mumbai refinery. it is your aptitude and attitude that only will determine altitude in your life
TRANSCRIPT
MUMBAI REFINERY
IT IS YOUR APTITUDE
AND
ATTITUDE
THAT ONLY WILL DETERMINE ALTITUDE
IN YOUR LIFE
• INTELLEGENCE IS QUICKNESS TO LEARN• ABILITY IS THE SKILL TO APPLY WHAT IS LEARNED• COMPETENCE IS THE ABILITY AND THE DESIRE TO APPLY WHAT IS LEARNED• DESIRE IS THE ATTITUDE THAT MAKES A SKILLFULL PERSON COMPETENT• MANY SKILLFULL PEOPLE ARE INCOMPETENT• ABILITY WITHOUT RIGHT ATTITUDE IS WASTED
LPG
NAPHTHA
PETROL
SOLVENTS
ATF
KEROSENE
DIESEL
LUBRICATING OIL
FUEL OIL
ASPHALT
CARBON BLACK FED STOCK -
HPCL - MUMBAI REFINERY PRODUCTS
DOMESTIC FUEL
PETROCHEMICALS
FERTILISERS
PLASITCS
DYES
PRIVATE TRANSPORT INDUSTRY
PAINTS
EDIBLE OIL REFINING
AVIATION TURBINE FUEL
DOMESTIC FUEL
INDUSTRY
ROAD BUILDING
SHIPPING
AUTOMOBIL / INDUSTRY
HIGH SPEED DIESEL
LIGHT DIESEL OILINDUSTRY
AGRICULTURE
TYRE INDUSTRY
CRUDE OIL
PETROLEUM HISTORY
• Col. Edwin Drake discovered oil in 1859 ,First to drill oil in village Titusville in Pennsylvania, called father of modern oil industry.
• 1865 JOHN D ROCKFELLER formed STANVAC.• 1908 oil struck in IRAN• 1927 in IRAQ• 1934 in KUWAIT• 1938 in S. ARABIA• 1950 in RUSSIA• 1960 OPEC was formed in Baghdad.• In India oil was struck in Makum near Margherita in Assam
1867
DISTRIBUTION OF CRUDE OIL RESERVES
• NORTH AMERICA 6%• SOUTH AMERICA 9 %• EUROPE 2%• FORMER SOVIET UNION 6 %• AFRICA 7 %• ASIA PACIFIC 4 %• MIDDLE EAST 65 % (PERSIAN GULF)
MAJOR OIL RESERVES IN WORLD
S. N. COUNTRY MILL. TONNES WORLD % SHARE
1 S. ARABIA 36000 25%2 IRAQ 15100 11%3 KUWAIT 13300 9%4 UAE 12600 9%5 IRAN 12300 9%6 VENEZUELA 10500 7%7 RUSSIA 6700 5%8 MEXICO 4100 3%9 LIBYA 3900 3%10 USA 3500 3%11 CHINA 3300 2%12 NIGERIA 3100 2%13 NORWAY 1400 1%14 INDIA / MAL. 600 0.5%
INDONESIA
WORLD TOP REFINERSNO. OF REFINERIES.
