-Mv-, :*' r:<?. I (\?` 2 4'Htf- ?i.e34-W-r?'E J- 2fco4- w * - a. : l-ilM . r<S>h L'-li *> r-r-o'i l. iocco nn 0 a ... 0 0 r. -0 J'Hn-eboxs-W'm- >' VHK'E&ftUs-fWa- i' 2"VU * - =4>n.T7 - u* ft/- ? S-*.V f.\-?, r. yb7j-^ 4- ?teet 4- .l-v>04 ViM-zfaoia-M-ra u 300cr\ n - >. - r - z'*ri -j ? 4n*r ` ' .*t r L no. _iL 70 -70 i' /<* fcE. \ Q..l O. .0J0.75. 0.1^7 2. 0.75 l&l - S^fl5 15 -- SUzA- 2.7 2 `. =r,i ."72 '* .0 /. 53 1 ! ,* : rr "irio aT c-.*?a f\.Cy' :;r r * i rziz, .' vi Remarks 5' urso' 5' ./eo' I >v 10 .1 \0 /r- 7-----# 200 "* F-i.Ci.1 AftajiT1.e^Ow oueftrvnv.1 Frc r-?>r> 4TPAu.L',r FLOW 101 E>1 o' r' rTT^ -i' 15' `ZO* ' ^v, ' RW'i 4* P^c p'pfe PROCESS PIPING SCHEDULE PROCESS ENGINEERING DEPARTMENT Date _ Project Plant _ Made By ) Li ne Designation 1* hk- ?,;.o*R-r -ft'- : l v.r f * -- m* r,? 2 1 - .!! F- ' - S r- ' bOnVN' f2'? 1 * H M .fU',-4 - h- I-''-' v; I - c-vo-C-r;* l\\ : -`hoi. -n* i* WK - Si-.?-''-'-- f'-at*': i ^rs-1 < *" Service From To * . . ** M . II * ., ' s - - V . .. FlOf V Rate L Lb/Hr (Hot BPSD) Normal At T and P LB/CF Vi sc F PSIG (SP GR) CP Press Drop PSIG/ 100` L- \ * |g? Vel ft/sec Remarks r r> r> Jj2- - Cv y. r * t 'V ' * *. - :' 7 21 ' , ; c' 1 16-00- -IV M-'i T`IWS >*. 4-00- lfa**e-rv-Ai- V rle% Dtkfe t- Hrr>- l.fcp.SI-V**-4- P-lc.o6 A-t(,e4 2- 14* -n-At-i T- tto-i. Vhw- - n- At- 3 T-tfcoi API c^nex toy L (Wi.faooiT* <?r UUt 2Co4=r L *50 j( i*T iA4 *' LiOt L VrtOOO iiSJ 4c ClUfc 2tol7 L in ooc 70 tlMt 2fe.&*i,\ C 2.4 6oo f c L. Z.U oo _IJ c >2.f 42.) 6/.F (l.o) _JL_ 0.11. 04 7 owi. $0 *5 C.(*4 <8 7 ) (5 0 4 4* a. 4.?/ Z72. T.72_ li' . 5' ze' lcy SHE000000120 INSTRUMENT LIST WASTE WATER TREATMENT REVISIONS ETHYLENE FEEDSTOCK PROJECT - EXPANSION CASE LAKE CHARLES REFINERY Level Instruments LI-2601 LAHL-2601 LC-2601 LS-2601 and LS-2602 LG-2601 LI-2602 LS-2603 Flow Instruments FIC-2603 FRIC-2602 FT-2601 FT-2602. : FT-2603 FY-2601 FY-2602 FSL-2601 FI-2601 FI-2602 FI-2603 FI-2604 . HCV-2601 Pressure Instruments PCV-2601 PSV-2601 PG-2601 and PG-2602 PG-2603 and PG-2604 PG-2605 and PG-2606 PG-2607 PG--2608 PG-2609 Service T-2603 Level Indicator T-2603 High, Low Level Alam DAP Feed Sump Level Controller DAP Feed Pump Level Switches Saturation Column Level Gauge