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8/13/2019 Refinery Overview
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Refinery
Overview
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We will seeCrude and its characteristics
Typical Refinery Configuration
Major refinery Process1.Distillation (CDU/VDU)
2.Alkylation3.Merox4.FCC ( For gas oils)5.Catalytic Cracking (Naphtha)
6.Hydro treating and Cracking7.Delayed Coking8.Sulphur Block unit (Sulphur, Sour water stripper, Amineregeneration units)
Questions ???
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3
ELEMENTAL COMPOSITION(%)RANGESELEMENTAL COMPOSITION(%)RANGES
FOR CRUDEFOR CRUDE
Carbon 83.9-86.8Carbon 83.9-86.8
Hydrogen 11.0-14.0Hydrogen 11.0-14.0
Sulphur 0.06-8.0Sulphur 0.06-8.0Nitrogen 0.02-1.7Nitrogen 0.02-1.7
Oxygen 0.08-1.8Oxygen 0.08-1.8
Metals 00-0.14Metals 00-0.14 Mainly vanadium and Nickel (Iron,Mainly vanadium and Nickel (Iron,magnesium ,Aluminum , Copper, Silver inmagnesium ,Aluminum , Copper, Silver in
traces)traces)
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4
PRINCIPAL TYPES OFPRINCIPAL TYPES OFHYDROCARBON PRESENTHYDROCARBON PRESENT
Composition of Crude oil
Paraffins:Straight chain compounds. Lighter ones are gas,heavier molecules are liquid (oil) and solid (wax).
Naphthenes:consist of carbon rings, with or without sidechains; saturated with hydrogen; Naphthenes are chemicallystable. Lighter Naphthenes are liquids but heavier ones couldbe solid.
Aromatics:compounds having a ring of 6 carbon atoms-Bzstructure they are relatively unstable.
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5
Paraffins
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6
Naphthenes
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7
Aromatics
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Classification of Crude oil Gravity as basis
API Gravity = 141.5 - 131.5
Sp. Gravity API Gravity is higher for lighter crude and lower for heavier crude.
Lighter Crude API>350
e.g, Mumbai High crude 400API
Medium Crude API between 250&340
e,g, Arabian crude: 340API
Heavy Crude API
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DIFFERENCE BETWEEN
PARAFFINC & NAPTHENIC BASE
9
Paraffinic NapthenicSP.gravity of crude Low High
Yield of gasoline High Low
Octane no.(St. run) Low HighSulphur content Low High
Smoke pt. Kerosene High Low
Cetane value HSD High LowPour point of HSD High Low
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Processing Schemes vs. type ofCrude oil
Refinery processing scheme and product
yields depend on type of crude in terms ofchemicals natureand gravity. Typically:
Paraffinic crudesare good for straight run fuel
production e.g diesel.
Light crudeyields more gasoline.
Medium crudegood for diesel production.
