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LNG Process Units
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LNG PROCESS TRAIN
01-MD01
68.8 Bar107.7 C
01-MC 0131.5 Bar34.5 C
66.7 Bar39.6 ºC
14-MD01
14-MD02
01-IC01
5m01-MJ01
NG 12-MD
27
12-MD
22
12-MD
21
MD
02-A
MD
02-C
13-MD01
MD
02-B
13-MC01
13-MD03
13-MC02
13-MD04
15-MC0115-MC02
15-MC03
MD02
15-MD
01
15-MJ01
15-MJ02
15-MC-05
MD
03
15-MJ0371-MF01/2
MJO1_2A/B/CLoading Arms
71-MJ05
7-MD
01
7-MD
02
MD08 MD03
12-MJ2212-MJ24
7-MJ017-MJ04
16-MJ01 16-MJ02 16-MJ03
16-MJ04
16-MD
01
MD06
C3 Liquid to Chillers
16-MC 09
16-MC04/05/06/07
HP F/G
46.3 ºC
65.2 Bar40.5 C
1.65 Bar71.1 C
1.8 Bar103 C
Vent
64.7 Bar22 C
63 Bar22 C
62 Bar-16 C
61.4 Bar-31.4 C
47 Bar-147.1 C
5.2 Bar-159.1 C
Unit 13
18 Bar68.3C
17.1 Bar50C
7.1 Bar14.6C 4.2 Bar
-3.5C2.3 Bar-21C
1.3 Bar-34.9C
63 Bar89.8C
4.3 Bar-34.4 C
59.5 Bar-42.8 C
61.4 Bar-31.4 C
21.5 Bar67.7 C
33.1 Bar72.8 C
3.9 Bar-33.8 C 61.2 Bar
-29.4 C
29 Bar-28.6 C
26.3 Bar0.2 C
7-MD03
C3C4C5
6. Bar-29.7 C
6. Bar-29.7 C
16-MC01 16-MC02 16-MC03
16-MD01
16-MJ06
Presley Wong
20/06/2003
± 70 Bar15 - 35 C
UNIT 01PRESSURE REDUCTION & METERING STATION
MD 02
PV
GMS
GMS
GMS
GMS
Gas Metering Run 1
MD 02
MD 02
MD 02
PV
MD 02
PV
PV
PV
MD 02 MD 02
Damietta -1
Water boilers
Filters/ separators
Damietta - 2
Feed Gas
Ex. G
rid
Temporary PRSSSO
SSO
FiltersPV PV
PV PV
Gas Metering Run 2
The purposes of Pressure Reduction & Metering Station are to preheat the feed gas from National Gas Grid to prevent hydrate formation & to maintain feed gas pressure to suction of feed gas compressor. It is also to meter the quantity of feed gas being produced in the downstream Liquefied Natural Gas (LNG) processing plant. The Temporary Pressure Reduction Station is a mean of fuel gas supply to run Gas Turbine Generator during plant initial start-up.
Mercury Absorber
68.8 Bar107.7 C
M
Warm LiquidHeader
PI 3004
Presley Wong20/06/2003
±33 Bar15 - 35 C
Feed Gas Ex. GASCO
PDI 3006
PDI 3007
FQI 3001
TI 3011
PI 3009
FI 3002
TI 3010
PI 3008
FI 3001
FQI 3002
UNIT 01PLANT FEED CONDITIONING
AI 305F
IC5 AI 305G
nC5 AI 305I
C6+
AI 305O
LHV AI 305P
HHV AI 3050
C2H
AI 305A
C1AI 305B
C2AI 305C
C3 AI 305D
IC4 AI 305E
nC4
AI 305J
N2 AI 305K
CO2 AI 305L
RD AI 305N
IWISWIAI 305M
XV3017
XV3018
M
M
31.5 Bar34.5 C
Common FGMake-up Unit 55
HP FG Make-up to Train 1 Unit 15
BOG Ex.Unit 71
01-MD01
01-MJ01
31.2 Bar34.5 C
01-MC 01
M
1 3 5 7
2 4 6 8
68 Bar40 C
UV1016
AI 3050
C2H
±33 Bar15 - 35 C
Feed Gas Ex. GASCO
The purposes of Plant Feed Conditioning Unit are to meter the feed gas in terms of quality and quantity, and to compress the gas to the pressure (68.8 bar) required for the downstream Liquefied Natural Gas (LNG) processing plant. Design feed gas rate to LNG process train is 28700 m3/h (644 ton/h).