Polyelectrolyte Tank Level Indicator Level Switch for F-260S T-2603 Flow Control Recycle Flow Ratio Controller OAF Feed Flow Transmitter Recycle Flow Transmitter T-2603 Flow Transmitter DAF Feed Flow Transducer Recycle Flow Transducer DAF Feed Low Flow Switch DAF Feed Flow Indicator (Board) Recycle Flaw Indicator (Board) Saturation Air Flow Indicator Polyelectrolyte Dilution Water Flow Indicator Recycle Back Pressure Control Valve Saturation Air Pressure Controller Saturation Column Safety Valve DAF Feed Pump Pressure Gauges Recycle'Pump'Pressure Gauges Polyelectrolyte Pump Pressure Gauges Saturation Column Pressure Gauge Recycle Pressure Gauge P-2605 Discharge Pressure - 41 - SHE000000121 PI AMT Y -JllA.V l.( : ENGINEERING CENTER PONCA CITY. OKLAHOMA OTOPWATKM SMUT pLOwifamuMcim ' i ,'nU:y PROJECT- fcTHyie/Jfc A.P t WO _ ______ _____ _______ DATE w O NO _ __ . MAOtlY PH<> INQ.NO------------------------ 4FP*0 tv MO NO M NO____ P. o. NO Pftt^e,cT - CKEAm^iO/j CA*3 -n TAONO. 2 Whwci " JL 4 & b 7 8 mmthumomT. typi LOCATION LfWNTTTPl LOCATION Line ia. ml 1 ntewi HC-SfceS T-xbot Pieu-> FA.l<L-tOX. DAP ROC/ttF. FLCUJ COWTACI. Ppo it o ihAtic LOCAL PNlUWATlC LOCAL oRPict. 4 - HO- UH7.P-AI-1 4-P8-lA7-M-A'*-4 4- 1 +o <t 1 4 Ft- 2bi <51 DA e c F c b F LOuJ Paje u idAti e. fOAKb ( b\ ORF ILL i-BP- KI#P 1- W-rt't- 4 61 40 1 9 OHf.l*. *15 HAMM. IN. MfO TT m PACTOH 12 VALV*TYPO t3 r.Pvrt d'i SuTTtR.PLY 2.* A 1*0 avrrtRFiy V \ 3-1+5 <400 t-ao 14 LOCATION IS MATOMAL j OOVMZS IT PLUOPOMP 1 POHTMa 18 &P | MIN | NON | MAX 7T "CIlC d. 1 I 1 VALW 8. 20 AIH TO cm OH CLOH .21 MAX. CMUTOPP A P 22 Piute 23 TIIMHATVHt*P 24 MMUMNM 26 API UP. PM <*6O*Ht0l7-W-Al- 5 .5. 31 4- 00-Xjloo7Cit + 1 4* V"**- t 1 t6 I7C f >peAj ~ rs7* 175 2L4. Op'll CLOIL uiATea. =10 t*S UiATfet ISO 7*5 \ p--------------------------------------------------\l \ i N; -------------- 1-------------- 1------------- i--\v- L_lA TIR 14 54 28 m. u. a> if6. 66nB. "* 27 'm. OH, AT P. o T. "r" "l l1"' "RF ewev. AT T.0P. 100NMMM0IUTV >`0 1 29 VlKOUITI ATP.OT. 30 PATI NOHMAL cp ^ pm __________c,1^-?o 31 enn e^3 esnm *** - !