CRUDE OIL REFINERY FOR SALE

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Origin:

Bahrain

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L/C

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1

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as is where basis 10 pct on signing moa subject to inspection

CRUDE OIL REFINERY FOR SALE - PLEASE OFFER TO PROSPECTIVE BUYERS
This is a HOT product in the to day hot oil marked.
15.9.13. 115,000 BPD (BARRELS PER DAY) REFINERY; CRUDE UNIT; CAPACITY
115 THOUSAND BARRELS PER DAY; DATE BUILT 1967; REVAMPED 1976, 1984, 1990, 1995;
EFFICIENCY 12.5 BARRELS OF FUEL EQUIVALENT PER THOUSAND BARRELS PER
DAY; OPERATING COSTS LESS THAN $1.50 PER BARREL; 31,000,000.00 USD
EUROPE; BT-JM-BN-SN-VW-NENMNA
THE REFINERY IS IN EXCELLENT CONDITION, HAVING HAD A TOTAL MAINTENANCE TURNAROUND IN 1995 AND CONTINUED INVESTMENT IN LATTER YEARS IT WAS ABLE TO MEET ALL EXISTING AND PROPOSED FUELS QUALITY REQUIREMENTS FOR EUROPE AND THE USA PAST THE MILLENNIUM. THE REFINERY IS UNDER NITROGEN BLANKET* (IT HAS BEEN STORED SO IT SHOULD NOT DETERIORATE DURING DISUSE);
ALL THE REFINERIES HAVE TO BE MOVED FROM WHERE THEY ARE LOCATED FOR NON COMPETE REASONS. WE HAVE ALSO LEARNED THAT THE TANK FARMS USUALLY STAY WHERE THEY ARE BUT TANKS ARE CHEAPER TO BUILD SO THE COST OF GAS FREEING THEM, CUTTING THEM DOWN AND PUTTING THEM BACK TOGETHER WOULD BE ABOUT THE SAME AS NEW BUILD ANYWAY. THE TANK BUILDING IS A SMALL PERCENTAGE OF THE COST AND TIME OF THE REFINERY SET UP.
DESCRIPTION: THE CRUDE UNIT (PLANT 1) IS A SINGLE TRAIN ATMOSPHERIC DISTILLATION UNIT CONSISTING OF: DESALTER - WITH UPDATED DISTRIBUTOR AND GRIDS (250 PSIG, 500F); EFFICIENT HEAT EXCHANGE - 27 SHELL AND TUBE HEAT EXCHANGERS (PARTIALLY BENEFITING FROM ANTI-FOULANT PROGRAM), 3 STEAM RAISERS AND 19 AIR COOLERS; FURNACE - HORIZONTAL TWIN CABIN CAPABLE OF MIXED FUEL FIRING WITH AIR PRE-HEAT; CRUDE COLUMN - 19 FEET 6 INCH. DIAMETER BY 135 FEET, 37 TRAYS WITH THREE SIDE DRAW STEAM STRIPPERS (62 PSIG, 775F); LGO VACUM DRYER - 28 THOUSAND BARRELS PER DAY 20 FEET BY 6 FEET (84 PSIG, 500F); KEROSENE CAUSTIC WASH - 30 THOUSAND BARRELS PER DAY ELECTROSTATIC PHASE SEPARATION FOLLOWED BY WATER WASH, FILTRATION/COALESCER, SALT DRYER AND CLAY TREATERS; ANALYZERS MONITORING NAPHTHA ASTM 90%, KEROSENE ASTM 90%, LGO CLOUD POINT.
THE CRUDE UNIT TAKES FEED FROM TANKAGE AND SEPARATES IT INTO OVERHEAD NAPHTHA, KEROSENE, LGO, HGO AND ATB. THE UNIT HAS INBUILT FLEXIBILITY TO OPTIMALLY PROCESS A VARIETY OF CRUDE BLENDS INCLUDING SWEET WAXY BEATRICE, THROUGH BRENT, FLOTTA, KIRKUK TO ESCRAVOS AND PENNINGTON.
TYPICAL OPERATING CONDITIONS: COLUMN INLET TEMPERATURE 710 F, OVERHEAD PRESSURE 30 PSIG.
