LNG Process Units.ppt

7/26/2019 LNG Process Units.ppt

1/19

LNG PROCESS TRAIN

01-MD01

68.8 Bar

107.7 C

01-MC 0131.5 Bar

34.5 C

66.7 Bar

39.6 C

14-MD01

14-MD02

01-IC01

5m01-MJ01

NG 12-MD27

12-MD22

12-MD21

MD02-A

MD02-C

13-MD01

MD02-B

13-

MC01

13-MD03

13-MC02

13-MD04

15-MC0115-MC02

15-MC03

MD02

15-MD01

15-MJ01

15-MJ02

15-MC-05

MD03

15-MJ0371-MF01/2

MJO1_2A/B/CLa!"#$ Arm%

71-MJ05

7-MD01

7-MD02

MD08 MD03

12-MJ2212-MJ24

7-MJ017-MJ04

16-MJ01 16-MJ02 16-MJ03

16-MJ04

16-MD01

MD06

C3 L"&'"! (

C)"**+r%

16-MC 09

16-MC04/05/06/07

, F/G

46.3 C

65.2 Bar

40.5 C

1.65 Bar

71.1 C

1.8 Bar

103 C

+#(

64.7 Bar

22 C

63 Bar

22 C

62 Bar

-16 C

61.4 Bar

-31.4 C

47 Bar

-147.1 C

5.2 Bar

-159.1 C

#"( 13

18 Bar

68.3C

17.1 Bar

50C

7.1 Bar

14.6C 4.2 Bar

-3.5C2.3 Bar

-21C

1.3 Bar

-34.9C

63 Bar

89.8C

4.3 Bar

-34.4 C

59.5 Bar

-42.8 C

61.4 Bar

-31.4 C

21.5 Bar

67.7 C

33.1 Bar

72.8 C

3.9 Bar

-33.8 C 61.2 Bar

-29.4 C

29 Bar

-28.6 C

26.3 Bar

0.2 C

7-MD03

C3

C4

C5

6. Bar-29.7 C

6. Bar

-29.7 C

16-MC01 16-MC02 16-MC03

16-MD01

16-MJ06


2/19

Presley Wong20/06/2003

70 Bar

15 - 35 C

UNIT 01

PRESSURE REDUCTION & METERING STATION

MD 02

GMS

GMS

GMS

GMS

Ga% M+(+r"#$

'# 1

MD 02

MD 02

MD 02

MD 02

MD 02 MD 02

Damietta -1

Water boilers

ilters! se"arators

Damietta - #

F++!Ga%

.Gr"!

Tem"orar$ PRSO

O

F"*(+r%

Ga% M+(+r"#$

'# 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 gaspressure 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.


3/19

M+r'r

A%r+r

68.8 Bar

107.7C

M

arm L"&'"!

,+a!+r

I

3004

Presley Wong

20/06/2003

33 Bar15 - 35 C

F++! Ga%

. GACO

DI

3006

DI

3007

FI

3001

:I

3011

I

3009

FI

3002

:I

3010

I

3008

FI

3001

FI

3002

UNIT 01

PLANT EED CONDITIONING

AI305F

IC5 AI305G

#C5 AI305I

C6;

AI

305O

L,

AI

305

,, AI

3050

C2,

AI305A

C1AI305B

C2AI305C

C3 AI305D

IC4 AI305

#C4

AI

305J

N2 AI

305+-'? #"( 55

, FG Ma>+-'?

( :ra"# 1 #"( 15

BOG .

#"( 71

01-MD01

01-MJ01

31.2 Bar

34.5C

01-MC 01

M

1 3 5 7

2 4 6 8

68 Bar

40 C

1016

AI

3050

C2,

33 Bar

15 - 35 C

F++! Ga%

. GACO

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).


4/19

Presley Wong20/06/2003

UNIT 1%MERCUR REMO'AL

F++! Ga%

. #"( 01

68 Bar

40 C

DI

1003

DI

1005

66.7 Bar

39.6 C

66.2 Bar

39.4 C

14-MD01

14-MD02

A"! Ga% +m@a* #"(

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 activatedcarbon bed impregnated with sulphur to prevent corrosion in the Main Cryogenic Heat Exchanger (MCHE) aluminium tubebundles. This will reduce the mercury level from the feed gas to less than 5 ng/Nm3 (1 nanogram ng = 1 / 1,000,000 mm)