• U. S. A. 154 165 LAKH B/D
• CHINA 95 45 LAKH B/D
• RUSSIA 51 73 LAKH B/D
• JAPAN 35 50 LAKH B/D
• INDIA 17 23 LAKH B/D
MAJOR OIL CONSUMERS IN WORLD (MMT)
S. N. COUNTRY TOTAL OIL DEMAND OWN PRODN. OIL IMPORT
1 U.S.A. 900 350 5502 CHINA 200 160 403 RUSSIA 180 300 (-)1204 JAPAN 260 -0 2605 GERMANY 130 0 1306 FRANCE 100 0 1007 INDIA 100 36 648 S. KOREA 100 0 1009 ITALY 90 6 8410 BRITAIN 80 140 (-)6011 UKR 1312 BRAZIL 80 60 2013 MEXICO 80 170 (-) 9014 SPAIN 70 0 7015 IRAN 60 175 (-)10516 S. AFRICA 20 0 2017 S. ARABIA 60 400 (-)34018 AUSTRALIA 40 25 15
LOCATION REFINERY CPACITY PRODUCTION MMT 2004-05 MMT
NORTH IOC MATHURA 8.0 6.383IOC PANIPET 6.0 6.387
SOUTH HPCL-VIZAK 7.5 7.826CPCL 6.5 8.181KRL 7.5 7.924CPCL-NARIMANAM 0.5 0.742
EAST IOC-GUWAHATI 1 1.002IOC-BARAUNI 4.2 5.078IOC-HALDIA 4.6 5.419IOC-DIGBOI 0.65 0.651BRPL-BONGAIGAON 2.35 2.312NRL NUMALIGARH 3.00 2.042
WEST IOC KOYALI 13.7 11.701 BPCL-MUMBAI 12.0 9.138 HPCL-MUMBAI 5.5 6.119 MRPL-MANGLORE 9.7 11.809 RPL JAMNAGAR 27 34.308 TOTAL 119 127.114
OIL REFINEIES IN INDIA
HPCL PERFORMANCE CRUDE PROCESSING MMT/YR
YR CRUDE PROCESSED
MR VR
1999 - 00 10.5 6.0 4.56
2000 - 01 11.98 5.58 6.4
2001 - 02 12.33 5.63 6.7
2002 - 03 12.93 6.079 6.85
2003 - 04 13.7 6.10 7.60
2004 - 05 13.94 6.11 7.84
CRUDE OIL COMPOSITION
Elemental composition
Typically over 95% hydrogen + carbon (hydrocarbons)
Hetroatoms as undersirable contaminants ( sulphur, nitrogen,
oxygen, nickel, vanadium, iron)
Possibly thousands of compounds.
Boiling range -256 to 1000oF.
Principal organic compounds
Paraffins
Naphthenes
Aromatics Asphaltenes
PARAFINIC SERIES.
• CH4 METHANE C2H6 ETHANE C3H8 PROPANE C4H10 BUTANE C5H12 PENTANE C6H14 HEXANE C7H16 HEPTANE C8H18 OCTANE C9H20 NENONE CnH2n+2 xxx.
TYPES OF CRUDES PROCESSED AT OUR REFINERIES
REFINERY LOAD PORT COUNTRY GRADES
MUMBAI RASTANURA
RASTANURA
ZIRKU. ISLAND
BY PIPELINE
S. ARABIA
S. ARABIA
ABU DHABI
INDIA
ARAB LIGHT
ARAB MIX.
UPPER ZAKUM
BOMBAY HIGH
VISAKH VISAKH
FATEH
MINA AL AHMADI
AL BAKER
AL SHIHR
NIGERIA
INDIA
DUBAI
KUWAIT
IRAQ
YEMEN
NIGERIA
RAWA
DUBAI
KUWAIT
BASARA LIGHT
MASILA
QUAIBE
BONNY LIGHT
ESCRAVOS
FORCADOS
CABINDA
CRUDE SELECTION IS A VERY IMPORTANT PROCESS.
Once selected, refinery yields are largely predetermined.
Crude units are designed on a particular crude or crude mix and therefore running of other crudes may result in sub-optimal operation.
Constrains may be overcome by blending crudes appropriately.
The same crude in different types of refineries will give different yields.
Different crudes in the same refinery will give different yields.
Crudes And Characteristics
• SAUDI ARABIAN CRUDES.• CRUDE API SUL. WT%
Arabian Extra Lt 36.4 1.19
Arabian Heavy 27.5 2.92
Arabian Light 32.7 1.8
Arabian Medium 31.8 2.45
Arabian Super Lt 50.6 0.04
IMP. PROPERTIES OF CRUDES.
• 80/20 ARAB MIX B. H. CR.
•
• SPECIFIC GRAVITY 0.8640 0.8280
• API 32.30 39.40
• BARRELS/TONNE 7.3 7.65
• SULPHUR WT% 2.030 0.170
• POUR POINT DEC C -35.0 30.0
PETROLEUM REFINING
PETROLEUM REFINING IS A GROUP OF PROCESSES TO
CONVERT THE CRUDE OIL TO WIDE RANGE OF HIGH
VALUE AND HIGH DEMAND PRODUCTS. IT IS DIVIDED
INTO FOUR TYPES :
•SEPERATION
•CONVERSION
•TREATING
• BLENDING
SEPERATION
SEPERATION IS THE 1ST PROCESS / STEP INVOLVING A BASIC
PRINCIPLE OF DERIVING PRODUCTS BASED ON PHYSICAL
PROPERTIES LIKE MOL, WT, SIZE AND B.P. IT IS THE MOST
VERSATILE METHOD AND MOST ECONOMIC BY WAY OF
DISTILLATION. THE MOLECULAR STRUCTURE OF THE
HYDROCARBON MOLECULE REMAINS MORE OR LESS
UNCHANGED AND NO NEW COMPOUNDS ARE FORMED. THE
VARIOUS COMPONENTS ARE SEPARATED OUT FROM
DISTILLATION TOWER OVER A RANGE OF BOILING POINTS.