Presley Wong
20/06/2003
UNIT 14 MERCURY REMOVAL
Feed Gas Ex. Unit 01
68 Bar40 C
PDI
1003
PDI 1005
66.7 Bar39.6 ºC
66.2 Bar39.4 ºC
14-MD01
14-MD02
Acid Gas Removal Unit
Set @ 75 bar g
Set @ 75 bar g
The purpose of the Mercury Removal Unit is to reduce the mercury (Hg) level in the feed gas by adsorption through activated carbon bed impregnated with sulphur to prevent corrosion in the Main Cryogenic Heat Exchanger (MCHE) aluminium tube bundles. This will reduce the mercury level from the feed gas to less than 5 ng/Nm3 (1 nanogram ng = 1 / 1,000,000 mm)
PIC 1074B
PIC 1074A
12-MJ23
12-MC23A/B
12-MD21
12-MJ22
12-MD31
12-MJ24
12-MJ21
12-MD27
12-MD2912-MC24
12-MJ29
Acid Gas Incinerator
12-MC22A/B
Hot Oil
Sweet Gas to Dehydration Unit
Rich Solvent
Lean Solvent
5m
LIC 1012
FIC 1015
LIC 1026
FIC 1028
LIC 1054
FIC 1117
LIC 1078
FIC 1076
LIC 1140
H
L
FIC 1070
TIC 1043
12-MD22
Vent at Safe Location
120.8 ºC
81.1 ºC
46.3 ºC
65.2 Bar40.5 C
65.2 Bar40.5 C
66.2 Bar39.3 C
1.65 Bar71.1 C
8 Bar1.1 Bar
1.85 Bar120.8 C
1.55 Bar40 C
1.8 Bar103 C
XV1014
XV1008
M
12-M
C21
TIC 1102
86.5 C
M
114.4 C86.1 C
NG Feed
UNIT 12
ACID GAS REMOVAL
The purpose of the Acid Gas Removal Unit is to remove acid gas, mainly Carbon Dioxide CO2 and Hydrogen Sulphide H2S, from the natural gas feed to prevent these components from freezing out and causing blockages and to meet LNG specification. Acid gas, mainly CO2 and H2S, is removed from the gas stream by absorption into aMDEA in the Acid Gas Absorber (12-MD21), licensed by BASF.This will reduce the CO2 < 50 ppm. Regeneration System in which the rich aMDEA from 12-MD21 is flashed in Rich Solvent LP Flash Column (12-MD22), to remove the adsorbed hydrocarbons and then the CO2 is stripped from the rich aMDEA at reduced pressure and elevated temperatures in the Solvent Regenerator Column (12-MD27).