5/19

IC

1074B

IC

1074A

12-MJ23

12-MC23A/B

12-MD21

12-MJ22

12-MD31

12-MJ24

12-MJ21

12-MD27

12-MD2912-MC24

12-MJ29

A"! Ga% I#"#+ra(r

12-MC22A/B

,( O"*

++( Ga% (

D+)!ra("# #"(

") *@+#(

L+a#

*@+#(

5m

LIC

1012

FIC

1015

LIC

1026

FIC

1028

LIC

1054

FIC

1117

LIC

1078

FIC

1076

LIC

1140

,

L

FIC

1070

:IC

1043

12-MD22

+#( a( a+ La("#

120.8 C

81.1 C

46.3 C

65.2 Bar

40.5 C65.2 Bar

40.5 C

66.2 Bar

39.3 C

1.65 Bar

71.1 C

8 Bar1.1 Bar

1.85 Bar

120.8 C

1.55 Bar

40 C

1.8 Bar

103 C

=1014

=

1008

M

12-MC21

:IC

1102

86.5 C

M

114.4 C86.1 C

NG F++!

UNIT 1#

ACID GAS REMO'AL

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 preventthese 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 richaMDEA 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 therich aMDEA at reduced pressure and elevated temperatures in the Solvent Regenerator Column (12-MD27).


6/19

. #! F*a%)

%(+m

, F'+* Ga%

%(+m

13-MD04

13-MD03

13-MD02-A 13-MD02-C

13-MD01

a(+r C#!+#%a(+

: #"( 12L"&'+a("# #"(

a(+r C#!+#%a(+

: #"( 1264 Bar

22 C

168 C

13-MC 03

65.2 Bar

40 C

64.7 Bar

22 C

26.5 Bar

40 C

27 Bar

168 C

29 Bar 35 C

0.5 ??m

Ba>-'?

LIC

1004

13-MD02-B

LIC

1055IC

1007

13-MC01

LIC

1003

IC

1062

13-MC02

:IC

1045

FIC

1048

15-F1048A

15-:1202A/B

,( O"* '??*

C3L"&'"!

. 16-MC10

C3a?'r

: 16-MD05

63 Bar

22 C

arm F*ar+

,+a!+r

,( O"* +('r#

26.8 Bar

40 C

1062A 1062B

UNIT 1(

DE)DRATION

=

1011

BD1167

D1196BD1138

arm F*ar+ ,+a!+r

Presley Wong

19/06/2003

M

=1059

28.2 Bar

++( Ga%

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 hydrateformation 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 RemovalUnit. 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 22C, atemperature 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 amoisture content of 0.5 ppmv maximum. In the regeneration, the molecular sieve beds are regenerated one at a time using regeneration gas, which is normallysupplied from the HP End Flash Gas Compressor Aftercooler (15-MC10) at 29 bar and 35C, flowing vertically upwards through the beds


7/19

LIC

1025

, F'+* Ga%

LIC

1021

D

1196

F1057C

BD

1169

UNIT 1*

LI+UEACTION

Presley Wong

23/06/2003

G

LIC

1005

15-MC03

LIC

1007

LIC1020

15-MC01

62 Bar

-16 C

63 Bar

21.8 C

D1013

61.4 Bar

-29.7 C

61.9 Bar

-16.1 C

FIC

1123

15-MD02

15-MD01

,1025

FIC

1026

FIC

1249

15-MJ02

15-MC05

:IC

1056

FIC

1057

IC

1073

IC

3002

F

1057C

F1057A/B

LIC

1083

15-MD03

15-MJ0115-MJ03

LNG '#!#

: (ra$+

L: / , M

L: M

, M

, M

IC

1089

LT MR

C1

LG

D 1176

BD1170

C*! F*ar+

,+a!+r

C*! F*ar+

,+a!+r

=1138

62.5 Bar

0.6 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

Fra("#a("# #"(

D+)!ra("#

#"(

C3 L"&'"!

C3 a?'r C3 a?'r

C3 L"&'"!

C3 a?'r

15-MC02

L: M

=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 willfreeze 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 heavyhydrocarbons 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 29.7C and partially condensed in the Scrub Column Overhead Condenser (15-MD03) against LP propane. This stream is further cooled and condensed in thewarm 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 drumtemperature is controlled at 61C 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 usingthe 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 condensateproduct. This combined stream is further cooled, liquefied and sub-cooled at about 148C 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 about159C. 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 FlashCompressor (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 HeatExchanger (MCHE) is 170000 m3/d (15300 ton/d) & LNG rundown to LNG storage is 33600 m3/d (14200 ton/d).