THESE SIDE STREAMS / CUTS DRAWN OUT FROM THE
DISTILLATION UNIT TOWER ARE THEN SUBJECTED TO
FURTHER PROCESSES TO OBTAIN THE FINAL PRODUCTS FOR
SALE.
Distillation is defined as a process in which a liquid or vapour mixture of two or more substances is seperated into its components fractions of desired purity by application and removal of heat
This process of seperating components of liquid mixture is based on their difference in boiling points.
WATER
WATER
Thermometer
Cooler / condenser
Mixture
DistillateHeat
SIMPLE DISTILLATION
WATER
EFF. WATER
CRUDE TANK
F.O. F.G.
PUMP PRODUCT
DESALTEREXCHANGER EXCHANGER
FURNACE
FBS D/O
ATF / KERO D/O
LVGO D/O
JBO D/O
HVGO D/O
RCO TO VPS
UNSATBILISED NAPHTHA TO STABILISER + COMPRESSOR
CRUDE DISTILLATION UNIT
BUBBLE CAP TRAYS
• BUBBLE CAP TRAY IS FLAT PERFORATED PLATE WITH RISER AROUND THE HOLES AND THE CAPS IN THE FORM OF INVERTED CUPS OVER THE RISER.
SIEVE TRAYS
• THE SIEVE TRAY IS A PERFORATED PLAT.VAPOUR RAISES THROUGH THE HOLES TO GIVE MULTIORIFICE EFFECT.THE VAPOUR VELOCITY KEEPS LIQUID FROM FLOWING DOMMWN THROUGH THE HOLES.
VALVE TRAYS
• THE VALVE TRAY HAS A VALVE DISKS WHICH RISE AS VAPOUR RATE IS INCREASED. THE VALVE OPENING IS ADUSTED ACCORDING TO THE THE VAPOUR FLOW. VALVE OPENING REDUCES WHEN VAPOUR FLOW IS LESS. THIS STOPS LIQUID WEEPING.
CHIMNEY TRAYS
• TRAYS USED FOR LIQUID DRAW OFFS
• NO MASS TRANSFER ACROSS THE TRAY
D/O
TYPICAL 1 - 2 SIEVE TRAY CONFIGURATIONFOR DISTILLATION COLUMN
VL
L
L L V V
V V
D/O
VALVE TRAYS
VL
V
MIDDLE DISTILLATES :- 40 to 45 %.
** Further Distilled at normal pressure to get final product or blending streams.
CRUDE SEPARATION
LIGHT ENDS :- 12 to 15 %.
** Further Distilled at high pressure ( > 120 psig. ) to separate - C3 , C4 , C5 , C6 .
HEAVY ENDS :- 35 to 40 %.
** Further Vacuum Distilled to get Lube product or blending streams.
HOT
CRUDE
WATER
EFF. WATER
CRUDE TANK
F.O.
F.G.
PUMP PRODUCT
DESALTEREXCHANGER EXCHANGER
FURNACE
FBS D/OATF / KERO D/O
LVGO D/O
JBO D/OHVGO D/O
5
12
19
32
42 / 48
RCO TO VPS
UNSATBILISED NAPHTHA TO STABILISER + COMPRESSOR
30 0C
120 0C 270 0C 365 0C
348 0C
165 0C
200 0C
260 0C
330 0C
350 0C
108 0C1.7 Kg/cm2
CRUDE DISTILLATION UNIT
PRODUCT
RCO TO VPS
CRUDE DISTILLATION TOWER
DISTILLATION COLUMN.
FBS 160 0C
ATF/ KERO201 0C
LVGO
268 0C
JBO336 0C
HVGO
351 0C
BPA
TPA
Cooler
Cooler
CRUDE from Furnace O/L.