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VACUUM UNIT
CAPACITY 42,000 BPD; DATE BUILT 1981; REVAMPED 1995; EFFICIENCY 14 BARREL OF FUEL EQUIVALENT PER THOUSAND BARRELS PER DAY;
DESCRIPTION: THE VACUUM DISTILLATION UNIT (PLANT 2) IS A SINGLE TRAIN
STAND ALONE UNIT THAT PRODUCES VGO AND FUEL OIL FROM ATB. THE PLANT WAS REVAMPED IN 1995 TO LIFT CAPACITY FROM ORIGINAL DESIGN OF 40,000 BPD TO 50,000 BPD. ALL REQUIRED MODIFICATIONS WERE INSTALLED EXCEPT AND ADDITIONAL FEED PREHEAT FURNACE AND LARGER CAPACITY FEED PUMPS.
VACUUM COLUMN 34 FEET DIAMETER; THREE STAGE STEAM EJECTOR; STRUCTURED PACKING IN WASH ZONE BED; EFFICIENT HEAT EXCHANGE; TWENTY FIVE SHELL AND TUBE EXCHANGERS; TWELVE STEAM RAISERS; SIX AIR COOLERS; FURNACE IS A TWIN HORIZONTAL CABIN DESIGN CAPABLE OF MIXED FUEL FIRING WITH AIR PREHEAT; SOUR WATER STRIPPER (POOR MECHANICAL INTEGRITY DUE TO CORROSION).
THE VDU IS DESIGNED TO RECEIVE ATB FEED FROM THE CRUDE UNIT OR FROM TANKAGE (AT DECREASED CAPACITY) AND IS A NET EXPORTER OF STEAM.
TYPICAL OPERATIONS ARE: FURNACE OUTLET TEMPERATURE 760 F; FLASH ZONE PRESSURE 25 MM HG ABSOLUTE; TOWER OVERHEAD PRESSURE 9 MM HG ABSOLUTE; FCC FEED/VAC RESIDUE TBP CUT POINT OF 1094 F AT 39 THOUSAND BARRELS PER DAY.
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DISTILLATE HYDROTREATER UNIT (1)
CAPACITY 11,000 BPD; DATE BUILT 1967; REVAMPED 1995; EFFICIENCY 15 BARRELS OF FUEL OIL EQUIVALENT/THOUSAND BARRELS OF FEED.
DESCRIPTION: DESIGNED IN 1967 USING GULFINER TECHNOLOGY, THIS UNIT (PLANT
4) IS SUITABLE FOR REMOVING SULPHUR FROM KEROSENE, GAS OIL OR LCGO. BASED ON IT'S DESIGN HAVING A WET PRODUCT STRIPPER, IT RECEIVED A MINOR REVAMP IN
1995 TO IMPROVE PRODUCT DRYING BY INCLUSION OF ADDITIONAL PRODUCT COOLING, FILTER/COALESCERS AND A LARGE SALT DRIER.
REACTOR 5 FEET 6 DIAMETER BY 17 FEET (DESIGN: 790 PSIG AT 800F); NINE SHELL AND TUBE HEAT EXCHANGERS; TEN AIR COOLERS; TWO FURNACES - GAS FIRED; THREE RECIPROCATING COMPRESSORS FOR HYDROGEN RECYCLE; TWO RECIPROCATING COMPRESSORS FOR OFF-GAS.
THIS UNIT WAS DESIGNED TO TAKE FEED EITHER DIRECTLY FROM THE CRUDE UNIT OR FROM TANKAGE.
TYPICAL OPERATING CONDITIONS WERE: TEMPERATURE AT REACTOR INLET 620 F; PRESSURE AT REACTOR INLET 600 PSIG.
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NAPHTHA HYDROTREATER
CAPACITY 38,000 BPD; DATE BUILT 1967; REVAMPED 1990; EFFICIENCY 5 BARRELS OF FUEL OIL EQUIVALENT/THOUSAND BARRELS OF FEED.
