Document QJRxbz9n07Q6rYwZkdGjnM1d5
DO A 0 2 2 1 8 2
CO NFIDENTIAL
REACTIVE CHEMICAL REVIEW EDC I PROCESS
LOUISIANA DIVISION DECEMBER 14, 1989
no A
CONFTDFNTT Al
D-2 1 -80 CHLORINE KNOCK OUT DRUM
DO A 0??1R4 CONF T DFNT 1 Al
P.-21-gO
REACTIVE POTENTIAL REACTIVITY OF CHLORINE A- GREASE
TITANIUM
B. LIQUID CL2 TO THE REACTORS
SOLUTION
ONLY FOUROLUBE IS USED. ON EQUIPMENT TO BE PUT INTO CHLORINE SERVICE
NO TITANIUM FITTING IN THE PLANT
TEMPERATURE MONITORED IN CL2 HEADER
DEW POINT CALC BASED ON PURITY TEMPERATURE AND PRESSURE LEVEL ALARM AND REDUNDANT DEVICES ON THE DRUM
VESSEL IS STEAM JACKETED AND INSULATED
CHLORINE TRANSFER LINE IS INSULATED AND STEAM TRACED
D0 A 0?:M8S C.ONF T DFNT T Al
TO C-14A
AIR INJECTION
--zQ
CHLORINE
ETHYLENE
W-
R-TE SYSTEM
00 A 0??18A r ONF TDFNT TAI
R-1E REACTOR
REACTIVE POTENTIAL 1. LIQUID CHLORINE
SOLUTION
ALL CHLORINE LINES ARE STEAM TRACED
CHLORINE LIQUEFACTION TEMPERATURE IS CALCULATED FROM PRESSURE AT R-1E METER RUN
LOW CHLORINE TEMPERATURE ALARM
REACTOR SHUTDOWN AT 2.5 C OF LIQUEFACTION
2. VAPOR PHASE REACTION
DUAL LIQUID LEVEL TRANSMITTERS
LOW LEVEL ALARMS
TEMPERATURE MONITORS IN VAPOR SPACE ABOVE BED
LOW LEVEL, HIGH TEMPERATURE TRIP SCHEME
00 A D?P)S7 r0NF T OFNT TA!
3. MIXING CL2 AND C2H4 VENT STREAMS
4. REACTOR BALANCE
5. LOSS OF PLANT AIR 6. LIQUID C2H4
7. HIGH TEMPERATURE 8. LOSS OF POWER 9. AIR ADDITION SYSTEM
VENT TEMPERATURE MONITOR
TEMPERATURE IS MON ITORED AND ALARMED DOWN STREAM OF THE JET
ETHYLENE TO CHLORINE RATIO IS MAINTAINED
BY THE MOD V
REDUNDANT EXCESS C2H4 ANALYZERS ON THE VENT
CL2 AND C2H4 EBV'S FAIL CLOSED ON LOSS OF AIR
CONSTANT MONITORING OF ETHYLENE TEMPERATURE AND CALCULATION OF THE DEW POINT
HIGH TEMPERATURE ALARMS IN THE VAPOR SPACE
CL2 AND C2H4 EBV'S WILL FAIL CLOSED
TRIPS EBV'S ON LOW AIR PRESSURE TO PREVENT CONTAMINATION OF AIR AIR HEADER
no a n??iB8
CONF T OF NT T Al
C-14A EDC LIGHTS REMOVAL
no A 0??1B9 rONFTDFNTTAi
T-110 FERRIC CHLORIDE ADDITION DRUM
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C.ONf TOFNT TAI
T-110 IRON ADDITION POT
POTENTIAL
EXPLOSIVE MIXTURE IN THE VAPOR SPACE OF THE DRUM