Heavy crudesgive better bitumen
Naphthenic crudegood for Lubricating oil.10
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11
Flow scheme of a modern refinery
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Reactions Resulting in CorrosionReactions Resulting in Corrosion
MgClMgCl22+ H+ H22O Mg(OH)O Mg(OH)22 +2HCL+2HCL
MgClMgCl22+ H+ H22S MgS +2HClS MgS +2HCl
Fe + 2HCl FeClFe + 2HCl FeCl22 +H+H22
FeClFeCl22 + H + H22S FeS + 2HClS FeS + 2HCl
Fe + HFe + H22S FeS + HS FeS + H22
HCl attacks heater tubes, trays, lining, OVHDHCl attacks heater tubes, trays, lining, OVHD
condensercondenser Corrosion controlled by neutralizing amineCorrosion controlled by neutralizing amine
injection and filming amines as inhibitorsinjection and filming amines as inhibitors
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DESALTER
CRUDE AT 120 - 140 DEG C
PROCESS WATER
LDT
LDCV
TRANSFORMER
100-120 DEG C
PDI
DESALTED CRUD
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WaterWaterCrude EmulsionCrude Emulsion
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Distillation of Crude OilDistillation of Crude OilDistillation of Crude OilDistillation of Crude Oil
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Atmospheric Distillation
Column Typical 40 to 50 actual trays No. of trays from bottom
4 to 6 bottom stripping4 to 6 flash zone/heavy gas oil
4 to 6 heavy gas oil/light gas oil
4 to 6 light gasoil/kerosene4 to 8 kerosene/heavy naphtha
4 to 8 heavy naphtha/light naphtha
2 to 3 pump arounds each Top temperature: 80 to 100 above water dew point (1200to
1300C typical)
Flash zone below cracking temperature: 3850
C typical
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Crude Distillation
Pump around Typically at product draw tray
return 2 to 3 trays above
60 to 800c temperature drop Stripping steam
Bottom: 18 to 24 kg /std m3 of RCO
Side strippers: 12 to 18 kg /std m3 ofstripped product
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Typical Op. Condns. of Crude Column
Crude Type 30 deg. API 40 deg. API
Op. Parameters
REF. DRUM
Pr., Kg/cm2(a) 3.0 3.1
temp., deg. C 45 45
COL. TOP
Pr., Kg/cm2(a) 3.5 3.6temp., deg. C 103 114
FL. ZONE Pr., Kg/cm2(a) 3.9 4.0
temp., deg. C 384 362O/F % 4 to 6 4 to 6
COT temp., deg. C 387 364.5
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Vacuum DistillationVacuum DistillationVacuum DistillationVacuum Distillation DRY DAMP WET
Top pressure mmHg a 8 25 75
Flash zone pressure mmHg a 24 42 95
Heater outlet temp.0C 395 405 420
Column dia Highest Int Least
Steam Nil Int Highest
Economics normally in favor of damp vacuum
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COLUMN INTERNALS
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22
Crude Distillation Column
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23
Vacuum Distillation Column
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24
Alkylation Alkylation combines low-molecular-weight olefins (primarily a mixture of
propylene and butylene) with isobutene in the presence of a catalyst, eithersulfuric acid or hydrofluoric acid.
The product is called alkylate and is composed of a mixture of high-octane,branched-chain paraffinic hydrocarbons.
Alkylate is a premium blending stock because it has exceptional antiknock
properties and is clean burning. The octane number of the alkylate dependsmainly upon the kind of olefins used and upon operating conditions.
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ChemistryRSH + NaOH NaSR + H2O (1)
4NaSR + O2+ 2 H2O 4NaOH + 2RSSR (2)
4RSH + O2 2RSSR + 2 H2O (3)
Reaction (1) is reverssible and favourable in forwarddirections, For
Low molecular weight mercaptans. Low temperature.
High Caustic concentration.
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operating conditions
EquipmentsEquipments TemperatureTemperature
( (00C)C)
PressurePressure
(Kg/cm(Kg/cm22g)g)
Caustic prewashCaustic prewashcolumncolumn
4545 19.519.5
11stststage CFC causticstage CFC caustic
wash contactorwash contactor4545 1818
22ndndstage CFC causticstage CFC causticwash contactorwash contactor
4848 17.517.5
Oxidizer TowerOxidizer Tower 5252 3.5-5.53.5-5.5
CFC solvent washCFC solvent wash
contactorcontactor5252 33
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CATALYTIC REFORMING
CATALYTIC REFORMING IS AN IMPORTANT PROCESS INPETROLEUM REFINING AND PETROCHEMICALS INDUSTRIES.