DESCRIPTION: DESIGNED IN 1967 USING GULFINER TECHNOLOGY, THIS UNIT (PLANT 6) WAS USED FOR REMOVING SULPHUR FROM ALL CRUDE UNIT OVERHEAD NAPHTHA AND GASES PRIOR TO SEPARATION INTO LPG, ISOMERISATION UNIT FEED AND REFORMER FEED IN THE DOWNSTREAM GAS PLANT. THE UNIT WAS REVAMPED FIRST TO ACCEPT FCC NAPHTHA HEART-CUT (IN 1986) AND SUBSEQUENTLY (IN 1990) TO DEBOTTLENECK TO 38,000BPD OF TOTAL NAPHTHA FEED.
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THE PLANT NOW COMPRISES: REACTOR 8 FEET 6 DIAMETER BY 21 FEET (DESIGN: 755 PSIG AT 800F); SIX SHELL AND TUBE HEAT EXCHANGERS; EIGHT AIR COOLERS; FURNACE - GAS FIRED VERTICAL CYLINDRICAL; TWO THOMASSEN RECIPROCATING COMPRESSORS FOR HYDROGEN MAKE-UP; TWO FLASH DRUMS; NAPHTHA STRIPPER COLUMN TO CONDITION FEED DRAWN DIRECT FROM STORAGE.
THE HYDROTREATER IS DESIGNED TO TAKE FEED DIRECT FROM THE CRUDE UNIT OR FROM TANKAGE.
TYPICAL CONDITIONS ARE: TEMPERATURE AT REACTOR INLET 585 F; PRESSURE AT REACTOR INLET 650 PSIG.
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PLATFORMER
CAPACITY 24,000 BPD; DATE BUILT 1967; REVAMPED 1992; EFFICIENCY 40 BARREL OF FUEL EQUIVALENT PER THOUSAND BARRELS PER DAY.
DESCRIPTION: A UOP SEMI-REGEN PLATFORMER UNIT (PLANT 7) ORIGINALLY (OVER)SIZED TO FACILITATE BOTH GASOLINE AND CHEMICALS PRODUCTION (CRUDE NAPHTHA WAS SUPPLEMENTED WITH IMPORTED NAPHTHA).
TWO RADIAL HOT WALL REACTOR 10 FEET DIAMETER BY 27 FEET (425 PSIG, 1010 F); ONE RADIAL HOT WALL REACTOR 8 FEET DIAMETER BY 23 FEET (450 PSIG, 1010 F); PACKINOX VERTICAL PLATE EXCHANGER (1992) IN REACTOR FEED/EFFLUENT SERVICE; TEN SHELL AND TUBE EXCHANGER (PLUS 12 REDUNDANT SHELL AND TUBE EXCHANGERS PREVIOUSLY IN REACTOR FEED/EFFLUENT DUTY; EIGHT AIR COOLERS (IN 4 SERVICES); FOUR CYLINDRICAL FURNACES - GAS FIRED (TWO WITH FD LOW ONx GAS BURNERS); DEMAG CENTRIFUGAL COMPRESSOR WITH 600 PSIG SIEMENS STEAM TURBINE; DE-PENTANISER 9 FEET 8 INCH DIAMETER BY 66 FEET 6 INCH, 30 TRAYS (160 PSIG,
465 F).
THE PLATFORMER WAS DESIGNED TO ACCEPT HYDROTREATED FEEDSTOCK FROM THE BASE OF THE DE-ISOHEXANISER ON THE GAS PLANT OR DIRECT FROM TANKAGE. THIS UNIT WAS LOADED WITH UOP R-62 REFORMING CATALYSTIC WHICH GAVE 18 MONTHS BETWEEN REGENERATIONS. THE UNIT OPERATED AT A REDUCED PRESSURE OF 210 PSIG AT THE REACTOR RPS.
FURTHER INFORMATION ON TYPICAL OPERATING CONDITIONS, ETC. CAN BE DIVULGED TO THIRD PARTIES ONLY AFTER THEY HAVE EXECUTED A CONFIDENTIALITY AGREEMENT WITH UOP.
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GAS SEPARATION
CAPACITY 38,000 BPD; DATE BUILT 1967; REVAMPED 1990, 1995; ENERGY MP STEAM
75 Mlb/Hr; LP STEAM 20 Mlb/Hr.
DESCRIPTION: A GAS SEPARATION PLANT (PLANT 8) FOR PRODUCING SALES GRADE PROPANE AND BUTANE AND FEED FOR BOTH THE C-5-C-6 ISOMERISATION AND PLATFORMER UNITS. THE PLANT WAS REVAMPED FOR INCREMENTAL CAPACITY IN 1990 (TO 38 THOUSAND BARRELS PER DAY NAPHTHA FEED) AND FOR ENERGY OPTIMISATION IN 1995.