8/19

I

1105

I

1205

IC

2089

M

D2033

D2022

=.2121

LNG C"r'*a("# ,+a!+r

LNG La!"#$ ,+a!+r

Presley Wong

23/06/2003

,1-M01 ,1-M0#

71-MJ05-A

La!"#$ Arm%

B"* O Ga% ( Ga%

M+(+r"#$ (a("#

L F*ar+ %(+m

Ma>+-'? Ga% .

F++! Ga% %(+m

:"+-"# r )a%+

: ?a#%"#

,1-MO#A!.!C,1-MO1A!.!C

,

2110M

M

,

2109

M,

2115

D.2122

D.2105

=.2104

D.2120

D.2103

D2130

IC

1202

IC

1102

,IC

2116

IC

2129

IC

2127

D2008

D2004

D2001

a?'r+('r#

.4)"?

71-ML01-A

71-ML01-B

71-ML03

71-ML02

D2006

D

2103

M

,

,2034

,2023

,2009

,2044

,

D 2068

UNIT ,1

LNG STORAGE & LOADING

Ca?a"(E 150000 m3 Ca?a"(E 150000 m3

FIC

1140/1/2

FIC

1240/1/2

M

:IC

4310

71-MJ05-B/C

71-MJ05-B/C

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 & toenable 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 issimultaneous 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 12,000m/h six LNG loadingpumps 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 2000m/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.


9/19

UNIT 1/

PROPANE RERIGERATION

Presley Wong

23/06/2003

16-MC 09

4.3 Bar

-3C

8 Bar

18C

7.2 Bar

14 C

2.4 Bar

-20C

16-MC10

18 Bar

68 C

16 Bar

35 C

17 Bar

50 C

1.4 Bar

-34C

1/-M 0%

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 Bar

14.6 C

2.3 Bar

-21 C

1.3 Bar

-35 C

MD 07

C3 :/. (ra$+16-MJ 05

LLLL

L L L L

L

M

:C

MC 11

LCC3 M/ ( M

C3 M/ ( M

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 fourpressure levels in a closed loop. Propane from the discharge of the Propane Compressor (16-MJ04) at 18.0 Bar and 68.3C is de superheated and condensed

by ambient air in the Propane Condenser (16-MC09). The condensed propane at 17.1 Bar and 50.0C is collected in the Propane Accumulator (16-MD06). Thepropane 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.


10/19

UNIT 1/

MIED RERIGERATION

Presley Wong

23/06/2003

16-MC01 16-MC03

16-MC 04

59 Bar -31 C

61.8 Bar

0.6 C

21 Bar

68 C

59 Bar -31

C

61.6 Bar

-16 C

62.5 Bar

40 C61 Bar

-30 C

62.2 Bar

18 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 Bar

73 C

63 Bar

89 C

61 Bar -29 C

3.9 Bar

-33.8 C

15-MC06

#! F*a%) Ga% Cm?r+%%r

C1 . D+m+()a#"%+r #"( 07H

NG O'(

NG I#

48 Bar

-125 C

57 Bar

-155 C

59 Bar

-31.5 C

AI

1261

C1

C2

C3

N2

LNG #! F*a%) Dr'm #"( 15H

:C*! J:

arm J:

LNG #! F*a%) Dr'm #"( 15H

F*ar+

16-MJ 01 16-MJ 02 16-MJ 03

C(

C1

N#

C#

M M M

NG F++!

LG .07

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 refrigerantused 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 MainCryogenic 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 MRCompressor 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 Separator16-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, andthen 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 lightMR 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 theMCHE 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 MRstream 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.


11/19

MC,

r' C*'m#

O,D C#!+#%+r

LG

Dr'm

MD 10

7-MJ02

C3

(ra$+

LG

Dr'm

MD05

UNIT 0,

RACTIONATION

Presley Wong

03/07/2003

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

C2

C3

C4

C5

C2

(ra$+

LG

Dr'm

29 Bar

-29 C

29 Bar

-29 C

29 Bar

139 C

29 Bar

-32C

29 Bar

43 C

14.3 Bar

41 C

26.8 Bar

4.3 C

13.8 Bar

40.1 C

26 Bar

0.2 C

14.6 Bar

119 C

27 Bar

131 C

4.9 Bar

45 C

4.4 Bar

40 C14 Bar

41 C

13 Bar

40 C

3.5 Bar

40 C

5.2 Bar

99 C5.2 Bar

99 C

62 Bar

-18 C

C#!+#%a(+ (

(ra$+

r' C*'m#

B((m

O-?+ C2 *"#+ O-?+ C3 *"#+

MD03

MD08

7-MJ03

LG

Dr'm

MD07

7-MJ05

14.6 Bar

119 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. Inaddition, aromatics, Benzene specially, are removed as these may freeze in cryogenic sections of the plant. When operating, the Fractionation Unit reinjects lighter, recoveredhydrocarbons (LPG) into the Liquefaction Unit to be blended into the LNG Product, or recycled through the Scrub Column, 15-MD01, depending on operational requirements. Inaddition, 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 willvary in quality depending upon whether the Depentaniser is operating.