SOLUTION
EVALUATING AN ISOLATION CHAMBER
SYSTEM
SUPPLY VERIFICATION OF DRUM
THIS IS THE ONLY PRODUCT PACKAGED IN THIS CONTAINER
TYPE
a- <r
DO A CONFTDFNTI
r,-13 TARPOT SYSTEM
nn a n??19? CONFTDFNT T Al
C-14B
00 A 0??19A
rONrTDFNTTAI
LOUISIANA DIVISION REACTIVE CHEMICALS REVIEW
ANHYDROUS HYDROGEN CHLORIDE AQUEOUS HYDROCHLORIC ACID
DECEMBER 14, 1989 BY: WAYNE MILLER
no a o?:-i94
CONF TDFNT T At
ABSORPTION UNIT
TANK VENTS. P/T
!!____________,
V 11
080
WAM 12/89
V 1 I P/T
HCL TO STORAGE
PURIFIED HCL
DO A 077195 CONFTDFNTTAl
ACID DISTRIBUTION
A0421
no A 07719f> CONFTOFNTTAl
THE SOLVENTS/EDC I PLANT RECEIVES AND PRODUCES HCL FROM THREE SOURCES. THESE PRODUCTS ARE EITHER LIQUIFIED, ABSORBED IN WATER, OR COMPRESSED AND TRANSPORTED TO THE OXYCHLORINATION PROCESS AT VINYL II. PURIFIED HCL IS ORIGINATED IN THE VINYL PROCESS AND TRANSPORTED VIA PIPELINE TO THE CHLORINATED METHANES PLANT WHERE THE ACETYLENE AND ETHYLENE IMPURITIES ARE REMOVED. IT IS THEN TRANSPORTED TO THE SOLVENTS/EDC I PLANT FOR LIQUEFACTION AND SOLD. THIS ELECTRONIC GRADE HCL HAS LITTLE REACTIVE CHEMICALS POTENTIAL EXCEPT WITH WATER AND CAN BE MIXED WITH ALL OTHER SOURCES OF HCL WITHOUT RISK. PER/TET-PRODUCED HCL IS HIGH-QUALITY HCL WHICH NORMALLY HAS NO HYDROCARBON POTENTIAL, BECAUSE THE PER/TET PROCESS OPERATES CHLORINE-RICH AT ALL TIMES. THIS MATERIAL, HOWEVER, DOES HAVE THE POTENTIAL TO CONTAIN CHLORINE AND, THEREFORE, MUST BE MONITORED CLOSELY. IF THIS STREAM DOES BECOME CONTAMINATED WITH CHLORINE, IT MUST NOT BE USED IN OXYCHLORINATION OR MIXED WITH HCL WHICH HAS EXCESSIVE ACETYLENE OR ETHYLENE. VINYL II PRODUCES HCL WHICH IS HIGH IN ACETYLENE AND ETHYLENE. THE SOLVENTS/EDC I PLANT HAS THE POTENTIAL TO ABSORB THIS HCL. HOWEVER, THIS IS NOT DONE WHEN THE PER/TET PLANT IS PRODUCING HCL, BECAUSE THE POTENTIAL TO MIX THE ACIDS WHILE PER/TET ACID CONTAINS CHLORINE WOULD CREATE A HAZARDOUS SITUATION. THIS IS PREVENTED THROUGH MOD V PROGRAMMING, WHICH ALARMS IF A FLOW FROM VINYL II IS DETECTED. ALARMS AND AUTOMATED VALVE CLOSURE IS ACTIVATED WHEN THE PER/TET PROCESS IS IN AN UPSET CONDITION.