DE-ETHANIZER 10 FEET / 3 FEET DIAMATER BY 96 FEET, 29 TRAYS (190 PSIG,350 F); DE-BUTANIZER 11 FEET 7 INCH / 8 FEET 2 INCH DIAMETER BY 73 FEET, 24 TRAYS (146 PSIG, 400 F); DE-ISOHEXANIZER 12 FEET DIAMETER BY 157 FEET, 70 TRAYS (COLUMN RENEWED IN 1995) (50 PSIG, 350 F); C-3-C-4 (?) SPLITTER 5 FEET DIAMETER BY 75 FEET, 32 TRAYS (225 PSIG, 250 F); AMINE ABSORBER 5 FEET DIAMETER BY 52 FEET, 18 TRAYS (288 PSIG, 300 F); MOL-SIEVE C-3/C-4(?) DRYERS; ELEVEN SHELL AND TUBE EXCHANGERS; TWENTY AIR COOLERS.
THE GAS PLANT IS A SINGLE TRAIN INTEGRATED UNIT THAT TAKES HYDROTREATED CRUDE UNIT NAPHTHA AND VARIOUS GAS STREAMS AS FEEDSTOCK. THE LARGE DE-ISOHEXANISER ALLOWS TIGHT CONTROL OF THE PLATFORMER FEED CUT.
CONSEQUENTLY BENZENE PRECURSERS CAN BE ROUTED PREFERENTIALLY TO THE ISOMERISATION UNIT FOR ELIMINATION THUS CONTROLLING TOTAL BENZENE IN FINISHED GASOLINE.
TYPICAL OPERATING CONDITIONS ARE: DE-ETHANISER COLUMN BOTTOMS 260 F, 120 PSIG; DE-BUTANISER COLUMN BOTTOMS 310 F, 90 PSIG; DE-ISOHEZANISER COLUMN BOTTOMS 260 F, 10 PSIG.
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AMINE REGENERATION
CAPACITY 2.4 THOUSAND OF BARRELS PER DAY; DATE BUILT 1967; REVAMPED 1995; ENERGY LP STEAM 4 Mlb/Hr.
DESCRIPTION: A CONVENTIONAL, EFFICIENT AMINE RECOVERY UNIT (PLANT 9) WHICH, UP TO SHUTDOWN IN DECEMBER 1997, PROCESSED A PROPRIETARY MDEA. THE UNIT WAS EXTENSIVELY REBUILT IN 1995 IN READINESS FOR LOW SULPHUR DIESEL PRODUCTION FROM MID-1996.
AMINE REGENERATOR 3 FEET DIAMETER BY 54 FEET, 22 TRAYS (50 PSIG, 350 F); FLASH DRUM 3 FEET DIAMETER BY 10 FEET t/t (90 PSIG, 350 F); FIVE SHELL AND TUBE EXCHANGERS; FOUR AIR COOLERS.
THIS IS A SINGLE TRAIN INTEGRATED UNIT THAT RECEIVES RICH AMINE FROM THE HP AND LP HYDROGEN SULPHIDE SCRUBBERS ON THE TWO HYDROTREATER AND FROM THE LPG ABSORBER ON THE GAS PLANT.
TYPICAL OPERATING CONDITIONS ARE: AMINE REGENERATOR BASE 250 F 12 PSIG.
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NAPHTHA SPLITTER
CAPACITY 13 THOUSAND OF BARRELS PER DAY; DATE BUILD 1967; REVAMPED 1993; ENERGY MP STEAM 15 Mlb/Hr.
DESCRIPTION: A GENERAL NAPHTHA SPLITTER, PLANT 11 HAS LASTLY BEEN ARRANGED
TO SPLIT REFORMATE FOR PRODUCING HIGH OCTANE HEAVY REFORMATE AS BLENDSTOCK INTO SUPER UNLEADED GASOLINE. THIS ALLOWED THE REFINERY TO REDUCE BENZENE IN THE GASOLINE POOL BY FEEDING THE OTHER PRODUCT, BENZENE RICH LIGHT REFORMATE, TO THE ISOMERISATION UNIT.