`0 i 0-4*5 / 7*5 t- t. O 1 0-95 44-5 //OF 1 Cl --------------------- 1--------------------- --" 1 rue O p f tc l ISJ< c tbe. S<r.' e l-y o4 a e. i ft ci-L IpcAiRC- <K| A A/ AL<_ CfKnC L> * U Ur pipe, il Aid 11 4 yvti*.4feA, T o 1 V Vo O* 1 U Al 4 ^c. P1 . f e \>-l r e i-*^ t ljY % 40 be J,,c4S tUCHL-s c?."j Plow rp^ie c*->4-vLtft. by F`T* <! ^5^ FKlClbet. PAChAaIL To iOcluCE. *. I A. p y- Z^mt. i'Uw Uk.",ttfclL 0- Ft-lWCt. tiCJAAB mPblN *60 ALCtoO IW^kATC'1'- (^*4 fCfcl>4(R CeA-TKTu c, C-Au- CYC'S. IfcaAfcW LOWS FLtlO A'-A (Lit-, C flltPLinL 0.*pj r Aoi A-6o**-i') To \J AL\}. 5b* PLN AT <V1 AJT l ivwiVi Flu ^X-*YOI TP tL-CLukR- A. A y- run L.. CAL- l%9! / . HL- 1L-* . li(W IpAlHOulftfe. tf*n-L "'f"*v'L4 L*L> feeuj AlALin i >. FC.i>lA owlfttu teexil i .-.iaj f iu- cahtch to uuc-r oi* p-uv f nv 4'b a- A oo 1 i AY CCW FliO J>y fVTOu UT4 C> i ftt FedmfcB. Lrur ft.o<_ tctoi^, - 42 - SHE000000122 PI AMT >></ ENGINEERING CENTER PONCA CITY. OKLAHOMA SKCIPICATIOM tMMT LIQUID LEVIL INSTRUMENTS PftQJiCT- A.P.C. NO--------------------------------- OATC **//?& w.O.NO. MAOC 1Y mo. NO.. APTO SY MO. MO. AM. MO_____ Fttb:ir<-1 P.ONO. t *. si,**,*,' 8 TAQMO. MRVH* ' f r. *./ r ?ao/ te i'ti. itX`4 y<t4 lz. un / tfcrt <. t-'P t ?L'/TCW tL-.iM * SU;iw/r. WSTRUMSNY, TY* L.fsVG.1. i TC*M eti/fj su^/tcm L.l*' f :. n LOCATION C.OC.AL. n ILftMINT.TVPS LOCATION n KANOS. INOMSS H.AK. Ft.AAT AAC ApaZ -* Or>>P III 64-ii UC4T ZH* <Cfc0 JUli.ft f.M MFr C.Tft'Tif'rJ (T-'l ;-i4. nn KU 111 m KO INTtltPACS UPPtR BSNMTY. ift/eu. FT. LONOK OCNBfTY. LSJDU. FT. tvmmnatvks *p UMIUMNM A'ft - It 0<ji0 *. ?V 5L riTo o A'l ft *1/1 cl# O C.tf 7T 27X i*G a _________ 4I< I i So EQ VALVSTYPO KU n LOCATION IQ MATWRIAL KO oovsrao POMTMB 1 1 ] 1 U PIUQPONM KO AP 1 MIN. NOR. |M*X. EH CALC On VALWCN , ED AIK TO OPSN OH SLOT 1 ,1 1 11 1 I1 1 1I 1 ED 1 MAXIMUM SHU1QPP P 13 FUND ED TSMPftRATWfti *P ED PNSSSUMPMO ED f* NUU ED ED M.OA.ATP, *T. ED HUOMTft VAPOO M-OliT ED VMCOMTY ATP. ft T. ED HATS, NORMAL ED RATVi E71 ED 1___________ 1 -- ___________ 1___________ ___________ 1___________ 0) Cc i p O. r\T + * u r r fl/i t*j- < *r t u ^ ! H / c < 'f. C-Iwif. fir.-. : 4 ; -,,.Y i <- 1.. .. r fc P-TTfeoi it 4'-O'' A ^ 1 Of <*. t! r. 4 t /. 