DO A 077197 OONFTDFNTTAl
METHANES AHCL IMPURITIES
VINYL CHLORIDE METHANE ETHANE ETHYLENE ACETYLENE NITROGEN
TEMPERATURE: 30C PRESSURE: 195-200 PSIG
< 1 PPM < 10 PPM < 10 PPM < 1 PPM < 1 PPM 100-1500 PPM
PROCESS DESIGN
HIGH PRESSURE AHCL (195 PSIG) ENTERS C-80, WHICH IS A LOW TEMPERATURE COLUMN WITH TWO PACKED SECTIONS AND A FREON-22 COOLED CONDENSER MOUNTED ON TOP OF IT. LIQUEFACTION RATES ARE CONTROLLED BY LEVEL CONTROL OF THE FREON ON THE EXCHANGER. LIQUID AHCL IS LEVEL CONTROLLED TO ONE OF TWO HIGH PRESSURE CHECK TANKS (110 PSIG). THIS AHCL CAN BE LOADED BY PRESSURE ON RAIL CARS OR TRANSFERRED TO T-87 (75 PSIG). T-87 HAS AN AUTOMATED PUMPING SYSTEM WITH AUTOMATIC SHUTDOWN FOR LOADING RAIL CARS ON ELECTRONIC SCALES.
HIGH AFFINITY FOR WATER
AQUEOUS HCL IS FORMED IMMEDIATELY UPON CONTACT WITH WATER OR WATER VAPOR IN THE AIR. HEAT OF REACTION IS APPROXI MATELY 200 BTU/POUND. PRECAUTIONARY PROCEDURES TO PREVENT SUCH OCCURRENCES ARE:
ALL EQUIPMENT IS BLOWN WITH NITROGEN TO -40C
PRIOR TO PUTTING INTO HCL SERVICE.
IMPURITY REACTIONS
THIS STREAM HAS LITTLE POTENTIAL FOR IMPURITY REACTIONS DUE TO THE LOW CONCENTRATIONS OF HYDROCARBONS AND CHLOROHYDROCARBONS IN THIS STREAM. HOWEVER, THIS STREAM IS CONTINU OUSLY MONITORED FOR LOW CONCENTRATIONS OF THESE PRODUCTS DUE TO THE QUALITY REQUIREMENTS OF OUR CUSTOMERS. IF THE CONCENTRATION OF THESE IMPURITIES RISE ABOVE 5 PPM, THE COLUMN IS SHUT DOWN UNTIL THE PURIFICATION SYSTEM STABILIZES.
DO A CONFTDFNTTAl
PER/TET AHCL IMPURITIES
TOTAL HYDROCARBONS CARBON MONOXIDE/CARBON DIOXIDE CHLORINE
< 10 PPM < 500 PPM < 5 PPM
TEMPERATURE: -7 5 C PRESSURE: 12 PSIG COMPRESSED TO 120 PSIG
PROCESS DESIGN
THE AHCL/CHLORINE MIXTURE IS DISTILLED IN C-510 AND IS COMPRESSED AND TRANSPORTED TO THE HEADER TO EITHER BE ABSORBED IN THE ADIABATIC ABSORBER (C-500) OR USED IN OXYCHLORINATION AT THE VINYL II PLANT.
A LOW PRESSURE LINE WHICH BYPASSES THE COMPRESSOR IS UTILIZED AT TIMES. THE GAS FROM C-510 IS HEATED TO -10C AND ABSORBED IN C-500. THIS LINE WAS DESIGNED TO ENHANCE THE RELIABILITY OF THE PER/TET PLANT WHEN COMPRESSOR MAINTENANCE IS NECESSARY.
MOD V CONTROL IS USED TO PREVENT HCL CONTAMINATED WITH CHLORINE FROM THE OXYCHLORINATION PROCESS FROM BEING IMPORTED INTO THE SYSTEM. IF C-510 COLUMN WARMS ABOVE DESIGNED OPERATING TEMPERATURE OR THE CHLORINE ANALYZER EXCEEDS 5 PPM, THE VALVE (A0421) WILL AUTOMATICALLY CLOSE, ISOLATING THE PER/TET PROCESS FROM THE OXYCHLORINATION PROCESS.