Ex. End FlashSystem
HP Fuel GasSystem
13-MD04
13-MD03
13-MD02-A 13-MD02-C
13-MD01
Water CondensateTo Unit 12
Liquefaction Unit
Water CondensateTo Unit 12
64 Bar22 C
168 C
13-MC 03
65.2 Bar40 C
64.7 Bar22 C
26.5 Bar40 C
27 Bar168 C
29 Bar 35 C
< 0.5 ppm
Back-up
LIC 1004
13-MD02-B
LIC 1055PIC
1007
13-MC01
LIC 1003
PIC 1062
13-MC02
TIC 1045
FIC 1048
15-FV1048A
15-TV1202A/B
Hot Oil Supply
C3LiquidEx. 16-MC10
C3VapourTo 16-MD05
63 Bar22 C
Warm FlareHeader
Hot Oil Return
26.8 Bar40 C
PV1062A PV1062B
UNIT 13 DEHYDRATION
XV1011
BDV1167
ESDV1196BDV1138
Warm Flare Header
Presley Wong19/06/2003
M
XV1059
28.2 Bar
Sweet Gas
The purpose of the Dehydration Unit is to remove water from the treating gas leaving the Acid Gas Removal Unit. Drying is required to prevent ice and hydrate formation in the Liquefaction Unit, which would cause blockage of lines and equipment The feed gas to Unit 13 is wet Natural Gas from the Acid Gas Removal Unit. The gas is precooled upstream of Unit 13 in the Drier Precooler (13-MC01) which results in condensation of part of the water vapour contained in the gas. This reduces the load on the Dehydration Unit. The temperature of the feed gas exiting the Drier Precooler (13-MC01) is 64.5 bar and is maintained at 22 C, a temperature high enough to avoid Hydrate formation but low enough to condense a significant amount of water . In the adsorption, the feed gas from the Drier Inlet Separator (13-MD01) flows vertically down to two of the Molecular Sieve Driers (13-MD02A/B/C). The treated gas from the adsorption beds must meet a moisture content of 0.5 ppmv maximum. In the regeneration, the molecular sieve beds are regenerated one at a time using regeneration gas, which is normally supplied from the HP End Flash Gas Compressor Aftercooler (15-MC10) at 29 bar and 35 C, flowing vertically upwards through the beds
LIC 1025
HP Fuel Gas
LIC 1021
ESDV1196
FV1057C
BDV1169
UNIT 15 LIQUEFACTION
Presley Wong23/06/2003
G
LIC 1005
15-MC03
LIC 1007
LIC 1020
15-MC01
62 Bar-16 C
63 Bar21.8 C
ESDV1013
61.4 Bar-29.7 C
61.9 Bar-16.1 C
FIC 1123
15-MD02
15-MD01
HS1025
FIC 1026
FIC 1249
15-MJ02
15-MC05
TIC 1056
FIC 1057
PIC 1073
SIC 3002
FY 1057C
FV
1057A/B
LIC 1083
15-MD03
15-MJ0115-MJ03
LNG Rundown To Storage
LT / HY MR
LT MR
HY MR
HY MR
PIC 1089
LT MR
C1
LPG
ESDV 1176
BDV1170
Cold FlareHeader
Cold FlareHeader
XV1138
62.5 Bar0.6 C
1.0 Bar-159.3 C
57.3 Bar-61.7 C
57.3 Bar-61.7 C
47.5 Bar-148.6 C
1.2 Bar-159.3 C
5.2 Bar-159.1 C
Fractionation Unit
DehydrationUnit
C3 Liquid
C3 Vapour C3 Vapour
C3 Liquid
C3 Vapour
15-MC02
LT MR
XV
1062
15-MC06
The purposes of the Liquefaction Unit are to liquefy the treated gas to enable storage at near atmospheric pressures & to remove heavy hydrocarbons in the feed stream, which will freeze in the cryogenic sections of the unit (for rich gas case). For the rich gas case, the pre-cooled two-phase mixture in the dry gas containing aromatics and other heavy hydrocarbons from the Feed Gas / HP & MP Propane Coolers (15-MC-01 and 15-MC02) are formed and removed in the Scrub Column (15-MD01). The vapour overhead from 15-MD01 is cooled at –29.7 C and partially condensed in the Scrub Column Overhead Condenser (15-MD03) against LP propane. This stream is further cooled and condensed in the warm bundle of the MCHE. The two-phase stream exiting the warm bundle of the MCHE is phase separated in the Scrub Column Reflux Drum (15-MD02). This reflux drum temperature is controlled at –61 C using bypass line across the MCHE warm bundle with part of the warm feed gas. The liquid is returned to the Scrub Column as reflux using the Scrub Column Reflux Pump (15-MJ01). The liquid stream from the scrub column bottoms is fed to the fractionation unit to generate refrigerant make-up and a condensate product. This combined stream is further cooled, liquefied and sub-cooled at about –148 C against MR in the middle and cold bundles of the MCHE. The liquefied natural gas at about –148 C, 47.5 bara is let down over LNG Expander (15-MJ02) and FV 1057A/B to about 1.2 bara. At this pressure some re-flash occurs and LNG temperature drops to about –159 C. The LNG enters LNG Flash Drum (15-MD03). The flash vapour is reheated in LMR / End Flash Gas Heat Exchanger (15-MC06) and send to the suction of End Flash Compressor (15-MJ04) to be recompressed for use as fuel. The LNG is pumped to storage using LNG Product Pump (15-MJ03) . Design feed gas rate to Main Cryogenic Heat Exchanger (MCHE) is 170000 m3/d (15300 ton/d) & LNG rundown to LNG storage is 33600 m3/d (14200 ton/d).