12/19

,-MC 01

,( O"*

LIC

1015

FIC

1009

29 Bar

-27.6 C

29 Bar

140 C

29 Bar

-27.9 C

FIC

1013

:IC

1007

IC

1002

,-MC 0

C3 a?'r

LIC

1134

LIC

1137

29 Bar

140 C

29 Bar

-32 C

29.5 Bar

43.4 C

-35 C

FIC

1140

FIC

1166

UNIT 0,

DEMET)ANISER

Presley Wong

03/07/2003

D1013

1262 15-MC 06H

,-MD 01

,-MD 02

Ba*a#"#$ *"#+

56.7 Bar

-30.5 C

56.7 Bar

-30.5 C

C3 L"&'"!

C*! F*ar+ ,+a!+r

1002B

,

1105

1

13

F++! . r'

C*'m#

D+ C2 C*'m#

15-MC 06

C2 C3 C4 C5

9

29 Bar

110 C

26.9 Bar

137 C

NNF

15-MC 03

MC,

07-MJ04A

07-MJ04

:I

1215

,,

The liquid stream from the bottom of the Scrub Column (15-MD01) is reduced in pressure and temperature from 62 bara and 18.1C to 29 bara 29.3C and then fed to theDemethaniser (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 tothe 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).


13/19

,-MC 0#

,( O"*

LIC

1036

FIC

1028

26.8 Bar4.3 C

27 Bar

131 C

27 Bar

106 C

FIC

1035

:IC

1027

IC

1022

,-MC 0(

C3 a?'r

LIC

1041

LIC

1046

27 Bar

131 C

26.8 Bar

1.0 C

14.4 Bar

103 C

-4.0 C

FIC

1140

FIC

1048

Presley Wong

03/07/2003

07-ML 01

O-?+ C2 Frm (ra$+ :a#>

,-MD 0#

,-MD 0(

C*! F*ar+ ,+a!+r

26.8 Bar

0.2 C

27 Bar

118 C

C3 L"&'"!

1022

1

28

F++! . D+ C1

C*'m#

D+ C3 C*'m#

UNIT 0,

DEET)ANISER

9

24

FIC

1047

D

1050

LI

1044

07-MJ01A

07-MJ01

26.9 Bar

0.3 C

29.5 Bar

0.3 C

15-MD08

C2 (ra$+

FI

1105

D1205

D1235

LI

1032LL

:I

1024

The feed liquid is reboiled in Deethanser Reboiler (07-MC02). The overhead vapours leave the column at 26.8 bara and 4.3C and fed to the Deethaniser Condenser (07-MC03) where the vapour ethane iscondensed 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 DeethaniserReflux 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 thestorage and reprocessed in the column.


14/19

,-MC 0%

,( O"*

LIC

1070

FIC

1068

14.3 Bar

42 C

14.6 Bar

120 C

14.4 Bar

103 C

FIC

1073

:I

1065

IC

1061

LIC

1083

14.6 Bar

120 C

14.1 Bar

40 C

5.1 Bar

74 C

FIC

1088B

FIC

1087

Presley Wong

03/07/2003

LL

O-?+ C3 Frm (ra$+ :a#>

,-MD 0%

,-MD 0*

C*! F*ar+ ,+a!+r

13.8 Bar

40 C

14.6 Bar

112 C

1061

1

28

F++! . D+ C2

C*'m#

D+ C4 C*'m#

22

19

FIC

1086

D

1089

LI

1084

07-MJ02A

07-MJ02

27.5 Bar

41.6 C

29.5 Bar

41.6 C

15-MD08

C3 (ra$+

FI

1152

D1059

D1236

,-MC 0*

M

FIC

1088A

:IC

1063

LI

1074

39

AI

1062

C2 C3 "C4 #C4

UNIT 0,

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 theDepropaniser Reboiler (07-MC04). The overhead vapours leave the column at 14.3 bara and 41.8C 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.