DO A 007199 rONFTDFNTTAl
VINYL II AHCL IMPURITIES
VINYL CHLORIDE ACETYLENE ETHYLENE METHANE ETHANE NITROGEN
TEMPERATURE: 30C PRESSURE: 105 PSIG
< 1 PPM < 2500 PPM < 100 PPM
< 20 PPM < 20 PPM < 5000 PPM
PROCESS DESIGN
AHCL CAN ENTER THE SOLVENTS/EDC I PLANT VIA THE SAME LINE USED TO TRANSPORT HCL TO THE VINYL II PLANT. THIS PROCESS IS NOT UTILIZED IF THE PER/TET PLANT IS OPERATING. THIS FLOW IS MONITORED BY TWO METER RUNS INTO THE BLOCK AND IS ALARMED IF THIS CONDITION EXISTS. THIS CONDITION RARELY EXISTS, AND NO POTENTIAL FOR REACTIVITY EXISTS IF THE PER/TET PLANT IS DOWN AND NO CHLORINE IS PRESENT IN THE HCL.
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00NFT0FNTTA1
AQUEOUS HCL
HIGH CORROSIVITY AQUEOUS HCL IS CORROSIVE TO VIRTUALLY ALL COMMON METALS. PRECAUTIONS SHOULD BE USED IN SELECTION OF COMPATIBILITY OF MATERIALS IN THIS SERVICE. A. USE OF SELECT MATERIALS OF CONSTRUCTION WHICH INCLUDE
TEFLON, POLYPROPYLENE, FIBERGLASS, KYNAR, KARBATE, AND RUBBER. B. SPILLS SHOULD BE WASHED WITH COPIOUS AMOUNTS OF WATER TO NEUTRALIZE THE MATERIAL.
HAZARDOUS TO HUMANS AQUEOUS HCL READILY ATTACKS THE SKIN AND MUCOUS MEMBRANE AREAS. VAPOR INHALATION SHOULD NOT EXCEED 5 PPM.
REACTION WITH CARBON STEEL IN RUBBER-LINED VESSELS, ANY FAILURE OF THE LINER WILL EXPOSE THE METAL TO HCL. THE CORROSIVE REACTION GENERATES HYDROGEN WHICH IS HIGHLY FLAMMABLE.
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C.ONFTDFNTTAl
PURGING ACID STORAGE TANKS
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ACCUMULATION IN TANKS THE ACCUMULATION OF INSOLUBLE AND BY-PRODUCT FLAMMABLES IS A CONCERN IN THE VAPOR SPACE OF STORAGE TANKS. THIS IS PREVENTED BY THE USE OF NITROGEN PURGING OF TANKS THROUGH FLOW CONTROLLERS AND LEVEL TRANSMITTERS. THE PURGES ARE INSPECTED ON DAILY ROUNDS TO ASSURE NO INTERRUPTION OF FLOWS NECESSARY TO MAINTAIN LOW CONCENTRATIONS OF ANY FLAMMABLES IN TANKS.
no A 000003 CONFTDFNTTAI
LOUISIANA DIVISION
PER/TET REACTIVE CHEMICALS REVIEW
DECEMBER 14,1989
BY : MIKE BIZZARRO
no A o???C)4
rONFTDFNT7A(
PFR/TFT REACTOR OVERVIEW
F'AB 12-39
DO A 07'?'? O 5
rONFTOFNTTAl
PFR/TFT CONDENSING TRAIN
r-VB 12/8Q
D0 A 0???OA r.ONF- T DFNT TAl
SOLVENTS I IGHTS SEPARATION
E-550
MA5 12/89
DO A 022207 CONFTDFNTTAI
PFR/TET DISTILLATION
FILTERS
rAB 12/89
DO A fr.;,,08 rONFTOFNTTA!