IN EARLIER SET-UP, THIS COLUMN ALSO FRACTIONATED A HEART CUT FROM FCC COMBINED NAPHTHAS TO PERMIT THE SATURATION OF CONTAINED OLEFINS IN THE NAPHTHA HYDROTREATER (PLANT 6) WHEN MIXED WITH STRAIGHT-RUN NAPHTHA. THIS COLUMN WAS ORIGINALLY (1068 TO 1981) THE FIRST COLUMN OF A UOP SULFOLANE UNIT.
SPLITTER 8 FEET DIAMETER BY 93 FEET, 30 TRAYS (50 PSIG, 500 F); FOUR SHELL AND TUBE EXCHANGER; THREE AIR COOLERS.
THE NAPHTHA SPLITTER WAS FED DIRECTLY FROM THE PLATFORMER AND RAN PRODUCT TO STORAGE AND TO THE ISOMERISATION UNIT AS REQUIRED. USE OF THE SPLITTER IN THIS MODE ALLOWED THE REFINEY TO MEET ALL NEAR TERM BENZENE IN GASOLINE SPECIFICATIONS.
TYPICAL OPERATING CONDITIONS ARE: (FOR REFORMATE SPLITTING) SPLITTER BASE
300 F 15 PSIG.
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C-5-C-6 ISOMERISATION
CAPACITY 12,500 BPD; DATE BUILT 1993; REVAMPS - NONE REQUIRED; ENERGY MP STEAM 15 Mlb/Hr; LP STEAM 30 Mlb/Hr.
DESCRIPTION: THE ISOMERISATION UNIT (PLANT 16) WAS DESIGNED AND
CONSTRUCTED BY BECHTEL IN 1993. IT IS A UOP TECHNOLOGY PENEX-MOLEX UNIT IN EXCELLENT CONDITION CONSISTING OF:
"HYDROGEN ONCE THROUGH" PENEX; TWO THOMASSEN RECIP MAKE-UP GAS COMPRESSORS; FEED AND HYDROGEN DRIERS WITH AUTOMATED DRIER REGENERATION; TWO REACTORS 8 FEET DIAMETER BY 23 FEET (545 PSIG, 500 F); SIXTEEN SHELL AND TUBE HEAT EXCHANGER; STABILISER 9 FEET / 7 FEET 6 INCH / 5 FEET 6 INCH DIAMETER BY 77 FEET, 30 TRAYS (235 PSIG, 370 F); NET GAS SCRUBBER 8 FEET /3 FEET DIAMETER BY 59 FEET, PACKED BEDS (240 PSIG, 250 F); MOLEX CHAMBER 9 FEET DIAMETER BY 45 FEET 6 INCH WITH EIGHT BEDS (350 PSIG, 400 F); UOP ROTARY VALVE -EIGHT PORTS, FOUR TRACKS; RAFFINATE COLUMN 9 FEET DIAMETER BY
137 FEET, 60 TRAYS (80 PSIG, 270 F); EXTRACT COLUMN 5 FEET 6 INCH DIAMETER BY 119 FEET Y INCH, 50 TRAYS (105 PSIG, 290 F); PARTIAL HEAT INTEGRATION BETWEEN PENEX AND MOLEX.
THE PENEX UNIT WAS DESIGNED FOR A C-4-C-6 FEED FROM A 70 TRAY NAPHTHA SPLITTER HAVING PRECISE CONTROL OF FEED COMPOSITION. PENEX INCREASED THE OCTANE AND REMOVES BENZENE. MOLEX REMOVES C-4 AND RECYCLES LOW OCTANE N-PARAFFINS TO PENEX. ISOMERATE PRODUCT IS 89 RON, 85 MON GASOLINE BLEND COMPONENT.
INFORMATION ON TYPICAL OPERATING CONDITIONS, ETC. CAN BE DIVULGED TO THIRD PARTIES ONLY AFTER THEY HAVE EXECUTED A CONFIDENTIALITY AGREEMENT WITH UOP.