PI 1105
PI 1205
PIC 2089
M
ESDV2033
ESDV2022
XV
2121
LNG Circulation Header
LNG Loading Header
Presley Wong23/06/2003
71-MF01 71-MF02
71-MJ05-A
Loading Arms
Boil Off Gas to Gas Metering Station
LP Flare System
Make-up Gas Ex. Feed Gas System
Tie-in for Phase Two Expansion
71-MJO2A/B/C71-MJO1A/B/C
HS 2110M
M
HS 2109
MHS 2115
ES
DV
2122
ES
DV
2105
XV
2104
ES
DV
2120
ES
DV
2103
ESDV2130
PIC 1202
PIC 1102
HIC 2116
PIC 2129
PIC 2127
ESDV2008
ESDV2004
ESDV2001
Vapour R
eturn Ex. S
hip
71-ML01-A
71-ML01-B
71-ML03
71-ML02
ESDV2006
ESDV2103
M
HV
HV2034
HV2023
HV2009
HV2044
HV
ESDV 2068
UNIT 71LNG STORAGE & LOADING
Capacity: 150,000 m3 Capacity: 150,000 m3
FIC1140/1/2
FIC1240/1/2
M
TIC 4310
71-MJ05-B/C
71-MJ05-B/C
PV
The purposes of the Storage and Loading Unit are to provide adequate storage and loading facilities to allow for continuous production of LNG at the design production rate & to enable intermittent export by LNG ship. The LNG storage tanks (capacity = 150,000 m3) are stored at slight above atmospheric pressure for safety reason. The unit is designed to operate in two modes: holding mode and loading mode. In holding mode LNG is rundown from Train 1 into either two of the LNG storage tanks. During loading mode there is simultaneous LNG rundown from Train 1 and LNG loading from both storage tanks to the LNG ship. To achieve the design LNG ship loading rate of 12,000m³/h six LNG loading pumps are provided; 71-MJ01A/B/C and 71-MJ02A/B/C. Each pump is a submerged type pump located in vertical wells within the LNG storage tanks and is rated for 2000m³/h. Three pumps are provided in each tank.. It takes approx. 4.5 days to fill up one LNG storage tank & 13 hrs to fill up one LNG tanker.
UNIT 16
PROPANE REFRIGERATION
Presley Wong23/06/2003
16-MC 09
4.3 Bar-3 C
8 Bar18 C
7.2 Bar14 C
2.4 Bar-20 C
16-MC 10
18 Bar68 C
16 Bar35 C
17 Bar50 C
1.4 Bar-34 C
16-MJ 04
MD 06
4.3 Bar-3 C
2.4 Bar-20 C
1.4 Bar-34 C
16-MC 04
15-MC 01
16-MC 06
15-MC 02
16-MC 05
13-MC 01
16-MC 07
15-MC 03
MD 04MD 03 MD 05MD 02
4.2 Bar-3.5 C
7.1 Bar14.6 C
2.3 Bar-21 C
1.3 Bar-35 C
MD 07
C3 To/Ex. Storage16-MJ 05
LVLVLVLV
LV LV LV LV
PV
LV
M
TC
MC 11
LCC3 M/U to MRC3 M/U to MR
M
M
The purpose of the Propane Refrigerant Circuit is used to supply refrigeration cooling to the natural gas feed circuit and mixed refrigerant circuit at four pressure levels in a closed loop. Propane from the discharge of the Propane Compressor (16-MJ04) at 18.0 Bar and 68.3 C is de superheated and condensed by ambient air in the Propane Condenser (16-MC09). The condensed propane at 17.1 Bar and 50.0 C is collected in the Propane Accumulator (16-MD06). The propane liquid from 16-MD06 is sub cooled in the Propane Sub-cooler (16-MC10) before being supplied to the natural gas & mixed refrigerant (MR) evaporators. To produce one ton of LNG, 3.5 tons of propane is required to provide refrigeration cooling.