HFX SVSTFM OVERVIEW
PER/TET
r-'AB i 2/69
no A 0;v;'09 CONF TDFNT TA1
PROCESS OVERVIEW
L MAJOR REACTION
CI1L C11L
H2C -- CH -- CH3
PDC
+ 6CL2
--------------- -
ccl2 =ccl2
PER
+ ecu TET
+ 6HCL
il. FEEDS
EDC
CL CL
i1 i1
h2c -- ch2
B-TRI
CL CL
i1 i 1
H2c -CH
1
CL
TCE
C|L C L HC -- C H
CL C L
CRUDE TET
CRUDE PER
III. SIDE REACTION
CCL.2 =ccl2 + CL2
PER ALSO FORMED: HCBD AND HCBZ
CCLj - ccl3
HCE
MAS 12/69
n0 A 0
CONF T OFNT T Al
PER/TET REACTIVE CHEMICAL CONCERNS
LOSS OF DILUENT - RUNAWAY REACTION
1.) AHCL IS AVAILABLE AS A BACKUP DILUENT SOURCE
CHLORINE /IRON FIRE
2.) CHLORINE AND IRON WILL REACT AT ELEVATED TEMPERATURES DURING UPSET CONDITIONS, CHLORINE MAY BE PRESENT IN THE AHCL COMPRESSOR SYSTEM. THE CU IN C-5 1 0 OVERHEADS AND THE FIRST STAGE DISCHARGE OF THE AHCL COMPRESSOR ARE CONTINUOUSLY MONITORED. ALSO MONITORED ARE THE SUCTION AND DISCHARGE TEMPERATURES OF THE COMPRESSOR. ALARMS AND TRIPS ARE ASSOCIATED WITH THIS INFORMATION TO ASSURE CONDITIONS DO NOT EXIST FOR SUCH A FIRE.
CHLORINE REACTION WITH 0IL/6REA5E
3.) ALL VALVES USED IN CL2 SERVICE ARE PROPERLY CLEANED, WRAPPED, TAGGED, AND STORED IN A SEPARATE LOCATION FROM NON-CL2 SERVICE VALVES.
DRY CHLORINE FIRE WITH TITANIUM
4.) ALL TITANIUM IN THE BLOCK IS TAGGED SO IT IS NOT INSTALLED IN DRY CHLORINE SERVICE.
B 12/39
DO A P7PP11 CONFTOFNTTAI
PER/TET REACTIVE CHEMICAL CONCERNS coni
LIQUID CHLORINE AS FEED TO REACTOR
5.) LIQUID CHLORINE FED TO THE REACTOR CAUSES INSTABILITY AND HAS IN THE PAST CAUSED VIOLENT EXPLOSIONS
THE TEMPERATURE OF THE CL2 FEED TO THE REACTOR IS CONTINUOUSLY MONITORED AND ALARMED IF IT FALLS BELOW A CALCULATED DEW POINT
REACTION BACKING INTO REACTOR INLET LINE
6.) TYPICALLY ONLY A CONCERN DURING STARTUP
INLET LINE TEMPERATURE IS MONITORED (CONTINUOUSLY DURING STARTUP) AND ALARMED. AHCL IS USED DURING STARTUP AS A DILUENT AND TO 'PUSH' THE REACTION FROM THE INLET LINE AND INTO THE REACTOR.
REACTION OF PERCHLOROETHYLENE WITH CHLORINE
7 ) PER AND CL: CAN REACT AT AMBIENT TEMPERATURES EXAMPLES INCLUDE A TAFFY POT AT CAM AND THE DISTILLATION TOWER AT CL3 IN TEXAS BOTH BLOWING UP
STANDARD OPERATING PROCEDURE PROHIBITS THE USE OF PER TO FLUSH ANY EQUIPMENT WHICH MAY CONTAIN FREE CL:. CARBON TET IS USED TO FLUSH EQUIPMENT AND AS A SOLVENT IN THE TAFFY POT OPERATION AT CL: AND CAM.
FERRIC OXIDE REACTION WITH AHCL
8 ) THE REACTION OF FERRIC OXIDE AND WATER PRODUCES WATER WHICH IN TURN FORMS AQUEOUS HCL THE AQUEOUS HCL IS HIGHLY CORROSIVE.