LVN to LEU
UNSATBILISED NAPHTHA LVN
4
1
FBS
1
4
ATFSTEAM
STEAM
FBS
STEAM
STEAM
LVGO
49
55
TRAY # 1
DISTILLATE DRUMD-1001
APS T-301
4
5
BPA
RCO
STEAM
FLOW PLANE FOR FR - APS DISTILLATION SECTION
HEATED CRUDE
4
1
1
4
HVGO
LVGO
JBO
STRIPPER
STRIPPER
REFLUX
NAPHTHA
WATER
6
1
4HVGO
STEAM
12
17
21
22
20
19
TPA
28
30
3233
4243
48
51
13
ATF
O/ H Condenser
TOWER DETAILS
Bottom Section :- 8 ft. dia. x 8 ft. Ht.
Middle Section :- 16 ft. dia. x 48.75 ft. Ht.
Top Section :- 14 ft. dia. x 80 ft. Ht.
Trays 1 -- 55 :- Sieve Trays - Double pass
Tray Spacing :- 2 - 2.75 Ft.
Tray Hole Diameter - 1/2 inch.
PUMP
4
1FBS
1
4
SKO
STEAM
STEAM
FBS
SKO
4
1
1
4
STEAM
STEAM
LVGO
JBO
LVGO
JBO4
5
10
17
20
21
31
34
35
49
58
TRAY # 1
DISTILLATE DRUMD-1001
APS T-1001
TPA
BPA
RCO
STEAM
TOWER DETAILS
Bottom Section :- 8 ft. dia. x 8.8 ft. Ht.
Middle Section :- 16 ft. dia. x 77. 5 ft. Ht.
Top Section :- 12 ft. dia. x 50 ft. Ht.
Trays 1 -- 58 :- Sieve Trays - Double pass
Tray Spacing :- 2 - 3 Ft.
Tray Hole Diameter
FLOW PLANE FOR FRE - APS DISTILLATION SECTION
HEATED CRUDE
STRIPPER
STRIPPER
REFLUX
NAPHTHA
WATER
PUMP
LVN
FBS
ATF
LVGO
JBO
HVGO
RCO
VR.LPG
HEXANE
NAPHTHA
HSD
ATF
HSD/IFO
HSD/LDO
LDO/RFO
LUBE feed
LVN
FBS
KERO
LVGO
JBO
RCO
VR.LPG
SOLVENT
HSD
HSD/IFO
HSD/IFO
LSHS
L.E. L.E.
DISTILLATES
T-301
T-1001
P.G.
CRUDE
BH
CRUDE
80/20 AM CRUDE BH CRUDE
H.E.
MID
DL
E
DIS
TIL
LA
TE
S
MID
DL
E
DIS
TIL
LA
TE
S
H.E.
F.O.
F.G.
FURNACE
EXCESS VGO D/O TO DIESEL
I –SS D/O TO LUBE
II – SS D/O TO LUBE
III – SS D/O TO LUBE
4
5
9
14
VTB TO ASPHALT / DE-ASPHALTING
VGO TO DIESEL
406 0C
330 0C
165 0C
265 0C
335 0C
375 0C
112 0C-0.88Kg/cm2.
VACUUM DISTILLATION UNIT
348 0C
RCO
399 0C -.63Kg/cm2.
VACUUM DISTILLATION FOR HEAVY ENDS
VDU S.S. conversion
Sr.No
SIDE STREAM 1st Step 2nd Step 3rd Step Product
1 XVGO
(TOBS)
NMP
extracted
Hydrogenated Dewaxed Spindle oil
2 1 s. s.
( M.O.)
NMP extracted Hydrofined Dewaxed 150 N
150 turbine oil
3 2 nd S. S.
( M. O.)
NMP extracted Hydrofined Dewaxed 500 N
500 Turbine
4 3rd S. S.
(M. O. operation).
3rd S. S.(I. O.)
NMP extracted Hydrofined Dewaxed
Dewaxed
1300N
Railex
250/350
5 VTB Propane
Deasphalted
NMP extracted Hydrofined
Dewaxed Bright Stock.
LUBE PLANT OVERVIEW.PROCESS
• VDU
• (DISTILLATES / SS)
• PROPANE DEASPHALTING UNIT(PDA)
• SOLVENT EXTRACTION
• HYDROFINER
• (HYDROFINED
• RAFFINATE)
• PROPANE DEWAXING UNIT(PDU)
• (DEWAXED OIL)
CONTROL FUNCTION
• VISCOSITY, COLOR, FLASH POINT.