VALUE ADDITION TO STRAIGHT RUN NAPHTHA AND HASSIGNIFICANT INFLUENCE ON OVERALL ECONOMICS OF THEINDUSTRY
CATALYTIC REFORMING PROCESS BASICALLY CONVERTSPARAFFINS AND NAPHTHENES TO HIGH OCTANE AROMATICCOMPONENTS AND THEREBY PRODUCES
HIGH OCTANE MOTOR GASOLINE BLENDING STOCK RICH CONCENTRATES OF AROMATICS VIZ. BENZENE, TOLUENE
AND XYLENES (BTX) H2 REQUIRED IN REFINERY FOR HYDROTREATING /
HYDROCRACKING, THUS MAKING MORE ECONOMIC VIABLEPROCESS LPG AN ANOTHER VALUE ADDED PRODUCT.
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SCHEMATIC OF THE CCR PLATFORMING PROCESS
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DEHYDROCYCLISATION OF PARAFFINS
CH3 CH2 CH2 CH3 CH2 CH2 CH2 CH3
CH2 CH2 CH2CH2 CH2 CH2
H2C
H2C
H2C CH2
CH2
CH2
3H2 +
TOLUENEMETHYL CYCLEOHEXANE
(O.N. = 120)
C7H16(O.N. = 0)C7H14
CYCLI-
SATION
DEHYDRO-
GENATION
3
2
1
+ H2
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Fluid Catalytic Cracking Oil is cracked in the presence of a finely divided catalyst, which is maintained in an
aerated or fluidized state by the oil vapours.
The fluid cracker consists of a catalyst section and a fractionating section that operatetogether as an integrated processing unit.
The catalyst section contains the reactor and regenerator, which, with the standpipe andriser, form the catalyst circulation unit. The fluid catalyst is continuously circulatedbetween the reactor and the regenerator using air, oil vapors, and steam as theconveying media.
Preheated feed is mixed with hot, regenerated catalyst in the riser and combined with a
recycle stream, vapourized, and raised to reactor temperature (485-540C) by the hotcatalyst.
As the mixture travels up the riser, the charge is cracked at 0.7-2 bar.
In modern FCC units, all cracking takes place in the riser and the "reactor" merelyserves as a holding vessel for the cyclones. Cracked product is then charged to afractionating column where it is separated into fractions, and some of the heavy oil is
recycled to the riser.
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The basic process of catalytic crackingThe basic process of catalytic crackingThe basic process of catalytic crackingThe basic process of catalytic crackingThe basic process of catalytic crackingThe basic process of catalytic crackingThe basic process of catalytic crackingThe basic process of catalytic cracking
Hydrocarbon feed is brought into intimate contact with hot
catalyst The feed is vaporized and cracked and leaves behind
coke The vapors and catalyst are separated
The vapors flow into a separation section The coke-laden catalyst is brought into contact with air The coke burns and leaves behind hot regenerated
catalyst The hot catalyst is brought into intimate contact with
hydrocarbon feed and the cycle continues..
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Fluid Catalytic Cracking
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Process flow diagram - HCU
VV-2VV-1
VV-4
VV-3
VV-6
VV-5
CC-01
VV10
CC-05
VGO/CGO
M/U H2
RB-01
RB-02
FF-01
FF-02
RECYCLE H2
RB-03
RGCHHPS.
CLPS off gas
To H2 UNIT
HY. [email protected]/H
SKO
71.131T/H
HSD
48.894T/H
LPG
3.874T/H
LT. NAPH.
@14.57T/H
KA002A
154
M3/Hr
3600C/170 Kg/Cm2
3870C/170Kg/cm2R.H2
2nd STAGE
141 m3/Hr
KA003A/B/C CC-06
FF-3
157 kg/cm21.1kg/cm2
GN001
35 kg/cm2
2200C
PRT
568KW
VV13
Gas 1.482 T/H
CHPS
HHPS
HLPS
CLPS
380
4130C
4100C
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Desulfurization
R
R CH SH + H2 R CH2 R + H2S
Denitrification
RCH2CH2CH2NH2+ H2 RCH2CH2CH3+ NH3
In the reactors, sulfur and nitrogen are removed from the
feedstock. In general, the carbon skeleton of the feed molecule isnot altered by heteroatom removal; however, the boiling point ofthe molecule decreases by 27-54 C for sulfur compounds and upto 104C for nitrogen compounds.