UNIT 16
MIXED REFRIGERATION
Presley Wong23/06/2003
16-MC01 16-MC03
16-MC 04
59 Bar -31 C
61.8 Bar0.6 C
21 Bar68 C
59 Bar -31 C
61.6 Bar-16 C
62.5 Bar40 C
61 Bar-30 C
62.2 Bar18 C
59 Bar -31 C
47 Bar -147C
16-MC 0516-MC 0616-MC 07
16-MD08
16-MD01
16-MJ06
15-MC05
16-MC02
33 Bar73 C
63 Bar89 C
61 Bar -29 C
3.9 Bar-33.8 C
15-MC06
End Flash Gas Compressor
C1 Ex. Demethaniser (Unit 07)
NG Out
NG In
48 Bar-125 C
57 Bar-155 C
59 Bar-31.5 C
AI 1261
C1C2C3N2
LNG End Flash Drum (Unit 15)
PV
TVCold JT
Warm JT
LNG End Flash Drum (Unit 15)
Flare
16-MJ 01 16-MJ 02 16-MJ 03
C3
C1
N2
C2
M M M
NG Feed
LPG Ex.U07
LNG
The purpose of the Mixed Refrigerant Circuit in conjunction with Propane Circuit is used to provide refrigeration cooling required for natural gas in Main Cryogenic Heat Exchanger (MCHE). The refrigerant used to liquefy the feed gas is a mixture of nitrogen, methane, ethane and propane, known as mixed refrigerant (MR). The MR circuit is a closed refrigeration loop. The superheated MR from the Main Cryogenic Heat Exchanger (MCHE); 15-MC05 is compressed by LP MR Compressor 16-MJ01, MP MR Compressor 16-MJ02 and HP MR Compressor 16-MJ03 in series. High pressure vapours from the MR Compressor are cooled in the HP MR Compressor Aftercooler; 16-MC03 and partially condensed in the respective MR / HHP, MR / HP, MR / MP and MR / LP Propane Coolers and fed to the HP MR Separator 16-MD08. Liquid from 16-MD08 (heavy MR) is cooled further in the "warm" bundle of the MCHE and by the let down in pressure through the MR Liquid Expander; 16-MJ06, recovering electrical power, and then sprayed over the "middle" bundle of the MCHE as a cooling medium. Most of the vapours from 16-MD08 (light MR) pass through both the "warm", "middle“ and "cold" bundles of the MCHE, and are let down over the "cold" Joule-Thomson (J-T) valve; 16-CrV-1035 to achieve the minimum required temperature. Prior to entering the MCHE shell side, this light MR stream is combined with the pre-cooled light MR stream in the MR/End Flash Gas Heat Exchanger; 15-MC06 where the MR is heat exchanged with 15-MD03 overheads vapour. The combined light MR stream is sprayed over the "cold" bundle of the MCHE as a cooling medium. Vapourised MR from the MCHE is recycled to the LP MR Compressor; 16-MJ01 via The LP MR Suction Drum; 16-MD01. Nitrogen, Methane and Propane are injected into the MR stream to the LP MR Suction Drum; 16-MD01 and Ethane is injected into the HP-MP Seperator, 16-MD08 as required, to maintain system inventory and composition.