NEW CARBON STEEL LINES PUT IN AHCL SERVICE ARE ACIDIZED AND
PASSIVATED.
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DO a 0??^; CONFTOFNTTAl
PER/TET REACTIVE CHEMICAL CONCERNS coni.
SOLID CAUSTIC REACTION WITH WATER
9.) SOLID CAUSTIC AND WATER REACT VIOLENTLY A Dl OCCURRED IN SARNIA WHEN HOT CAUSTIC BURPED OUT OF THE TOP OF A CUASTIC POT OPERATING DISCIPLINE AND PROCEDURES ARE USED TO AVOID INCIDENTS WHEN CLEANING CAUSTIC POTS. A NEW FILTER SYSTEM ELIMINATING THE USE OF CAUSTIC IS IN THE EARLY DESIGN PHASES.
ALUMINUM REACTION WITH FREON
I 0 ) THE SOLVENTS PLANT'S REFRIGERATION MACHINE FAILED IN JUNE 1979 DUE TO A ALUMINUM/FREON 22 REACTION BOTH THE REFRIGERATION MACHINES IN THE SOLVENTS PLANT HAVE NO ALUMINUM IN CRITICAL AREAS.
LIQUID PROPYLENE AS FEED TO REACTOR
I 1 ) LIQUID PROPYLENE FED TO THE REACTOR CAUSES INSTABILITY CHANGE HYROCARBON PRIME FEED TO ETHYLENE
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LAD SOLVENTS THERMAL OXIDIZER REACTIVE CHEMICALS REVIEW
DECEMBER 14, 1989 BY: LEN CONLEY
DO A 0?P?17 OONFTDFNT TAl
LAD SOLVENTS TOX FACT SHEET
DESCRIPTION THE SOLVENTS TOX IS A HORIZONTAL, LIQUID INJECTION INCINERATOR RATED AT 23.5 MMBTU/HOUR.
FUNCTION THE THERMAL OXIDIZER WAS ORIGINALLY DESIGNED TO INCINERATE FOUR PROCESS WASTE STREAMS:
HEX WASTE
- HEAVIES PRODUCED IN PER/IET REACTOR
EDC I WASTE
- HEAVIES PRODUCED IN EDC REACTOR
TAFFY
- HEAVIES PRODUCED IN CHLORINE
PLANTS
SOLVENTS WASTE - HEAVIES DUMPED FROM PER/TET
FEED EVAPORATORS
CURRENTLY, SOLVENTS' THERMAL OXIDIZER IS UTILIZED TO DISPOSE OF SEVERAL OTHER WASTES GENERATED IN DOWS LOUISIANA DIVISION AS NEEDED.
REPLACEMENT COST: $4 MM
DO A 0???1R fONF TDFNTTAl
SOLVENTS TOX FLOWSHEET
a
COMBUSTION BLOWER
LIQUID FEEDS ..