Olefin saturation
RCH2CH=CH2+ H2 RCH2CH2CH3
Hydrocracking
RCH2CH2CH2CH3 + H2 RCH3 + CH3CH2CH3
Process Chemistry
H d d t lli ti (HDM)
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Fig. 5 Reaction mechanism for
Hydrodemetallization (HDM)
H d d lf i ti (HDS)
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Fig. 6 Postulated mechanism for Hydrodesulfurization
Hydrodesulfurization (HDS)
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Fig. 7 Typical Desulfurization reactions
Hydrodenitrification (HDN)
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Hydrodenitrification (HDN)
Fig. 8 Postulated mechanism for Hydrodenitrification
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T i l H t t
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Types of sulphur compounds
Mercaptans R-SH
Aliphatic Sulfide R-S-R
Disulphide R-S-S-R
Thiophenes
Benzo-thiophene
Typical Heteroatoms
S
C C
CC
S
C
C
S
C
C
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Nitrogen compounds
PyrroleHN
Indoles
NH
Carbazoles
NH
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Pyridine, quinolines
& acridines
Oxygen compounds Furan,
Carboxylic acids & phenols
Aromatics Benzene,
Tetralin & biphenyl
Naphthalenes and
anthracenes
N NN
OH
H2 Consumption & Heat Release
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Reaction Hydrogen Consumption BTU/SCF
Desulphurization 3 mol H2per mol of Sulfur 60
Denitrification 5 mol H2per mol of Nitrogen 65-75
Olefin Saturation 1 mol H2per mol of C=C 130-160Aromatic Saturation 3 mol H2per mol of ring Saturated. 70-85
Heat Release Thumb Rule : 130 BTU/SCF for Olefin Saturation.
60 BTU/SCF for every thing else.
Typical Classes Of Molecule in HydroprocessingParaffins Poor Pour,Cloud, Octane ; Good Cetane
Iso-paraffins Good Octane
Olefins (mono) Good Octane (comes from FCC & Coker).
Olefins (di) Foul Hydroprocessing equipment and catalyst.
Naphthenes Poor Octane, Acceptable CetaneAromatic (mono) Good Octane (Large amount in FCC Product)
Aromatic (di) Good Octane, Poor Cetane.
Aromatic (poly) Foul Hydroprocessing Catalyst
H2Consumption & Heat Release
Order Of Reaction
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Demetalization
(Metals Removal From Feed) EASY
Olefin Saturation
(Destroy Double Bond With H2)
Desulfurization
(Sulfur Removal From Feed)
S + H2H2S
Denitrification
(Nitrogen Removal From Feed)
N + H2NH3
Aromatics Saturation
Cracking
(Lower Boiling Point
C12 C8 + C4 H2 HARD
Order Of Reaction
DCU FLOW DIAGRAM
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VV-01
RFO
# 35
# 27
KERO-I
-KERO-II
183oC
251oC
CC-03
CC-04
GO
HGO
293oC
341oC
#25
# 20
GO CR
HGO CR
CC-01
FF-01
RB-01 RB-02
CC-02
445oC, 2.5 kg/cm2
EA-06
SOUR WATER
OFF GAS
425oC
P-1.75Kg/cm2
T-115oC
320oC
Cold VR
Hot VR
Slop
PREHEAT
502 oC
BFW
VV-02
DCU FLOW DIAGRAM
# 37
# 43
#29
STEAM GEN
SS
SWITCHVALVE
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OPERATING CONDITIONS
HEATER OUTLET TEMPERATURE, oC 480 510
COKE DRUM TEMPERATURE, oC 440 465
COKE DRUM PRESSURE, Kg/cm2 1 5
RECYCLE RATIO, VOL/VOL%OF FEED10 100
CYCLE TIME 24 hrs
INTRODUCTION T VISBREAKING
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INTRODUCTION To VISBREAKING
The atmospheric or vacuum residual oils are veryviscous and have high pour points. It is difficult topump them as fuel oil. Therefore, they must beblended with relatively high value distillates to meet
the finished product viscosity specification.