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SULPHUR RECOVERY
CAPACITY 13 TPD (TONS PER DAY); DATE BUILT 1980; REVAMPED 1996; S RECOVERY 95%.
DESCRIPTION: THE ORIGINAL UNIT (PLANT 14) WAS BUILT AS A SKID MOUNTED UNIT IN 1980 BY SNAMPROGETTI BUT WAS NEVER COMMISSIONED DUE TO INSUFFICIENT SOUR FEED GAS AVAILABILITY FROM THE PROCESSING FROM THE PROCESSING OF NORTH SEA CRUDES.
IN PREPARATION FOR THE PRODUCTION OF LOW SULPHUR DIESEL TO MEET NEW LEGISLATION IN 1996, SNAMPROGGETTI REBUILT THE SULPHUR RECOVERY UNIT TO IMPROVE OPERABILITY AND TO LIFT CAPACITY TO 13 MT PER DAY OF PRODUCT SULPHUR. THE ORIGINAL SULPHUR RECOVERY EFFICIENCY OF 95% WAS RETAINED FOR THE REVAMP AS IT WAS IMPOSSIBLE TO RETRO-FIT ANY TAIL GAS TREATMENT FACILITIES.
THE UNIT OPERATED SUCCESSFULLY BETWEEN AUTUMN 1996 AND NOVEMBER 1997.
EQUIPMENT COMPRISES: REACTOR FURNACE WITH DUIKER BURNER; TW REACTORS (CRS
31 CATALYST NOW REMOVED); LIQUID SULPHUR STORAGE PIT WITH LOADING ARM; LP STEAM GENERATOR; INCINERATOR; TWO AIR COMPRESSORS.
TYPICAL OPERATING CONDITIONS WERE: REACTOR FURNACE 2000 F, 6 PSIG.
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NITROGEN, NATURAL GAS, FUEL GAS, FUEL OIL, COOLING WATER; DATE BUILT 1967.
DESCRIPTION: THE REFINERY PROCESS UNITS HAVE GENERAL FACILITIES TO SUPPORT
OPERATIONS (PLANT 15).
TWO LIQUID NITROGEN STORAGE TANKS; NATURAL GAS SUPPLY AND CONTROLS; PROPANE VAPORISER FOR REFINERY FUEL GAS MAKE UP; FACILITY TO STORE AND DISTRIBUTE VACUUM RESIDUE AS REFINERY FUEL OIL; FIVE COOLING WATER CELLS WITH INDUCED DRAFT.
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REFINERY TDC 2000/3000 SYSTEM
THE REFINERY MONITORING AND CONTROL SYSTEMS ARE BASED AROUND HONEYWELL TDC 2000/3000. THERE ARE INTEGRATED DATA HIGHWAY, LOCAL CONTROL AND UNIVERSAL CONTROL NETWORK DEVICES INSTALLED IN THE THREE CONTROL ROOMS.
1. DATA HIGHWAY (DH)
THIS IS THE ORIGINAL TDC 2000 RANGE OF EQUIPMENT WHICH IS INSTALLED IN THE PROCESS AREA CONTROL ROOM. IT CONSISTS OF BASIC CONTROLLER FILES, LOW AND HIGH LEVEL PROCESS INTERFACE UNITS AND UNINTERRUPTED AUTOMATIC CONTROLLERS.
SOME OF THIS EQUIPMENT HAS BEEN IN OPERATION SINCE 1978 WHEN THE GULF REFINERY MADE THE STRATEGIC DECISION, AS PART OF A REINSTRUMENTATION PROJECT, TO INSTALL DISTRIBUTED CONTROL SYSTEM. OVER A PHASED IMPLEMENTATION, STARTED IN 1978 AND COMPLETED IN 1981, ALL PROCESS AREA BASED CONTROL AND MONITORING SYSTEMS WERE RELOCATED ONTO TDC 2000.
THE REMAINING DATA HIGHWAY BASED HARDWARE STILL IN OPERATION CONSISTS OF THE
FOLLOWING: BASIC CONTROLLER FILES 62; UNINTERRUPTED AUTOMATIC CONTROLLERS
8; LOW LEVEL PROCESS INTERACE UNIT 4; HIGH LEVEL PROCESS INTERFACE UNITS
2; HIGHWAY TRAFFIC DIRECTORS 2.