F-700 REACTOR '
_________ /
PROCESS VENTS
uunt
jnvt*
WATR
QUENCH DRUM
HCL ABSORBER
WEST DITCH
C-7J0
CHLORINE SCRUBBER
VACUUM BLOWER
EAST DITCH
czn
STACK
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r.ONFTOFNT TAI
OPERATING CONDITION'S
1. TEMPERATURE
1100 - 1500 C
2. FEED RATE
2 - 10 GPM
3. HEAT LOAD
8 - 21 MMBTU/HR
4. TYPICAL OPERATING RATE
20 MMBTU/HR
5. CHLORINE LOAD
0 - 7000 LBS/HR
6. RESIDENCE TIME
1.59 - 3.00 SECONDS
7. PRESSURE
5 - 25 " WATER VACUUM
8. OXYGEN CONCENTRATION
3 - 10 %
9. CARBON MONOXIDE
10 - 30 PPM
10. COMBUSTION EFFICIENCY
99.98 %
11. DRE
99.9999 %
on a oppppo CONFTDFNTTAI
TOX PERMITTED SHUTDOWNS
SHUTDOWN PARAMETER
PERMIT
TIME
____ LIMIT______ DURATION
LOW TEMP
< 1,100 C
2 seconds
HIGH AIR FLOW
> 25,000 #/HR
2 seconds
LOW PRESS ON UQ. N0Z7IFS <
41 PSIG
2 seconds
LOW SCRUBBER PH
< 7.5 PH
2 seconds
LOW ABSORBER WATER FLOW < 25,000 #/HR
2 seconds
LOW SCRUBBER WATER FLOW < 50,000 #/HR
2 seconds
LOW OXYGEN
< 2.0%
2 seconds
LOW OXYGEN
< 3.0%
30 seconds
HIGH CO
> 90 PPM
60 seconds
HIGH CO ROLLING AVG
> 100 PPM
2 seconds
HIGH CHLORINE LOAD
> 7000#/HR
20 seconds
HIGH BROMINE LOAD
> 95#/HR
20 seconds
HIGH PCB LOAD
> 2.3#/HR
20 seconds
HIGH ASH LOAD
> 1.6#/HR
20 seconds
HIGH BTU LOAD
> 23 MM BTU/HR 20 seconds
DO A OPPPP1 CONFTDFNT TAl
CURRENT REACTIVE CHEMICALS CONCERNS & SOLUTIONS 1. WASTE FEED HANDLING (COMPATIBILITY/REACTIVITY) 2. VENT STREAM HANDLING (COMPATABILITY/REACTIVITY) 3. GENERAL PROCESS PROTECTION
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1. WASTE FEED HANDLING
A. TAFFY FEED: FEED COMPOSITION HIGH IN LIQUID CHLORINE. TAFFY FED INTO TOX THROUGH AN INDEPENDENT FEED SYSTEM AND NOZZLE USED ONLY FOR THIS SERVICE.
B. HEX WASTE: WASTE AT 200C AND CONTAINS FREE CHLORINE. WASTE FED TO TOX THROUGH AN INDEPENDENT FEED SYSTEM AND NOZZLE USED ONLY FOR THIS SERVICE.
C. GENERAL WASTE: REACTIVE CHEMICAL TESTING IS DONE ON ALL NEW FEEDS TO DETERMINE COMPATABILITY WITH OTHER WASTES THAT MAY COME IN CONTACT WITH THE NEW WASTE. WASTE CHARACTERIZATION SHEETS MUST BE SUBMITTED FOR ALL NEW WASTE STREAMS.
D. WASTE WITH FREE CHLORINE: PER/TET SATURATED WITH FREE CHLORINE WILL BE FED TO THE OXIDIZER THROUGH A FEED SYSTEM THAT HAS BEEN FLUSHED WITH PERCHLOR. PROCEDURES ARE WRITTEN FOR HANDLING THIS WASTE.
E. REACTIVE WASTE: WILL NOT BE INCINERATED IN SOLVENTS TOX WITHOUT APPROVAL FROM THE REACTIVE CHEMICALS
DEPARTMENT.