Visbreaking, a thermal conversion process has beenfound to be a good process which reduces the
viscosity and pour point of processed residues. Tomeet the fuel oil specifications, a small quantity ofdiluents or cutter stock (Light Gas Oil) may berequired.
Visbreaking also produces a small amount of lightgases and gasoline.
VISBREAKING
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A mild liquid phase thermal conversion process to reduceviscosity and pour point of residues (coke formation avoided) forproducing lower viscosity product suitable to use as stable fuel oil.
Products include:
VISBROKEN GASES (UP TO C4-)
VISBROKEN NAPHTHA (UP TO 150oC)
VISBROKEN FUEL OIL (150oC+)
OPTIONS FOR REFINERS
Production of visbroken gas oil to be used as diesel
Production of visbroken vacuum gas oil to be used as feed stock
for FCC operation
Production of visbroken vacuum residues to be used as refineryfuel oil
TYPICAL COMBINATION CRACKING UNIT
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Feed
Visbreaker Heater
Recycle Heater
Main Fractionator
Gas
Gasoline
Gas Oil
Vacuum
Vac.Fractionator
Residue
Operating conditions:
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Operating conditions:
Visbreaking temp. - at the heating coil outletrange from 450 - 500 C, depending on thedesign of the unit and the nature of the feed
stock.
Pressure - may vary between 4 and 20 bars,but higher pressure is often preferred, sincethis gives greater control over residence timeby minimizing vaporization.
Residence Time Temperature andresidence are interchangeable within certainlimits
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AN OVERVIEW OF SRB
ATU
ARU SWSSRU
SRB
H2S RICH GAS
NH3 RICH GAS
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SWS
GSU ARU
SRU
inciS.W.EXDCU
S.W.ex HCU
SOUR FUEL
GAS Ex DCU
SOUR
FUEL GAS
Ex HCU
SWEET FUEL GAS
(
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1/18/2013 55
Claus ProcessClaus Process
H2S O2
Catalytic ConverterCatalytic Converter
Sulphur Condenser
Further Treatment
LP Steam
Sliquid
200 - 3500
C(340 - 6600F)
130 - 2000C
(270 - 3900F)
S Yields in the range of 80 90%
3 H2S + 3/2 O2 3/x Sx + 3H2O
Modified-Claus ProcessModified-Claus Process
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Modified-Claus ProcessModified-Claus Process
Reaction Furnace
Wasteheat exchanger
Catalytic converter
Sulphur condenser
Further treatment
H2S
HP steam
LP steam
S liquid
925-12500C
(1700-23000F)
170-3500C
(340-6600F)
130-2000C
(270-3900F)
O2
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CLAUS PROCESSCLAUS PROCESSCLAUS PROCESSCLAUS PROCESS THE CONVENTIONAL CLAUS PROCESS WAS