2. LOCAL CONTROL NETWORK (LCN)
THE OPERATOR INTERFACE CONSOLES -2 OFF - IN THE PROCESS AREA CONTROL ROOM WERE REPLACED BY TDC 3000 UNIVERSAL OPERATOR STATIONS IN 1990. AT THE SAME TIME, AS PART OF CAPITAL EXPENDITURE PROJECTS, NEW PROCESS INTERFACE INPUT/OUTPUT SYSTEMS USING ADVANCED PROCESS MANAGERS AND A THIRD OPERATOR/ENGINEERING CONSOLE FOR PROCESS MONITORING AND SYSTEM CONFIGURATION WERE INSTALLED.
THE TWO MAIN OPERATOR CONSOLES ALSO INCORPORATE HARD-WIRED ALARMS, EMERGENCY TRIP SWITCHES AND STATUS LIGHTS. THERE ARE SIX SCREENS/CONSOLE, FOUR OPERATOR KEYBOARDS, ONE "QWERTY" KEYBOARD AND ONE BERNOULLI CARTRIDGE. THE ENGINEERING CONSOLE CONSISTS OF TWO SCREENS AND OPERATOR KEYBOARDS, ONE "QWERTY" KEYBOARD AND DOUBLE BERNOULLI CARTRIDGE DRIVES.
THE NETWORK CABINETS CONTAIN HISTORY MODULES, APPLICATIONS MODULES, HIGHWAY GATEWAYS AND PLC GATEWAYS. AL UPGRADED TO K2 LEVEL BOARDS.
THERE IS A SEPARATE LCN IN THE COGENERATION CONTROL ROOM WHICH IS LINKED TO THE MAIN PROCESS AREA CONTROL ROOM VIA FIBRE OPTIC CABLES. THIS LCN CONSISTS OF A TWO SCREEN OPERATORS' CONSOLE, HISTORY MODULE, NETWORK INTERFACE MODULES AND PLC GATEWAY. [NOTE THAT THE CHP PLANT AND ASSOCIATED EQUIPMENT IS BEING RETAINED AND OPERATED BY...]
THE PROCESS INTERFACE HARDWARE IS ADVANCED PROCESS MANAGERS WITH VARIOUS COMBINATIONS OF ANALOGUE AND DIGITAL I/0 CARGDS. THE CABINET POWER SUPPLIES AND ANALOGUE I/O CARDS ARE FULLY REDUNDANT.
A FULL HARDWARE INVENTORY OF THE MAIN HONEYWELL NODES IS AS FOLLOWS:
UNIVERSAL OPERATOR STATIONS 16; NETWORK INTERFACE MODULES 4 (2 REDUNDANT PAIRS); HISTORY MODULES 4; APPLICATIONS MODULES 2; HIGHWAY GATEWAYS
2(2 REDUNDANT PAIRS); COMPUTER GATEWAYS 2; ADVANCED PROCESS MANAGERS 6.
3. OIL MOVEMENTS TDC 3000.
A TDC 3000 SYSTEM IS USED FOR MONITORING AND CONTROL OF A NUMBER OF MAJOR AREAS OF OIL MOVEMENTS. THIS SYSTEM WAS INSTALLED IN 1996.
SINCE THE TANK FARM AND ALL ASSOCIATED EQUIPMENT IS BEING RETAINED AND OPERATED BY..., NO FURTHER INFORMATION IS GIVEN HERE.
THE EXTERNAL ELECTRICITY SUPPLY IS VIA 2-OFF 132 Kv OVERHEAD LINES RATED AT 50MVA. THESE LINES THEN FEED 20FF 132 Kv TO 11 Kv, 30 MVA TRANSFORMERS, WHICH IN TURN SUPPLY AN 11 Kv DISTRIBUTION SWITCHBOARD. ALL THIS EQUIPMENT IS THE PROPERTY OF SWALEC. THE REFINERY DOES HOWEVER, OWN 2 OIL CIRCUIT BREAKERS WHICH ARE PART OF THIS 11 Kv SWITCHBOARD.