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OTHER POSSIBLE WASTE FEEDS
C-720 BOTTOMS: (VINYL II)
EDC BET-TRI TETRACHLOROETHANES ALPHA-DI C4H5CL3 NVM
CHLOROBENZENE
2. T-ll BOTTOMS (GLYCOL II)
3. OTHER LA. DIVISION WASTES (IF COMPATIBLE WITH SOLVENTS TOX FEEDS)
5% 11%
6% 6% 29% 1% 4%
DO A 000004 C.ONF T [IF NT T Al
COMPOSITION OF WASTE STREAMS FED TO THE THERMAL OXIDIZER
NORMAL WASTE FEEDS
1. HEX WASTE: PERCHLORETHYLENE HEXACHLOROETHANE HEXACHLOROBUTADIENE HEXACHLOROBENZENE
2. EDC I HEAVIES: ETHYL CHLORIDE EDC BETA-TRI TETRACHLOROETHANES PENTACHLOROETHANES
3 . SOLVENTS HEAVIES: CARBON TET PDC EDC BETA-TRI
TETRACHLOROETHANES PENTAS & HIGHER
4 . TAFFY: LIQUID CHLORINE CARBON TET HEXES
5. ISOPAR C: ISO OCTANE (POLY A) LUBE OIL SHORE LUBE PEROXIDE CATALYST
6. NPC WASTE: GENERAL CHLORINATED
(PPI WASTE)
HYDROCARBONS
HEXO CHLORO BUTADIENE
7. BLOCK 49: SIMILAR TO PPI WASTE
8. EB TARS
TETRAETHYLENE GLYCOL
(DOWANOLS) BUTYL ETHER
PENTAETHYLENE GLYCOL
BUTYL ETHER
HEXAETHYLENE GLYCOL
BUTYL ETHER
HIGHER ETYHYLENE GLYCOL
BUTYL ETHER
9. ETHER
DI-ISOPROPYL ETHER
(GLYCOL I) EPICHLOROHYDRIN
PDC
5 - 20% 10 - 40%
5 - 20% 30 -- 70%
0 2%
10 - 70% 10 - 50%
5 - 50% 0 -- 5%
1 _ 10% 10 - 50%
1 - 10% 5 - 30% 10 - 30% 5 - 50%
50 _ 80% 20 - 50%
1 - 5%
70 _ 80% 15 - 25%
5 10%
55 88% 10 - 30%
10%
65%
15%
5%
50% 20% 20%
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C.ONF T
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2. MIXING VENT STREAMS A. FLAMMABLE VENTS: ALL FLAMMABLE VENTS HAVE A FLAME ARRESTOR.INSTALLED IN THE VENT LINE. IN ADDITION, A NITROGEN PURGE IS MAINTAINED ON THE VENT AT THE OXIDIZER WHERE ALL COMPATIBLE PROCESS VENTS MIX. B. INCOMPATIBLE VENTS: REACTIVE CHEMICAL TESTING IS DONE TO INSURE THE COMPATIBILITY OF ALL VENTS MIXED. ANY INCOMPATIBLE VENTS (CHLORINE CONTAINING VENTS) FLOW THROUGH A DEDICATED VENT LINE AND INTO THE OXIDIZER THROUGH AN INDEPENDENT VENT NOZZLE.
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3. GENERAL PROCESS PROTECTION A. RHLA ON ALL TOX STORAGE TANKS TO PREVENT LIQUID ' FROM ENTERING FURNACE. B. TEMPERATURE ALARM ON D-700 AND P-700. C. BURNER MANAGEMENT SYSTEM ON TOX. D. ALL PURGES ARE INERT: AIR, CC14 ON TAFFY, AND PER ON OTHER SYSTEMS. E. CRITICAL INSTRUMENT CHECK.
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c.o^ ^
REACTIVE CHEMICALS TESTING
TEST NO. CHEMICAL MIXTURE
1. LARC # 173
HEXES AND DOWTHERM G
2. LARC # 174
HEXES, FERRIC CHLORIDE, DOWTHERM G
3 . LARC # 191
T-95-A AND EDC I HEAVIES
4 . LARC # 192
T-95-A AND D-700
5. LARC # 194
T-95-A AND D-67-C
6. DTA
# 86041 A-D PPI WASTE AND D-700,EDC I HEAVIES, T-95-A
7. DTA
# 87064 A
BLOCK 49 WASTE AND TOX COMPOSITE WASTE
8 . DTA
# 87065 A
DOWANOLS EB TARS AND TOX COMPOSITE WASTE
9. DTA
# 87065 B
POLY A ISOPAR C AND TOX COMPOSITE WASTE
DO A C ONFTDFNTTAI