DELOVEPED C. F. CLAUS. THE PROCESS WAS LATER
MODIFIED BY I. E. FRABENTHE PRESENT PROCESS CONSISTS OF A THERMAL
STAGE FOLLOWED BY TWO OR THREE CATALYTIC
RECTOR STAGES. THE THERMAL STAGE CONSISTS OF
REACTION FURNACE, WASTE HEAT BOILER AND
CONDENSER. IN THIS STAGE, H2S IS OXIDISED BY
COMBUSTION AIR TO SO2 ACCORDING TO THE
REACTION.3H2S +3/2O2 2H2S + SO2+H2O
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EACH CATALYTIC STAGE CONSISTS OF FEED HEATER, CATALYIST BEDEACH CATALYTIC STAGE CONSISTS OF FEED HEATER, CATALYIST BEDEACH CATALYTIC STAGE CONSISTS OF FEED HEATER, CATALYIST BEDEACH CATALYTIC STAGE CONSISTS OF FEED HEATER, CATALYIST BED
AND SULPHUR CONDENSER. CHEMICAL THERMODYNAMICAND SULPHUR CONDENSER. CHEMICAL THERMODYNAMICAND SULPHUR CONDENSER. CHEMICAL THERMODYNAMICAND SULPHUR CONDENSER. CHEMICAL THERMODYNAMIC
EQUILIBRIUM IS ESTABLISHED IN EACH BED ACCORDING TO THEEQUILIBRIUM IS ESTABLISHED IN EACH BED ACCORDING TO THEEQUILIBRIUM IS ESTABLISHED IN EACH BED ACCORDING TO THEEQUILIBRIUM IS ESTABLISHED IN EACH BED ACCORDING TO THE
CLAUS REACTIONCLAUS REACTIONCLAUS REACTIONCLAUS REACTION
2H2H2H2H2222S + SOS + SOS + SOS + SO2222 3/n Sn + 2H 3/n Sn + 2H 3/n Sn + 2H 3/n Sn + 2H2222OOOO
FOR MAXIMUM SULPHUR RECOVERY, IT IS IMPORTANT TO MAINTAINFOR MAXIMUM SULPHUR RECOVERY, IT IS IMPORTANT TO MAINTAINFOR MAXIMUM SULPHUR RECOVERY, IT IS IMPORTANT TO MAINTAINFOR MAXIMUM SULPHUR RECOVERY, IT IS IMPORTANT TO MAINTAINHHHH2222S : SOS : SOS : SOS : SO2222 MOLE RATIO OF 2:1. DEPENDING UPON THE HMOLE RATIO OF 2:1. DEPENDING UPON THE HMOLE RATIO OF 2:1. DEPENDING UPON THE HMOLE RATIO OF 2:1. DEPENDING UPON THE H2222SSSS
CONCENTRATION IN THE FEED.CONCENTRATION IN THE FEED.CONCENTRATION IN THE FEED.CONCENTRATION IN THE FEED.
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REACTION FURNACEREACTION FURNACEREACTION FURNACEREACTION FURNACE
MAIN REACTIONS
H2S + SO2 S + H2O
2H2S + SO2 2H20 + 3S
2NH3+ O2 3H2O + N2
SIDE REACTIONS
CH4+ 2O2 CO2+ 2H2O
CO2+ H2S COS + H2OCOS + H2S CS2 + H2O
2H2S + HEAT 2H2 + S2
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SOUR WATER STRIPPER
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S
T
R
I
P
P
E
R
I
S
T
R
I
P
P
E
R
II
S.W.
TANK
S / D
CBD
WPC
1001
WLC
1004
SDV
1007
SDV
1004
WPC1101
WPC
1102
WTC
1107 WFC
1105
WFF
C
1102
WTC
1103
WLC
1106
WPC1201
WTC
1205WFC
1202
WFFC
1201
WLC
1201
S.W.ex DCU SW
S.W. ex HCU SW
S.W, ex GSU
F M
COOLER
EE-
001
N2
EE
03A/B
WFC
1101
EE
002PA
001
STD.W.
COOLER
EA-02
EA-01
EE-04
EE-05
SL
SM
WLC
1102
WF
C
1002
PA
003
PA
02
PA-04
WFC1203
TO
EE01
PA
005
FLAR
E
INCI
.