• VISCOSITY, COLOR, CCR
• VI
• COLOR-STABILITY, DENITRIFICATION, DE-SULPHURIZATION
• CLOUD POINT , POUR POINT
MUMBAI REFINERY
DRUM
LPG FOR TREATING
WATER
O/ H Condenser
PUMP
PUMP
PREHEATER
LANREBOILER
STEAM
MEROX UNIT
HEXANE FEED
HIGH PRESSURE DISTILLATION FOR LIGHT- ENDS FRACTIONATOR
CONVERSION
PROCESS CAUSES A CHANGE IN THE SIZE AND STRUCTURE OF
HYDROCARBON MOLECULE. IT INVOLVES A CHEM. CHANGE
OF THE PETROLEUM FRACTIONS OR STREAMS WHICH ARE
EXCESS IN ORDER TO MAKE THEM MARKETABLE AND HIGH
VALUE PRODUCTS. IF CRUDE OIL IS SUBJECTED TO
SEPERATION PROCESS ONLY THEN PRODUCT AVAILABILITY
OF REINERY WILL BE TOTALLY OUT OF BALANCE V/S MARKET
DEMANDS. HENCE ADDITIONAL PROCESSES HAVE TO BE
EVOLVED LIKE.
CONVERSION PROCESSES
SOME OF THE CONVERSION PROCESS MAINLY USED TO MAXIMISE / IMPROVE GASOLINE
A] CATALYSTIC REFORMING.
B] ALKYLATION.
C] ISOMERISATION.
D] HYDROTREATING.
E] CATALYTIC CRACKING.
F] HYDROCARCKING.
CRACKING : BREAKING DOWN OF LONG CHAIN , MOLECULE IN TO SMALL MOLECULES.
| | | | | | | | | |-C- -C- -C- -C- -C -C- -C -C- -C- -C- | | | | | | | | | |
FCCU
WAXYDISTILLATES
FUEL GAS
LPG
PETROL
DIESEL
RESIDUE
Heavy waxy oils Catalyst
Heat Light Hydrocarbons
CAB
MAB
CATFEED
REACTOR PRODUCTTo FRACTIONATOR
WASTE HEATBOILER
DILUTE PHASESPRAY
EMERGENCYSTACK SPRAY
REGENERATED CATALYST
SPENT CATALYST
RISER
CYCLONES
Fluid Catalytic Cracking Unit. ( FCCU )
FRESH CATADDITIONLINE
ROV
ROV
INJ STEAM
Gas plant
Gasoline
Gas
LPG
FRACTIONATOR REACTOR
REGENERATOR
Light Gas Oil
Heavy Gas Oil
Resid
Yields % W
5
18
40
30
12
4
To CO-Boiler
15
CAB
MAB
CATFEED
REACTORPRODUCTTO FRACTIONATOR
WASTE HEATBOILER
DILUTE PHASESPRAY
EMERGENCYSTACK SPRAY
PDRC
TT
PT
PT
STACK
TO COB
RISER
CYCLONES
STRIPPINGSTEAM
FCC REACTOR & REGEN SECTION
TT
TT
680C
TT
FRESH CATADDITIONLINE
ROV
ROV
675C
24PSIG
28PSIG
500C
508C
508C
INJ STEAM
: BLENDING
* FINAL PROCESS FOR OBTAINING THE BEST POSSIBLE PRODUCT RANGE OUT OF ANY CRUDE OIL BY JUDICIOUS MIXING OF VARIOUS SIDE STREAMS AND BY PRODUCTS.
* SOME SIDE STREAMS FROM DISTILLATION TOWERS AS WELL AS STREAMS OBTAINED FROM THE SECONDARY PROCESSING UNITS LIKE FCCU CAN NOT BE MARKETED IN ISOLATION DUE TO REASONS LIKE LACK OF DEMAND OF UNSUITABILITY OF THEIR PROPERTIES.
* THESE SS’s ARE MIXED WITH EACH OTHER AND IN APPROPRIATE RATIO AND A PROPER BELND OF “COMBINATION” IS FORMULATED TO THE REQUISITE PROPERTIES FOR SPECIFIC APPILCATIONS.
PRODUCT PROPERTIES.
• FLASH POINT : LOWEST TEMP. AT WHICH VAPOURS FROM THE OIL IGNITE INSTANTANEOUSLY.