15/19

,-MC 0/

,( O"*

LIC

1105

FIC

1103

4.9 Bar

45 C

5.2 Bar

99 C

5.1 Bar

75 C

:I

1164

IC

1098

LIC

1117

5.2 Bar

99 C

4.9 Bar

40 C

3.5 Bar

40 C

FIC1121

Presley Wong

03/07/2003

LL

,-MD 0/

,-MD 0,

C*! F*ar+ ,+a!+r

4.4 Bar

40 C

5.2 Bar

94 C

1098

1

F++! . D+ C3

C*'m#

C#!+#%a(+ :

(ra$+

18

17

FIC

1120

D

1122

LI

1118

07-MJ03A

07-MJ03

29.5 Bar41.8 C

15-MD08

,-MC 0,

M

LI

1106

34

UNIT 0, DE.UTANISER

:IC

110032

,-MC 02

M,

1105

FIC

1162

FIC

1129

D1161

C#!+#%a(+

. 7-MJ 06

C#!+#%a(+

. 7-MJ 05

LIC

1165

D+ C5 C*'m#

4.7 Bar

40 C

D+ C5 C*'m#

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). Theoverhead vapours leave the column at 4.9 bara and 45.2C and fed to the Debutaniser Condenser (07-MC07) where the vapour butane is condensed by ambient air. The condensed butane is then used toprovide 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 99.0C and depending on the modeof operations; the bottom product is either sub cooled by ambient air to 40.0C in the Condensate Product Cooler (07-MC08) and then send to storage or fed to the Depentaniser Column (07-MD09).

UNIT 0,


16/19

,-MC 10

,( O"*

LIC

1165

FIC

1103

4.9 Bar

45 C

5.2 Bar

99 C

5.1 Bar

75 C

:IC

1174

IC

1177

LIC

1117

4.9 Bar

40 C

FIC

1191

Presley Wong

03/07/2003

LL

,-MD 0

,-MD 10

C*! F*ar+ ,+a!+r

4.4 Bar

40 C

5.2 Bar

94 C

1098

1

F++! . D+ C4

C*'m# 19

15

FIC

1192

D

1122

LI

1118

07-MJ05A

07-MJ05

29.5 Bar

41.8 C

15-MD08

D1237

,-MC 11

M

LI

1163

32

UNIT 0,

DEPENTANISER

FIC

1191

07-MJ06/A

D#%(r+am07-MC 08

?%(r+am

07-MC 08

,-1105

30:I

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 DepentaniserColumn. 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 DepentaniserReboiler (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 theDepentaniser Reflux Pump (07-MJ05) and send to the LPG Re-injection Drum (07-MD08).

UNIT ,(


17/19

UNIT ,(

ET)ANE STORAGE

.a?r+('r#

IC

1009

FIC1020

,(-M01,(-M0(

IC

1003

Re3ri4eratio5

Pa67a4e

D1010

,(-MD01

C*! F*ar+ ,+a!+r

C2 Ma>+-'?

: M %(+m

C2 : / .

D++()a#"%+r

C*!F*ar+,+a!+r

19 Bar

-14 C

C2 IO C#(a"#+rC2OBB-%?+L"#+

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 ethanerefrigerant storage vessel, 73-MD01, is a pressurized drum with storage volume 660 m3. The propane refrigerant is stored at approximately 14oC and 19 bar. Displacementvapour, flash vapours and vapour generated by heat in-leak are vented to cold flare by pressure control.

UNIT ,(


18/19

UNIT ,(

PROPANE STORAGE

FIC

1045

IC

1028

IC

1033

D1037

LI

1029

D1046

,(-MD0#

,(-M0#

,(-M0%

C*! F*ar+ ,+a!+r

C3 : / .

'm?-'( C3 %(+m

8.4 ~ 15.4 Bar

20 ~ 45 C

.a?r+('r#

C2 IO C#(a"#+r

C3 : / .

D+?r?a#"%+r

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. orship & 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: @ 20C the storage pressure will be 8.4 bar & @ 45C the storage pressure will be15.4 bar. Displacement and flash vapours are vented to cold flare by pressure control. The propane refrigerant system is not insulated.


19/19

15 / -2.1 mbar g

15 / -2.1 mbar g

LI1017

UNIT 0#

aMDEA STORAGE

Mohd Awad

20/06/2003

D+m"#. a(+r

02-MF2202-MF21

*@+#( (/+. 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 aMDEAsolvent 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 solventstoragetank,02-MF22.Themixedsolventssupplypumps,02-MJ22thattakesuctionfromthistankanddischargeittoanothertank,thesolventstorage

LNG Process Units.ppt

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