MCHE
Scrub ColumnOHD Condenser
LPGDrum
MD 10
7-MJ02
C3 Storage
LPGDrum
MD05
UNIT 07 FRACTIONATION
Presley Wong03/07/2003
7-MJ01
15-MC 06 MC 03
MC 02
MD 06
MC 01
MC 09
MC 07 MC 11
MC 04
MC 06
MC 05
MC 10
7-MJ06MC 07
7-MJ04
C2C3C4C5
C2 Storage
LPGDrum
29 Bar-29 C
29 Bar-29 C
29 Bar139 C
29 Bar-32C
29 Bar43 C
14.3 Bar41 C
26.8 Bar4.3 C
13.8 Bar40.1 C
26 Bar0.2 C
14.6 Bar119 C
27 Bar131 C
4.9 Bar45 C
4.4 Bar40 C
14 Bar41 C
13 Bar40 C
3.5 Bar40 C
5.2 Bar99 C
5.2 Bar99 C
62 Bar-18 C
Condensate to Storage
Scrub Column Bottom
Off-Spec C2 line Off-Spec C3 line
MD03
MD08
7-MJ03
LPGDrum
MD07
7-MJ05
14.6 Bar119 C
MD 01 MD 02
MD 04
MD 06MD 09
The purpose of the Fractionation Unit is to remove heavier hydrocarbons from feed gas that will affect the length of the carbon chain, C5+, specification of the LNG product. In addition, aromatics, Benzene specially, are removed as these may freeze in cryogenic sections of the plant. When operating, the Fractionation Unit reinjects lighter, recovered hydrocarbons (LPG) into the Liquefaction Unit to be blended into the LNG Product, or recycled through the Scrub Column, 15-MD01, depending on operational requirements. In addition, it produces both ethane and propane of refrigerant grade quality for make-up to the Propane and MR Compressor Circuits, and a condensate product stream, which will vary in quality depending upon whether the Depentaniser is operating.
7-MC 01
Hot Oil
LIC 1015
FIC 1009
29 Bar-27.6 C
29 Bar140 C
29 Bar-27.9 C
FIC 1013
TIC 1007
PIC 1002
7-MC 09
C3 Vapour
LIC 1134
LIC 1137
29 Bar140 C
29 Bar-32 C
29.5 Bar43.4 C
-35 C
FIC 1140
FIC 1166
UNIT 07 DEMETHANISER
Presley Wong03/07/2003
ESDV1013
PV1262 (15-MC 06)
7-MD 01
7-MD 08
Balancing line
56.7 Bar-30.5 C
56.7 Bar-30.5 C
C3 Liquid
Cold Flare HeaderPV1002B
HS 1105
1
13
Feed Ex. Scrub Column
De C2 Column
15-MC 06
C2 C3 C4 C5
9
29 Bar110 C
26.9 Bar137 C
NNF
15-MC 03
MCHE
07-MJ04A
07-MJ04
TI 1215
HH
The liquid stream from the bottom of the Scrub Column (15-MD01) is reduced in pressure and temperature from 62 bara and –18.1 C to 29 bara –29.3 C and then fed to the Demethaniser (07-MD01). This column serves as a stripper and is reboiled by a kettle type hot oil reboiler 07-MC01. The overhead vapour from the Demethanser Column is fed to the LMR End Flash Gas Exchanger (15-MC06). The bottoms product stream is reduced in pressure to 26.9 bara and then fed to the Deethaniser Column (07-MD02).
7-MC 02
Hot Oil
LIC 1036
FIC 1028
26.8 Bar4.3 C
27 Bar131 C
27 Bar106 C
FIC 1035
TIC 1027
PIC 1022
7-MC 03
C3 Vapour
LIC 1041
LIC 1046
27 Bar131 C
26.8 Bar1.0 C
14.4 Bar103 C
-4.0 C
FIC 1140
FIC 1048
Presley Wong03/07/2003
07-ML 01
Off-Spec C2 From Storage Tank
7-MD 02
7-MD 03
Cold Flare Header
26.8 Bar0.2 C
27 Bar118 C
C3 Liquid
PV1022
1
28
Feed Ex. De C1 Column
De C3 Column
UNIT 07 DEETHANISER
9
24
FIC 1047
ESDV1050
LI 1044
07-MJ01A
07-MJ01
26.9 Bar0.3 C
29.5 Bar0.3 C
15-MD08
C2 Storage
FI 1105
ESDV1205
ESDV1235
LI 1032 LL
TI 1024
The feed liquid is reboiled in Deethanser Reboiler (07-MC02). The overhead vapours leave the column at 26.8 bara and 4.3 C and fed to the Deethaniser Condenser (07-MC03) where the vapour ethane is condensed against a Medium Pressure (MP) propane stream from the Fractionation Refrigerant Package (07-ML01). The condensed ethane is then used to provide reflux for the column via the Deethaniser Reflux Pump (07-MJ01) and to supply ethane refrigerant make-up. Excess ethane liquid will be send to re-injection. A bypass line around the column allows off-specification ethane to be imported from the storage and reprocessed in the column.