• POUR POINT : LOWEST TEMP. AT WHICH THE OIL NO LONGER FLOW.
• FREEZING POINT: CONSTANT TEMP. AT WHICH OIL SOLIDIFIES.• VISCOSITY : A MEASURE OF RESISTANCE TO FLOW OF OIL.• RECOVERY%: PERCENT OF OIL DISTILLED AT 370 DEC. C.• SULPHUR% : SULPHUR CONTAIN IN OIL AS WT %• OCTANE NO.: DETERMINES THE ANTI-KNOCK PROPERTY OF
GASOLINE. HIGHER THE OCTANE BETTER THE ANTI-KNOCK PROPERTY OF GASO.
• VISCOSITY INDEX: dv/dt. DETERMINES LUBRICATING PROPERTY OF LUBE OIL.
IMP. SPECS OF BLENDED PRODUCTS.
• SULPHUR POUR POINT FLASH POINT. VISCOSITY RECOVERY.
• WT.% DEC.C DEC. C SSU %
• HSD 0.25/0.05 18 SUMMER 32 MIN. 50@100F 95%@ 370C
• 6 WINTER MAX.
• LDO 1.8 21 SUMMER 66 MIN. 80 @100F
• 12 WINTER MAX.
• IFO 4.0 MAX. 27 MAX. 66 MIN. 820 @ 50C
• LSHS 1.2 60 MAX 66 MIN. 14MIN TO 59MAX
• @100 C
MUMBAI REFINERY PROCESS UNITSMUMBAI REFINERY PROCESS UNITS
LPG
PG CRD
BH RCO
LPG
NAPHTHAATF/SKO
LDO
LSHS
MS
ASP./ IFO
LUBE BLOCK
LOBS
PG RCO
FR
APS
FR/LRVPS
FRE
APS
BH CRD F
CCU
L E Unit
ATF Treating
LPG
NAP
SKO/MTO
DHDS
HSD
HSD
H S D
EL HSD
“S”
FREVPS
DISTRIBUTED CONTROL SYSTEM
• DCS. CONTROL ROOM
- FLOW
- PRESSURE
- TEMPERATURE
- LEVEL
* O M & S AUTOMATION AND AUTO- PRODUCT BLENDING.
• APC.
TREATING :REFINERY OPERATION FOR REMOVAL OF UNDESIRABLE COMPONENTS OR IMPURITIES LIKE - CRUDE DESALTING FOR REMOVAL OF SALTS, SEVERAL OPTION FOR REMOVAL OF H2S OR MERCAPTANS AND AROMATICS BY VARIOUS TREATMENTS.
--H2S AND R-SH REMOVAL FROM LPG BY MEA AND
CAUSTIC TREATMENT
-- H2S AND R-SH REMOVAL FROM NAPHTHA BY MEROX
AND CAUSTIC TREATMENT
-- HYDRODESULPHURISATION OF HSD TO REMOVE
SULPHUR
- REMOVAL OF H2S AND R-SH FROM ATF BY MEROX
AND CAUSTIC TREATMENT
REFINERY PROCESS UNITS REFINERY PROCESS UNITS REFINERY PROCESS UNITS REFINERY PROCESS UNITS
• CRUDE DISTILLATION - 2
• VACUUM DISTILLATION - 3
• F C C U
• D H D S
• NAPHTHA STABILISER - 2
• NAPHTHA CAUSTIC & MEROX TREATING
• HEXANE MAXIMISATION UNIT
• LPG TREATING FACILITIES
• PROPANE UNIT
• ATF TREATING
• BITUMEN BLOWING UNIT
REFINERY PROCESS UNITS REFINERY PROCESS UNITS REFINERY PROCESS UNITS REFINERY PROCESS UNITS
REFINERY PROCESS UNITS
• LUBE EXTRACTION UNITS-3
• LUBE HYDROFINER - 2
• PRPANE DEWAXING UNIT.
• PROPANE DEASHALTING UNIT.
• BOILER HOUSE.
