LNG Process Units 200904.ppt

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


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


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


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


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


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


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


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


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


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


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


LL

7-MD 06

7-MD 07

Cold Flare Header

4.4 Bar40 C

5.2 Bar94 C

PV1098

1


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


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.

Documents

LNG Process Units 200904.ppt