1*1 I 4 * 4 uv /. H i #5 At*n ie<* A. / i-i* : V L^- "lie Cl LO 1 bw 4TAR-T AAJO ft l tQuio UlvjltU It. 4#'0- AAJfe P'Lke6 WHIP mi. lUi jo*vfk +'<ftfc - 43 SHE000000123 B.AK.T ENGINEERING CENTER ROMCACITV. OKLAHOMA MOmCATtOM IMC8T FLOW INSTFUBItMTl *-** , OATt JSJjJjLS. maprnv PH*> Afro BY IUNA * O NO __ ino NO. _ MO NO . .. R O NO -. Ult. tKAftHt itfct'Mfi.y NROJCCT- tTHii'Cfciwe- FF-fcbilc** Pd-iK*T- txA-<asE rr 1M NO. 2 RVlG* 3 4 6 T' ? a 0 INBTRUMNT. TVT* LOCATION HIMTNT TTTR LOCATION LIN< llll,IN, | 04*. IN. ONNUU FI- 8.401 0 1 D-2.6e/ A/A. Acmj r<woic.ATeA ujATfcrt. &/ AW XAjOiOVTOfc Local. RoTC**ifcrtie. )R*5AJTh- "Litb iio-/wa|-omi-4 .4 LA t_ 4TwWfcA. V. - Oo- 7 *oi4- /*/- 4 yv 1 **o 1 1 id HANOI. IN. N0 IT MlT1RRACTOR 12 VALVT TYTR 13 14 i ! 14 NATURAL 14 mot *m 17 mjjofomt l pomtmm 18 | N | NON | MAX 19 CALC C* | L*1 C* 20 AIR TOWN ON CLOOt 21 MAX.WttfTORR AT 22 RLUtO 33 TtMMNATgM 24 NNOUNNN H tfl HA. AM 28 . on. aV are. coho. 27 IR.OR.ATR.NT. 1 "S' WCV. ATTAR, lOOMRMMBtUTT 29 VMOOWTT AT f. O T. 30 RATI NORMAL. diCFA-A 31 RATlI MM | MM LPt* i i, i i A/A zoo ; oo 1 L//>S TClY i 1 i 1 1- 11 1 ' " ' i '________ : i i i -Are^ too i /o 1 *S / j ______ B____ I____v.* 1i _____________ 1_____________ 1 _____________ i_____________ 32 (.1 To St PItw>Otb By PLT4riaU l<kmT i^c.LjCeft. t - 44 - t__ ty_____ ftv. SHE000000124 pLA^-j CAU*. CHAiLL- ENGINEERING CENTER PONCA CITY, OKLAHOMA SPECIFICATION SHEET PRESSURE INSTRUMENTS LI E NO ^ HATE /`Vt/TF MADE ay aprt> ay H M NO -- W IJ NO |N<) NO . in n no I' I* Ml . PROJECT H*1 ytfcMfe pfcl.O SfOt-W. -PAoJAeT > C^APISIT-' PUtt T 7 1 4 t> 4} 7 H y~ 10 i1 1? 13 t4 lb lt> 17 1R 19 30 ?1 n 73 2\ n 76 77 78 39 30 31 33 TAG NO SERVICE INSTRUMENT, TYPE Z *0/ fl'H P ' A t< p/essvst. c*a ix\ (,) location HANOI. P*H1 ELEMENT TYPE | MATERIAL l oCA t 0- yo nr LOCATION TimiLTuw PRESSURE mo VALVE TYPE 7USSVH LOCATION ELkYLATPA. MATERIAL oov mi | port am ------------------------ ,------------------------- PLUS P0M A P | UW | NOR. | MAX. 11 LALCCv 1 VALVE 0* AIR TO OPEN OR CLOSE MAX EHUTQPP Af IUI0 TEMPERATURE** PRESSURE PSIG > oc A> ft. IOO TccJSS 1 APT lU Wt ip or, at rro cono. PH AT PI T (Z*\ 1 HEIGHT * VAPO* in out VISCOSITY Af P. fe T ICC - 1 # HATE.NORMAL -JC^LVI RATsI MAS | MIN. 54 Cl*t Z.*' JC 1 .1 NOYIS UJ to ly viwbA> PtAtC-T AC.Tt*t ( C*tA MUHt) e*iE#i pa***op **.