CAPTIVE POWER PLANT
• GTG 1, 2, 3, 4, CAP 7.18 MW EACH
STEAM 33.3 T/HR EACH
• GTG 5 CAP 20 MW
STEAM 60 T/HR
A.Mix. BH CRUDE
(Weight %)
LPG 1.1 2.4
MS 00 5.8
NAPTHA 12.6 13.4
ATF/KERO 16.5 12.0
HSD 20.2 48.8
LDO 7.3 00
LUBES 6.3 00
IFO 26.3 00
ASPHALT 8.6 00
LSHS 00 11.6
F& L 7.0 7.0
PRODUCT STATE
TOTAL PRODUCTS = 30FUELS=13 LUBES=10 SPECIALITIES=7
• FUELS PRODUCTS = 13
1 PROPANE 9 LIGHT DIESEL OIL
2 LPG 10 KERO
3 GASOLINE 11 SPL. CUT KERO
4 LOW AROMATIC NAPHTHA
5 HIGH AROMATIC NAPHTHA
6 SPECIAL CUT NAPHTHA 12 FUEL OIL NORMAL
7 AVIATION TURBO FUEL
8 HIGH SEED DISEL 13 LSHS.
TOTAL PRODUCTS = 30FUELS=13 LUBES=10 SPECIALITIES=7
• LUBE PRODUCTS=10
• NEUTRAL OILS=3
• TURBINE OILS =2
• INDUSTRIAL OILS=2
• SPINDLE OIL
• TRANSFORMER OIL BASE STOC
• BRIGHT STOCK
• SPECIALITIES = 7• HEXANE • SOLVENTS = 2• CBFS / RPO = 2• ASPHALTS =1• SULPHUR
PRODUCT MOVEMENT FACILITIES
BPT PIRPAUMANIFOLD
TROMBAYO N G C
HPHPHP
JAWAHARDWEEP
NAPHTHA,HSD,KERO/ATF
SP. OILS
TATA
LSHS
LONI,WADALA
SEWREE,MAZGAON
WADI BUNDER
BH-GAS / NGLLPG
SANTACRUZ
TERMINAL
LPG BOTTLING PLANT
BPCLREFINERY
MAHUL
VASHI
HP REFINERY
PIRPAV
M / F
BPCL REF.
HPCL REF.
NEW PIRPAV
J 1 J 2 J 3
J 4
SEWREE WADALA
C-1 C-2
W-1W-2
W-3
BOL
C-1 - CRUDE LINE
W-1 - NAPHTHA LINE
W-3 - KERO LINE
BOL- BLACK OIL LINE
C-2 - CRUDE LINE
W-2 - HSD LINE
C-1 W-1W
-1
W-2 W-3
BOL
W-2
W-3
C-1C-2
WATER
BOL
LPG
LSHS
MPT - PIPE LINE NEWTWORK
FACTORS DETERMINIG GRM
• TYPE AND QUALITY OF CRUDE.
• REFINERY TYPE HARDWARE AND COMPLEXITY.
• EFFICIENCY OF UTILIZATION OF GIVEN HARDWARE
• ENERGY EFFICIENCY OF REFINERY OPERATION.
• PREVAILING CRUDE AND PRODUCT PRICES.
• CRUDE FREIGHT COST.
ENVIRONMENT PROTECTION.
• Every component of our ecosystem is it AIR, WATER or LAND is affected due to changes in their inherent characteristics due to industrial activities
• Management of solid waste mass which is generated like sp. Catalyst, spent/used charcoal, oil sludge from storage tanks.
• Management of liquid waste like effluents going out. ETP-1, ETP-2 (pH, O&G,SS,Sulphides,COD,BOD Phenol,Temp.)
• Management of air pollutants.Air quality monitoring, furnace stack emissions control.(SPM,SO2,NOX,CO)
• ISO 14001 and environmental policy.
GFEC PROPOSED PROJECT• GREEN FUELS AND EMISSION CONTROL
PROJECT.• Bring down gasoline sulphur content from existing 1000
wppm to 150 wppm and 50 wppm for EURO3 and EURO 4 respectively.
• Octane to be incresed from existing 89 to 95 for premium gasoline and 91 for regular gasoline.
• Benzene content to be reduced to 1% vol. From 3% vol. Max
• Olefines to be reduced from existing 55vol.% to 18vol% for premium and21vol.% for normal
• Aromatics content to 42vol.% and 35vol% for euro 3 &4
EXCELLENCE
• EXCELLENCE IS A JOURNEY, NOT A DESTINATION.
• EXCELLENCE can be attained
• If You care more than others think is wise.
• Risk more than others think is safe.
• Dream more than others think is practical.
• And expect more than others think is possible.
THANK YOUTHANK YOU