TEP10 Natural Gas Liquefaction - 2008
TEP10 Natural Gas Liquefaction - 2008
TEP10 Natural Gas Liquefaction - 2008
Status: Draft
Jostein Pettersen
Fuel
gas
CH4/N2
End
flash
HHC
Extraction
Power
&
heat
CO2 reinjection
(to pipeline)
Fuel gas
system
Feed from
pipeline
Slug
catcher
Inlet facilities/
Metering
CO2
removal
CO2 drying
and
recompression
Nitrogen
removal
LNG
Storage
Dehydration
Mercury
removal
C1 / C2 / C3 Refrig. Make
-up
MEG
Recovery
Natural gas
liquefaction
Fractionation
(Refrigerant
Make-up)
LNG
Storage
LPG
Storage
Lean MEG
(to pipeline)
Condensate
treatment
Utility
Systems
Flare
Facilities
Condensate
Storage
Control
room
Mercury removal
Mercury can cause corrosion problems, especially in aluminium heat exchangers
Requirement: Max 0.01 g/Nm3
Source: Advantica
LNG
1,10
91,92
5,59
1,11
0,23
0,04
0
0
0,005
0
0
0
100
GCV (MJ/Sm)
40.5
40.45
40.4
Calculated ageing
effect during the
voyage from Melkya
to USA, Cove Point
40.35
40.3
40.25
0
10
12
14
16
Day
Calculated according to ISO 6976 based on real gas
Nitrogen Removal
Nitrogen need to be removed from LNG in order to meet
Gen Set
LNG
EXPANDER
END
FLAS H
HP
FUEL GAS
LNG
RUNDOWN
Gen Set
10
Utility power
and steam
Sulphur
recovcery
Utilities
Slugcatch
er
Condensate
stabilization
11
MCR Heat
Exchanger
Gas turbines
and
compressors
CCR
CO2
absorber
Qatargas
12
Jetty
Compressors
Air cooled
condenser
s
Cold boxes
(Heat exchangers)
Classification: Internal
Area 1
Status: Draft
Area 2
Area 3
LP flare
Subsea road
tunnel
Administration building / control
room
Sea water outlet /sea water
Holding basin / waste waterinlet
Camp area
treatment
Utility
MDEA storage / substation
fuel gas
Condensate storage
tank
LNG storage
tanks
Product jetty
LPG storage tank
Storage & loading
N2substation
cold box
NG Cold box
Process
substation
Electrical power generation
chemical storage
tanks
Pig receiver
Construction jetty
Slug catcher
14
50
60
10
20 bar
-30
Temperature, C
100
p=1.3 bar
-70
-110
-150
-190
-230
-4
-2
Entropy, kJ/(kgK)
15
20
30 %
15
50 %
100 %
10
0
0
20
40
60
80
100
16
T, oC
10oC
NG
Pumping of heat
evaporation temperature
(cascade process), or
evaporates at gliding
temperature (mixed refrigerant
process)
-160oC
Heat transferred
17
W = T0 S = To(SC - SH)
To
T = 1 K
SC
SH
Sub-ambient temperature
W = extra power input needed to
compensate for heat transfer across
a temperature difference of T = 1 K
10
0,01
-250
-150
-50
Reduced work
output
50
150
Temperature, deg C
18
-200oC
-100oC
-150oC
-50oC
0 oC
Precooling
Liquefaction
Subcooling
50oC
Pressure [bara]
Expansion
10
JT Throttling
1
-900
End
-800 flash -700
-600
-500LNG
-400
-300
-200
-100
100
200
Enthalpy [kJ/kg]
19
Heat sink
(Air/water)
Condenser
High pressure
Compressor
Expansion valve
Low pressure
Fluid to
be cooled
Evaporator
Evaporating
refrigerant
20
40oC at
Compressor
discharge
Condensation at 30oC
2
100,0
80 100