FLARE
SRU-VV02
SRU-VV02
TO DCU/ETP
H2S RICH GAS
C
W
SOUR WATER STRIPPER
SOUR WATERSOUR WATERSOUR WATERSOUR WATER
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NITRGEN AND SULPHUR COMPOUNDSIN CRUDE OILS
H2S + NH3
NH3
WATER CONTAININGNH3WITH SMALL AMOUNTS OF H2S
SOUR WATERCOMPOSITION NH3 100 5000ppmw H2S 100 10000ppmw
CH, PHENOL, HCS, CO2, COOH, S-, M+
ADVERSELY AFFECTS BOILOGICAL LIFE.TREATED BEFORE DISCHARGING
REFINING PROCESSES
AMINE TREATING (-H2S)
WATER WASH
How much do we use?
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63
How much do we use?
Imagine a lake 10 miles long, 9 miles wideand 60 feet deep. Fill that lake with oil. Thatwould be about as much oil as the entireworld uses in one year. The United Stateswould use about 1/4 of it.
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1/18/2013 64
THANK YOUTHANK YOU
IOCL MATHURA REFINERY
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C
D
U
V
D
U
VBU
BBU
FCCU
OHCUDHDT
DHDS
N
S
L
H2 Plant
CRUMSQP
LPG
NAP
HVY
NAPH
ATF
KERO
AGO
NAPH
DIESEL
NAPH
DIESEL
LIQ
FUEL
VGO
VR
VR
VB TAR
VB NAPHTHA
BITUMEN
ST RUN NAPH
REFORM
F
CC
LTGASO
MS
FCC TCO
AR
LPG
LHT NAPH
HVY NAPH
KERO
DIESEL
RELIANCE JAMNAGAR REFINERY COMPLEX
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CDU
VD
U
KeroMEROX
Sat GasConcn
Delayed
Coker
VGO
HDT
DHDT
FCCU
HEAVYNAPHHDT
Gasoline
MEROX
CRUDE
Light
Kerosene
ATMResidue
Diesel
HAGO
Diesel
Unstabilis
ed
Naphtha
Naphtha
Coke to PPVacuum
Resid
LIGHTNAPH
HDT
H2 PLANT
H2
C5 -C6
Unsat gasconc.
LPGMEROX
PropyleneRecovery
LPG
Heavy kerosene
C5
-C10
NC
6/BN
Sat LPG
MEROXC3/C4
LPG
NormalButane
Recovery
N- Butane
Ga
soline
toStorage
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Source K J Pai, L &T
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Source K J Pai, L &T
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Source K J Pai, L &T
3-D Model View
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Fig.
Construction status - RefineryConstruction status - RefineryConstruction status - RefineryConstruction status - Refinery
Fi
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HCU / DHT Overall Progress:92.8%
71
Fig.4
Overview of Reliability Concerns for Hydroprocessing PlantsOverview of Reliability Concerns for Hydroprocessing PlantsOverview of Reliability Concerns for Hydroprocessing PlantsOverview of Reliability Concerns for Hydroprocessing Plants
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Richmond Isomax Fire 1989Richmond Isomax Fire 1989Richmond Isomax Fire 1989Richmond Isomax Fire 1989
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Brittle FractureBrittle FractureBrittle FractureBrittle Fracture
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Brittle FractureBrittle FractureBrittle FractureBrittle Fracture
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Richmond steam generator brittle fracture duringhydrotest
TANKAGE AREA
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Essar Oil Refinery, Vadinar
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Reaction sectionReaction sectionReaction sectionReaction section
Riser (reactor)
Maintains the feed and the catalyst in close contact as
a well-dispersed mixture while avoiding backmixing
Designed to minimise catalyst sticking to the walls
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Reaction sectionReaction sectionReaction sectionReaction section
Riser Termination Device
Designed to eliminate post-riser cracking thermal / secondary
Stripping zone
Designed to keep hydrocarbons out of the
regenerator
Reactor internalsReactor internalsReactor internalsReactor internals
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Riser Termination device
Catalyst to regen
Vapors to fractionator
Secondary cyclones
Stripper baffles