** SAfivrY yAbut. MSP/ t&*> 1 I \ 1 1 1 1 1 1 . 1 11 1 _____________ ________________ I________________ ________________ 1_______________ P*fctSU*6 *AA.pn*T#*. (?) TO C-TN^>u- At ft. rfT 7# p^.-j - 45 - SHEFT. SHE000000125 ENGINEERING CENTER PONCA CITY. OKLAHOMA SPECIFICATION SMCST LIQUID LEVEL INSTRUMENTS PROJECT- gruytfcufc A.F.C.NO. OATS 't' w n wo MADE Y (NO. NO AFTDBY REP- NO. EM. NOP.O.NO---------------------- LL;.k^ *. T~ ,, >^A .>:>rvs &AS< T1 TAB NO. 7 SSftVICt 3 4 a a 7 X 0 INOTMMMIfT. TYB LOCATION CLEMENT, TVPS LOCATION KANOS.INOISB INTENCACS 10 TT 12 13 14 UPPSK OENMTY. LAMM PT. LOWSR PSNMTV. LSJOU. PT. TlMPEAATUMcW PMMUNSBM VALVE TVPS IS 16 LOCATION 17 MAT1NIAL 16 OOVNZE | PONTMB 10 PUJOFOHM 20 P | MIN. INOO. (MAX. 21 CALC.0* | VALVE OP 22 Al R TO OPEN ON CLOSE 23 ' MAXIMUMSHl/TOPF AP "34 PLUG 26 TEMPERATURE *F 26 PRSSSURSPMO 27 AP1MLMJ 20 ef. on. at5?5!^5S5! 20 w. an.ATP.OT. X NSIOHT * VAPON MC-OUT 31 vtacasmr atp.rt, ep 32 MATE, NORMAL X NATSi MAX. 1 ' MB. F1B3Z3 / E - 2 40 / M 4 AY T-2fc* 4lZL_ ZMOltATDK. <GV4 TK>til<An>K. LOCAL f=4pa r T-tkoS <90 AlA-uauiO o SS.o e LI*1MOX T*2fcOft Lt^L tNCllATPA Uvft TAaD'CATp*. LocAU 0ALL ALPAr /!> T-iaoi UG AIR.. Kv>lO 0 2.1 io o 4 4.- E<r| (6> D-LVOI LEVEL 6UA4F LtvftL 4VA6E CP CAL 1&OA46. UtA^ Q.4MOI AI <4 - L l Q O >C o 61.T_ So 1 I1 1 ii i 1 11 1 1 11 1 fLOP OIL. *e> o 6Jt WATS A. C4\ ICC 1.0 13 Oti _____________ 1______________ _____________ 1_____________ _____________ 1______________ _____________ 1- 10 CX- IPOl l % TO BC A RtSifrtHTlb FK it RlftcM TAajK, SfcAUit-t . CA * L C. di A Tfe A lAL cmdulb h. CALftdN sTtfeu (jf a l- a i1 ,* rft. HASTtury ' t & i*n f,X* 2ftOI cA&Lfc. "1 w fc Cfk>wtfl.Uli lPl{.iU.'A.L. 1 UAIIOR fr-.CCp-. te> THt, Ll - 'ti,ei I.*- 1C C_ IQoiRM'.Q ll> i t m a lit Aftu <. 't . D H t, K A*OL l*?u` A'-Afr- .. . I v. < f- *-.> *.. 4k<t '* * ! ,i j w r. S'-c" A "iS'-o" LLOEuS ,, Uh(. -Ul Jt 16 ^E. t c c. A i ( t Ik' T H It ft. t, pft-mi- i'j re kc-O^1- 1C ID *5t TATn*fc"r puAut, u'llrl -u* *1* ^'yiwfeo, ikj LAb LA*\ 4. & IV1E T W > t k, . TO Itfc CUpp Li LU ty t|.BTATiew Uu'iT Vl - 46 - .CP- . RCV. SHE000000126 ENGINEERING CENTER PONCA CITV> OKLAHOMA vtctMCATtoMMrr UOUiO LEVEL INSTMUMEKTI at amt tAteg ctfA tee s 4/i