1
3
10,0
Pressure [bara]
Evaporating
temperature 30oC
1,0
Condensing
temperature 30oC
0,1
-700
-600
-500
-400
-300
-200
-100
100
200
300
Enthalpy [kJ/kg]
10
21
25
20
Temperature [C]
60
15
40
10
20
2 bar
0
-20
p = 1 bar
-40
-60
-80
-700
-600
-500
-400
-300
-200
-100
Enthalpy [kJ/kg]
100
200
300
22
100
CO2
C1
N2
Ethylene
C2
Pressura(Bara)
C3
10
n-C4
LNG Range
1
-200
-150
-100
-50
50
Temp(C)
11
23
Nitrogen
NBP
dhNBP
[C]
[kg/kJ]]
[kJ/kg
Triple point
[bara]
[C]
N2
-195,75 202,678
-210,0
Critical point
[bara]
[C]
0,125 -146,95
33,944
0,117 -82,55
46,002
Methane
CH4
-161,45 522,080
-182,5
Ethylene
C2H4
-103,71 487,132
-169,2
0,0012
9,20
50,359
Carbon dioxide
CO2
-78,45 392,780
-56,6
5,170
31,05
73,765
Ethane
C2H6
-88,65 496,999
-182,8 0,000013
32,25
48,839
Propane
C3H8
-42,07 431,517
-187,6 1,960E-09
96,67
42,496
n-Butane
C4H10
-0,45 389,746
37,997
24
Phase envelope
(for a given composition)
Cricondenbar
Critical Point
Cricondentherm
Cricondenbar
Quality Lines
Bubblepoint Curve
Critical
Pressure
75%
Quality
Lines
50%
Cricondentherm
25%
Temperature
12
25
Tx-diagram example:
Cooling C2/C3 at a constant pressure of 5 bara
Equilibrium between
liquid and vapour
5
0
Bubble
Superheated
vapour
-5
Dew
(Saturated)
T em p erature [C ]
-10
Temp/concentration
of last vapour to
condense
Two-phase
-15
-20
-25
-30
-35
Temp/concentration
of first liquid
condensed
-40
-45
-50
Subcooled
liquid
-55
-60
0
10 15 20 25 30 35 40 45 50 55 60 65 70 75 80 85 90 95 100
Weight-% Ethane
26
T em p eratu re [C ]
60
40
25
20
20
15
10
-20
2 bar
-40
-60
-80
-800
p = 1 bar
-700
-600
-500
-400
-300
-200
-100
100
200
300
Enthalpy [kJ/kg]
13
27
Shell
Linde/Statoil MFC Mixed Fluid Cascade Process (Snhvit, 4.3 Mtpa start up 2007)
28
45 bar
1.4 bar
19 bar
1.4 bar
LNG -155 C
-96 C
-32 C
7 bar
12 C
NG
Methane
Ethylene
Propane
14
29
T em p eratu re [C ]
60
40
25
20
20
15
10
-20
2 bar
-40
-60
p = 1 bar
-80
-800
-700
-600
-500
-400
-300
-200
-100
100
200
300
Enthalpy [kJ/kg]
30
NG
12 C
30 bar
NG
6,5 C
12 C
99,8 C
-155 C
LN
G
5 bar
-155 C
-155,5 C
Refrig
C1
0.897 0.360
C2
0.055 0.280
C3
0.018 0.110
nC4
0.001 0.150
N2
0.028 0.100
15
31
Temperature - Enthalpy
150
100
Temperature, C
50
NG 60 bar
-150
-200
-1500
-1000
-500
500
1000
1500
32
(MFC)
process (Linde-Statoil)
NG
PrePre-cooling
Section
E1A
E1B
C1
Liquefaction
Section
E2
CW2
C2
SubSub-cooling
Section
E3
LNG
CW
3A/B
G
X1
C3
16
33
Natural gas
from pre-processing
Precooling
-25oC
-50oC
Scrubber column
LPG Fractionation
Refrigerant make-up
34
Feedgas from
pre-processing
Precooling
Liquefaction
Subcooling
CH4 from
nitrogen
removal
N2/CH4 to
nitrogen
removal
LPG Fractionation
Refrigerant make-up
LNG
17
35
36
320
280
Heat [MW]
240
200
160
120
R
e
b
o
i
l
e
r
Liquefaction
Refrigerant
Subcooling Refrigerant
Precooling Refrigerant
80
40
0
110
130
150
170
190
210
230
250
270
290
Temperature [K]
Hot (sum)
Cold (sum)