THE SITE DISTRIBUTION NETWORK IS AT 11 Kv, WHICH IS THEN TRANSFORMED DOWN TO
415 v AND 3.3 Kv AND THEN TO INDIVIDUAL LOADS FROM 10 SITES SUBSTATIONS.
THESE SUBSTATIONS ARE BRICK BUILDINGS, WHICH HOUSE 11 Kv SWITCHBOARDS, 415 v AND 3.3 Kv MOTOR CONTROL CENTERS. THE SITE DISTRIBUTION TRANSFORMERS ARE EXTERNAL TO THE SUBSTATIONS IN INDIVIDUAL SEGREGATED BAYS.
THE 11 Kv DISTRIBUTION SWITCHGEAR IS ALL 350 MVA RATED, OIL CIRCUIT BREAKERS. THE LOW AND MEDIUM VOLTAGE MOTOR CONTROL CENTERS ALL HAVE INCOMING CIRCUIT BREAKERS, WHICH ARE A MIXTURE OF OIL, VACUUM AND AIR BREAK OPERATION. ALL MOTOR STARTERS ARE DIRECT ON-LINE OPERATION.
THEE ARE A TOTAL OF 61, 11 Kv CIRCUIT BREAKERS, MOST OF WHICH WERE INSTALLED IN 1968. ALL THESE CIRCUIT BREAKERS ARE BVP17 MODEL, MANUFACTURED BY G.E.C.
LTD.
MOST OF THE TRANSFORMERS WERE INSTALLED AT THIS TIME, BUT SOME HAVE BEEN UPGRADED DUE TO PLANT EXPANSIONS. THERE ARE 32 TRANSFORMERS, WHICH ARE ALL OIL IMMERSED, WITH OIL CONSERVATOR AND NATURAL AIR COOLING. THEY ARE ALL STAR/DELTA WOUND FOR VECTOR GROUP Yd-1. MOST TRANSFORMERS ARE EITHER BRUSH OR S.W.S. LTD MANUFACTURE.
THERE ARE 11, 3.3 Kv AND 24, 415 VOLT MOTOR CONTROL CENTERS OF DIFFERENT MANUFACTURE AND AGE. HOWEVER, THE REFINERY COMPLETED AN UPGRADING EXERCISE IN THE PROCESS AREA, IN WHICH MOST 415 VOLT m.c.c's WERE CHANGED AT THE SAME TIME. THE RECENT 415 VOLT m.c.c's ARE ALL ALLENWEST AMD TJE 3/3 Lv m.c.c's ARE HAWKER SIDDLEY.
THIS IS THE KIND OF MONEY THAT THE BUYER HAS TO HAVE IN ORDER TO BE A VIABLE BUYER OF A REFINERY THIS SIZE. THE SELLER WILL NOT DEAL WITH ANYONE WHO DOES NOT SHOW EVIDENCE OF THIS AMOUNT OF MONEY. TOTAL IS $452,000,000. TO $502,000,000. OPERATING COSTS LESS THAN $1.50 PER BARREL; 115,000 BPD:
1 PURCHASE 31,000,000.00 USD (PLUS ANY TAXES REQUIRED IN BUYER'S COUNTRY);
2 MARK, TAG, SUPERVISE LOAD OUT AND SHIP OVER ABOUT 1 TO 2 YEARS $50,000,000.
3 PREPARE SITE, SET UP AND MAKE INITIAL TEST/TRAINING RUN $250,000,000.TO $300,000,000.
4 CRUDE AND PRODUCT TANK FARM AND CRUDE OIL STOCK OPERATING CAPITAL TO
HOLD SUPPLY OF ABOUT 3,000,000 BBL, 30 TO 45 DAYS SUPPLY $125,000,000.
5 TOTAL IS $ 452,000,000. TO $ 502,000,000.
6 A REFINERY LIKE THIS WITHOUT LAND, SHIPPING AND ACCESSORY EQUIPMENT
COSTS $1.15 BILLION NEW. AND THIS WILL HAVE A USEFUL LIFE OF ABOUT 20 YEARS WITH NORMAL MAINTENANCE.
OPERATING COSTS LESS THAN $1.50 PER BARREL; 31,000,000.00 USD EUROPE; BT-JM-BN-SN-VW-NENMNA

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