7-MC 04
Hot Oil
LIC 1070
FIC 1068
14.3 Bar42 C
14.6 Bar120 C
14.4 Bar103 C
FIC 1073
TI 1065
PIC 1061
LIC 1083
14.6 Bar120 C
14.1 Bar40 C
5.1 Bar74 C
FIC 1088B
FIC 1087
Presley Wong03/07/2003
LL
Off-Spec C3 From Storage Tank
7-MD 04
7-MD 05
Cold Flare Header
13.8 Bar40 C
14.6 Bar112 C
PV1061
1
28
Feed Ex. De C2 Column
De C4 Column
22
19
FIC 1086
ESDV1089
LI 1084
07-MJ02A
07-MJ02
27.5 Bar41.6 C
29.5 Bar41.6 C
15-MD08
C3 Storage
FI 1152
ESDV1059
ESDV1236
7-MC 05
M
FIC 1088A
TIC 1063
LI 1074
39
AI 1062
C2 C3 iC4 nC4
UNIT 07 DEPROPANISER
Liquid hydrocarbons from the bottom of the Deenthaniser are dropped in pressure from 26.9 bara to 14.4 bara and then fed to the Depropaniser Column (07-MD04). The feed liquid is reboiled in the Depropaniser Reboiler (07-MC04). The overhead vapours leave the column at 14.3 bara and 41.8 C and fed to the Depropaniser Condenser (07-MC05) where the vapour propane is condensed by ambient air. The condensed propane is then used to provide reflux for the column via the Depropaniser Reflux Pump (07-MJ02) and to supply propane refrigerant make-up. Excess propane liquid will be send to re-injection. A bypass line around the column allows off-specification ethane to be imported from the storage and reprocessed in the column.
7-MC 06
Hot Oil
LIC 1105
FIC 1103
4.9 Bar45 C
5.2 Bar99 C
5.1 Bar75 C
TI 1164
PIC 1098
LIC 1117
5.2 Bar99 C
4.9 Bar40 C
3.5 Bar40 C
FIC 1121
Presley Wong03/07/2003
LL
7-MD 06
7-MD 07
Cold Flare Header
4.4 Bar40 C
5.2 Bar94 C
PV1098
1
Feed Ex. De C3 Column
Condensate To Storage
18
17
FIC 1120
ESDV1122
LI 1118
07-MJ03A
07-MJ03
29.5 Bar41.8 C
15-MD08
7-MC 07
M
LI 1106
34
UNIT 07 DEBUTANISER
TIC 110032
7-MC 08
MHS 1105
FIC 1162
FIC 1129
ESDV1161
Condensate Ex. 7-MJ 06
Condensate Ex. 7-MJ 05
LIC 1165
De C5 Column
4.7 Bar40 C
De C5 Column
The bottoms liquid product is reduced in pressure from 14.6 bara to 5.1 bara and then fed to the Debutaniser Column (07-MD06). The feed liquid is reboiled in the Debutaniser Reboiler (07-MC06). The overhead vapours leave the column at 4.9 bara and 45.2 C and fed to the Debutaniser Condenser (07-MC07) where the vapour butane is condensed by ambient air. The condensed butane is then used to provide reflux for the column via the Debutaniser Reflux Pump (07-MJ03) and to re-inject into the MCHE. The Debutaniser Column bottom product leaves the column at 99.0 C and depending on the mode of operations; the bottom product is either sub cooled by ambient air to 40.0 C in the Condensate Product Cooler (07-MC08) and then send to storage or fed to the Depentaniser Column (07-MD09).