18
37
Precooling cicruit
25-133
SW
25-262
25-171
25-UV-1009
25-UV-1308
25-129
25-164
27
25-HX-103
25-166
25-158
25-TV-1268
25-128
46A
25-162
25-HG-103 A/B
25-161
25-HV-1302
25-HX-101
25-125
25-VE-102
25-154
25-181
25-132
25-131
SC I
SC II
25-UV-1878
25-130
25-121
25-169
25-163
25-127
25-281.1
25-254
25-PV-1255B
42-104
25-124
25-257
25-149
42
25-155
25-156
25-149.1
25-FV-1203
27A
25-137
25-179
25-HX-102
25-PV-1559
25-135
25-256
25-FV-1236A
25-FV-1236B
26
25-PV-1560B
25-PV-1560C
25-VD-104
25-PA-102 A/B
25-FV-1543
25-132.2
25-141
25-PV-1282A
25-HV-1138
25-255
25-148
25-253
25-211
25-143
25-CT-101
25-EG-101
25-VD-106
25-259
46A
25-260
26A
25-140.2
25-140.1
25-165
25-261
26B
25-FV-1451
26-139
25-FV-1562A
25-FV-1562B
25-144.1
25-KA-103
25-120
27A
25-PV-1282B
25-PV-1561B
25-PV-1561C
25-VD-114
START-UP LINE
25-VD-107A
25-173
25-UV-1010
25-209
25-177
27A
25-133.1
25-258
25-136
25-183
LC
25-KA-102
25-140
26-174
25-VD-107
25-VD-105
25-223
25-FV-1221A
25-FV-1221B
25-113
25-VD-112
25-VD-110
25-133.2
25-820
25-115
25-225
MIN. FLOW
25-122.1
25-PV-1561A
25-FV-1227A
25-FV-1227B
25-215
25-121.1
25-202
25-PV-1560A
25-122.2
25-810
26-205
25-196
25-UV-1548
25-203
25-818
25-816
25-116
25-FV-1546
ANTISURGE
25-118
25-LV-1435A
25-LV-1435B
25-817
25-819
25-UV-1877
27A
25-189
25-114
25-806
25-219
25-102
25-KA-101
25-117
25-808
25-121.2
25-LV-1327A
25-LV-1327B
SW
25-HA-113
ANTISURGE
25-206
25-807
25-141
PC
25-105
25-117
42
25-196.1
25-196.3
25-196.2
25-FV-1549
25-205
25-VD-101
25-196.4
25-UV-1879
ANTISURGE
START UP RECYCLE
ANTISURGE
25-815
25-HA-104
SW
25-132.1
25-202
25-200
MIN. FLOW
26A
26-140
25-168
26-102
25-106
25-FV-1550
26B
25-114
25-190
25-HG-102 A-F
25-809
25-280
26-112
25-811
25-VD-111
26D
25-112
25-142
26-184
25-271
25-812
25-813
25-FV-1224A
25-FV-1224B
25-HG-101 A-D
25-LV-1430A
25-LV-1430B
25-268
26-175
25-109
25-FV-1219A
25-FV-1219B
25-805
26-180
25-801
25-272
26C
25-108
25-804
25-139
25-VD-109
25-803
25-802
26D
25-LV-1448
25-248
25-LV-1321A
25-LV-1321B
26C
25-111
25-LV-1463
25-252
25-VE-101
25-195
25-UV-1012
25-274
25-VD-102
25-UV-1011
25-273
25-VD-116
25-HG-105
25-264
25-110
25-138
25-172
25-HA-114
25-201
25-279
MIN. FLOW
25-247
25-270
25-HA-101
25-263.1
25-PV-1626
25-277
25-249
25-HG-104
25-167
27-131
27-FV-1025
27-130
27
25-156.1
25-156.2
25-159
25-153
25-HA-105
25-123
25-152
25-212
HO
25-134
G
25-EG-102
25-CT-102
25-PV-1316
25-157
25-PA-103 A/B
25-144
25-FV-1654
25-FV-1657
25-FV-1531
25-126
SW
21-102
25-VD-115
25-251
SW
25-LV-1007
25-263.2
25-266
25-269
25-PV-1464
25-278
21
25-207
25-263
25-193
25-104
25-265
25-210
25-HA-111
25-103
25-VD-103
OVERVIEW
38
25-133
25-122
SW
25-HA-112
25-198
25-PA-101
A/B
25-160
42
25-FV-1725A
25-150
25-151
26
19
26-VE-101
25-HA-105
25-VE-101
25-CT-102
25-HG-101
27-VE-102
25-HX-102
25-HX-101
25-HX-103
25-VD-107
25-HG-103
25-PA-103
25-VE-102
25-HA-101
27-VE-101
25-PA-101
25-PA-102