PWQJtCT- A.fNO DATE maooiy APTO IV ______________ w a wo fHl INO. NO.. CQ. NO. t. M. NOP.O.NO., fetfc57ftcK A*jg.T- farft<)i*/wv <vgc TAO NO. ti-ltcl Mavtoo INIIUHMT,mi LOCATtON 5-lbOl -E.VfcL. C e/oi n b. Hm LumAric Lc CAL , auMiNT.ryot LOCATION IMQMRG PtAlb A LOAT LO CAN P*e.fcO iiiwp a* uS umuPAca uaaoo ocmntv. mow. rr. LOOM OMMTY, LAAOU. FT. niMMTVMN HHUNIM A it - wiA riA t9 4/.b i ro a - VALWOTVW EurrfcfcPLy LOCATION NAT1MAA I0BTM1 | KMT Nil t-Oo-ttaoi-r\-Te CI 1 KUO MM* FTlOidCIM CALOC* | VAkVtOr . AtA TOOFVN OK MOM MAKHflUMlMUVOM PUAO 1 Z* 1 *o 3WS, W)1 r.LO?. SO T1NFMAT\M0F IP--lUM HM ANNUM ` 4p. dpt'A1! 8WT5BBK~,~" O.MATMT, 0 'o DNiom m vamo iN-ovr VNOOBTV ATP.AT. CP NATO, MONMAA - AATtt MAX 1 NOTtSi INN. tPib 015 -.4qs i P or* 1 O 1 1 .1 1 1 lL 1 i ii L_ :_______ --i"____________ -_____________ i______________ (I'l ^ to AT "TO &. (.etATib ifj t'l'ULifcJfc UJtlA. Cl J '!''? L PQuT roft LC*2teO\ if J i* SrCI. vs TO BE T *r*c. C3) (41) UAtog. Di-sc. To U.'H itrt limns BE Lin-iiTtb io 7P TRAOfcC rtu) -ro MOO ^ pm *_ To 5*0 iiTi I\ C&LRCSPOWbf. TO VAI.u^ <t~7* ePtio at niA/imoovt J'loua - 47 - .PV_ SHE000000127 PLAN 1 asas "#|r ym V C****<LZ engineering center KONCA CITY. OKLAHOMA SPECIFICATION SHEET PRESSURE GAUGES AH NO. ___ ... dan /'v-'-C.TJL w u no . . MAOfc HY INO.NO.______ API''.) (1Y REO NO It M NO P 0 NO . ___ > ______ PROJf CT . f ,,iY<-JL.. ft f-r ' fc'.S...-**-c-T _"*'1 .J2*rfc 1 TAG ? NO. SERVICE 3 4 P-- iio*. PittiOtL 5 6 P- 1**4 LUS/^A/fPC. PRttu'iHf ft.r- e 9 p ? 10 P& ; ? V. u ffc,- 2 *>T 12 n "" " 14 6- 7 (m O 1 P/?< r: C;J P. KEC/gtr S/es.w*"l P-Z.fcoS DrtcHAfl-it. Pet' Ifi 16 17 18 19 X) 21 22 23 ?4 25 7fi 27 28 29 30 31 32 33 34 3b .16 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 INSTRUMENT RANGE PSIG t< ' (m/S n- Ct o o '/oc' P'/JO a- tf>o 0-/C.C C-tco C~ tcC C-(*o OPERATING PRESS PSIG i-S 75 7 tc a ICC is <# 5 o OPERATING TEMP F /a<> /So /To `TO . . /0c /tc /?<? )?<? ISP.. LOCATION P- ~r o P-tt-f-K ti*.'HA44E P-Zt.c4 J -zee'? 3~Zc.*t >/Z/-'4<L*L C\ - 7* C / >c- 7 **'/ -P-JHZ-fP-c.bc (iii.HAebP 1 a js 551 _ 56_i ouon- r M in v. U , NOT HE CCJNSIOEHEO If SUPPLIER OOES NOT COMPLETE RIGHT HAND (.01 'IHN - 48 - -- MU 11. .. .. Ruv J .{ SHE000000128