7-MC 10
Hot Oil
LIC 1165
FIC 1103
4.9 Bar45 C
5.2 Bar99 C
5.1 Bar75 C
TIC 1174
PIC 1177
LIC 1117
4.9 Bar40 C
FIC 1191
Presley Wong03/07/2003
LL
7-MD 09
7-MD 10
Cold Flare Header
4.4 Bar40 C
5.2 Bar94 C
PV1098
1
Feed Ex. De C4 Column 19
15
FIC 1192
ESDV1122
LI 1118
07-MJ05A
07-MJ05
29.5 Bar41.8 C
15-MD08
ESDV1237
7-MC 11
M
LI 1163
32
UNIT 07 DEPENTANISER
FIC 1191
07-MJ06/A
Downstream07-MC 08
Upstream07-MC 08
HS-1105
30 TI 1170
If the feed gas composition is such that it becomes necessary to supply a low-benzene C5 stream to supplement the LPG re-circulation, the Debutaniser Column bottom product is routed to the Depentaniser Column. The bottoms liquid product from the Debutaniser is fed to the Depentaniser Column (07-MD09) and is reduced in pressure to 2.1 bara in the column. The feed liquid is reboiled in the Depentaniser Reboiler (07-MC10). The overhead vapour is totally condensed by ambient air using the Depentaniser Condenser (07-MC11). The condensed liquid is then used to provide reflux for the column via the Depentaniser Reflux Pump (07-MJ05) and send to the LPG Re-injection Drum (07-MD08).
UNIT 73
ETHANE STORAGE
Vap
or R
etur
n
PIC1009
FIC1020
73-MJ0173-MJ03
PIC1003
RefrigerationPackage
ESDV1010
73-MD01
Cold Flare Header
C2 Make-up To MR System
C2 To / Ex.Deethaniser
Col
d Fl
are
Hea
der
19 Bar-14 C
C2 ISO Container
C2
Off
-spe
c L
ine
Ethane storage vessel 73-MD01 receives liquid from 2 sources; Deethaniser 07-MD02 in the common fractionation train & ISO containers delivered by rod or ship. The ethane refrigerant storage vessel, 73-MD01, is a pressurized drum with storage volume 660 m3. The propane refrigerant is stored at approximately –14oC and 19 bar. Displacement vapour, flash vapours and vapour generated by heat in-leak are vented to cold flare by pressure control.
UNIT 73
PROPANE STORAGE
FIC1045
PIC1028
PIC1033
ESDV1037
LI1029
ESDV1046
73-MD02
73-MJ02
73-MJ04
Cold Flare Header
C3 To / Ex.Pump-out C3 System
8.4 ~ 15.4 Bar20 ~ 45 C
Vap
or R
etur
n
C2 ISO Container
C3 To / Ex.Depropaniser
The Propane Storage Vessel, 73-MD02, receives liquid propane from three sources; Depropaniser, 07-MD04, in the common fractionation train, ISO containers delivered by road. or ship & Pump-out connections in the liquefaction unit. The Propane Refrigerant Storage Vessel, 73-MD02, is a pressurised sphere with a gross volume of approximately 1500m3.The propane refrigerant is stored at ambient temperature and the corresponding vapour pressure: @ 20°C the storage pressure will be 8.4 bar & @ 45°C the storage pressure will be 15.4 bar. Displacement and flash vapours are vented to cold flare by pressure control. The propane refrigerant system is not insulated.
15 / -2.1 mbar g
15 / -2.1 mbar g
LI 1017
UNIT 02
aMDEA STORAGE
Mohd Awad20/06/2003
Demin. water
02-MF2202-MF21
Solvent to/ex. U 12
FI 1004
02-MJ22 02-MJ21
LI 1008
ATM
N2
ATM
N2
Set @ 7.5 mbar g
Set @ 15 mbar g
Set @ 7.5 mbar g
Set @ 15 mbar g
The acid gas removal unit uses an activated MDEA. The common facilities are used to provide space and volume for the mixing and storage for the aMDEA solvent used in the AGR unit. The facilities also allow enough volume to hold solvent from the AGR unit. The common facilities consist of the mixed solvent storage tank, 02-MF22. The mixed solvents supply pumps, 02-MJ22 that take suction from this tank and discharge it to another tank, the solvent storage tank, 02-MF21. The solvent transfer pump, 02-MJ21 takes suction from this tank and discharge to the acid gas removal unit.