PROSESS STRM
Classification: Internal
Status: Draft
26-VE-101
39
27-KA-101
25-HA-105
25-VE-101
25-CT-102
25-HG-102
25-HG-101
27-VE-102
25-HX-102
25-HX-101
25-HX-103
25-VD-107
25-HG-103
25-PA-103
25-VE-102
25-HA-101
27-VE-101
25-PA-101
25-PA-102
25-VD-105
25-HA-114
Classification: Internal
Status: Draft
PROSESS STRM
VSKEDANNINGSKRETS
40
25-KA-102
27-KA-101
20
26-VE-101
25-HA-105
25-VE-101
25-CT-102
25-VD-109
25-HG-102
25-HG-101
25-VD-112
25-VD-110
27-VE-102
25-HX-102
25-HX-101
25-HX-103
25-VD-107
25-HG-103
25-PA-103
25-VE-102
25-HA-101
27-VE-101
25-PA-101
25-PA-102
25-VD-105
25-HA-112
25-HA-111
25-HA-114
25-HG-105
25-HG-104
25-VD-101
PROSESS STRM
VSKEDANNINGSKRETS
41
FORKJLINGSKRETS
25-VD-115
Classification: Internal
25-VD-116
Status: Draft 25-VD-103
25-VD-102
26-VE-101
25-KA-101
25-HA-105
25-KA-102
25-VE-101
27-KA-101
25-CT-102
25-VD-109
25-HG-102
25-HG-101
25-VD-112
25-VD-110
27-VE-102
25-HX-102
25-HX-101
25-HX-103
25-VD-107
25-HG-103
25-PA-103
25-VE-102
25-HA-101
27-VE-101
25-PA-101
25-CT-101
25-PA-102
25-HA-104
25-VD-105
25-VD-106
25-HA-112
27-HA-113
25-HA-111
25-HA-114
25-HG-105
25-HG-104
25-VD-101
25-VD-115
Classification: Internal
25-VD-116
Status: Draft 25-VD-103
25-VD-102
25-KA-101
25-KA-102
27-KA-101
25-KA-103
PROSESS STRM
VSKEDANNINGSKRETS
42
FORKJLINGSKRETS
UNDERKJLINGSKRETS
21
25-HG-102
25-VD-104
25-HX-102
25-HX-101
25-VD-105
25-HA-114
25-KA-102
VSKEDANNINGSKRETS
Classification: Internal
Status: Draft
43
25-VD-109
25-HG-102
25-HG-101
25-VD-112
25-VD-110
27-HG-101
25-HA-112
25-HA-111
25-HG-105
25-HG-104
25-VD-101
25-VD-115
Classification: Internal
Status: Draft 25-VD-103
25-VD-116
44
FORKJLINGSKRETS
25-VD-102
25-KA-101
22
25-HG-102
25-VD-114
25-HX-102
25-HX-101
25-CT-101
25-HA-104
25-VD-106
27-HA-113
Classification: Internal
Status: Draft
45
25-KA-103
UNDERKJLINGSKRETS
46
23
47
Gas turbine
Direct mechanical compressor drive using gas turbine
Small plot area, low CAPEX
Most common solution today
Capacity of plant determined by available gas turbine sizes
Electric
Only Snhvit so far, but considered in several current developments
Increased availability, potential use of high-efficiency combined-cycle technology
48
24
49
Unit 25
Unit 25
NG
G
Plate Fin
Heat
Exchangers
Precooling
Cycle
Sea
water
cooling
Spiral Wound
Heat
Exchangers
Generator
PCC Compressor
Hot
oil
cycle
M
Subcooling
Cycle
LNG Expander/
Generator
LNG
Air
Fuel gas
M
Liquefaction
Cycle
5 x GE LM 6000 GT
with waste heat recovery
SCC
Exp./
Gener.
LCC Compressor
M
SCC Compressor
Electric Power
from the Grid
G
Process heat
consumers
50
25
51
On-line Availability
Fraction of time
2 circuits
GT
2 circuits
1 parallel
driver/compr
3 circuits
= 0.96
GT
0.98
0.98
GT
= 0.97
GT
0.98
GT
GT
0.99
= 0.94
GT
GT
0.98
0.98
0.98
52
Heat rejection
Air cooling
Water cooling
Tube-in-shell
heat exchanger
26
53
Heat rejection
Air cooling
Water cooling
54
27
55
28