appendix 4 technical design parameters and drawings · document no. ptac co2 enhanced hydrocarbon...

Appendix 4Technical Design Parameters and Drawings

CO2 RECOVERY STUDYPrepared for: Petroleum Technology Alliance Canada (PTAC) Project 017798, January, 2008 App 4-1 Chemicals and Petroleum

TITLE

DATE SCALEDEC 2007 NTS

DOCUMENT NO.

PTAC CO2 ENHANCED HYDROCARBON RECOVERY STUDY

RWSA DM

017798-49-01-BFD-001 Rev.A

BLOCK FLOW DIAGRAMCASE 1

DESIGNED BY CHECKED BY APPROVED

SYNTHESIS GAS

FROM PETROCANADA SMR/HTS PHASE 1

PRELIMINARY DRAWING

HYDROGEN RICH GAS

TO PETROCANADA PSA PHASE 1 FUEL GAS

CO2 TO INJECTION

HP STEAM

LP STEAM

ABSORPTION REGENERATION

DRIVER9,505 kW

LP COMPRESSOR2 STAGES

HP COMPRESSOR3 STAGES

DEHYDRATION

249,000 Sm3/h114 t/h

2070 kPag38 ºC

CO2: 18% (vol.)H2: 74% (vol.)

MAKEUP WATER

208,000 Sm3/h36.9 t/h

2060 kPag45 ºC

3.7 t/h

CO2: 1.5% (vol.)H2: 88.5% (vol.)

46,400 Sm3/h81 t/h

26 kPag50 ºC

CO2: 89.3% (vol.)

1755 kPag

78.2 t/h6150 kPag

399 ºC

281 kPag142 ºC

19,075 kPag60 ºC

CO2: 99.5% (vol.)

41,770 Sm3/h77.3 t/h

28 Sm3/h21 kg/h

1848 t/dPIPELINE6", 1.5 km

POWER

DRIVER16,780 kW



CO2: 99.4% (vol.)

1755 kPag

19,290 kPag60 ºC

CO2: 99.4% (vol.) 3480 t/d

PIPELINE6", 1.5 km

78,400 Sm3/h145 t/h

16 kPag17 ºC

18,616 kPag396 t/h9504 t/d

SYNTHESIS GAS

HYDROGEN RICH GAS

TO SHELL PSA EXISTING

FUEL GAS

HP STEAM

LP STEAM

ABSORPTION

REGENERATION

DRIVER21,480 kW



DEHYDRATION

324,000 Sm3/h149 t/h

2070 kPag38 ºC

CO2: 18% (vol.)H2: 74% (vol.)

MAKEUP WATER

269,000 Sm3/h47 t/h

2060 kPag45 ºC

8.2 t/h

CO2: 1.5% (vol.)H2: 88.5% (vol.)

104,500 Sm3/h182 t/h

26 kPag50 ºC

CO2: 89.3% (vol.)

1755 kPag

177 t/h6150 kPag

399 ºC

281 kPag142 ºC

19,829 kPag60 ºC

CO2: 99.5% (vol.)

94,100 Sm3/h174 t/h

62 Sm3/h46 kg/h

4176 t/dPIPELINE8", 8 km

SYNTHESIS GAS

HYDROGEN RICH GAS

TO SHELL PSA PHASE 1

237,000 Sm3/h109 t/h

2070 kPag38 ºC

197,000 Sm3/h35 t/h

2060 kPag45 ºC

ABSORPTION

FROM SHELL SMR/HTS EXISTING

FROM SHELL SMR/HTS PHASE 1

GASIFIER OFF GAS

FROM NORTH WEST UPGRADER

BOILER60.2 MW

BOILER136 MW

FUEL GAS

FUEL GAS

8,080 Sm3/h6 t/h

18,250 Sm3/h13.6 t/h

WATER

WATER263 kg/h

117 kg/h

PETROCANADA SITE

NORTH WEST UPGRADING SITE

SHELL SITE

COMMON DELIVERY POINT

TITLE


DOCUMENT NO.


RWSA DM

017798-49-02-BFD-001 Rev.A



SYNTHESIS GAS


PRELIMINARY DRAWING

HYDROGEN RICH GAS

TO PETROCANADA PSA PHASE 1

FUEL GAS

CO2 TO INJECTIONHP STEAM

LP STEAM


DRIVER5,506 kW



DEHYDRATION

249,000 Sm3/h114 t/h

2070 kPag38 ºC

CO2: 18% (vol.)H2: 74% (vol.)

MAKEUP WATER

208,000 Sm3/h36.9 t/h

2060 kPag45 ºC

3.7 t/h

CO2: 1.5% (vol.)H2: 88.5% (vol.)

46,400 Sm3/h81 t/h

26 kPag50 ºC

CO2: 89.3% (vol.)

66 t/h6150 kPag

399 ºC

1052 kPag223 ºC

135,900 Sm3/h251.4 t/h

90 Sm3/h67 kg/h

PIPELINE10", 1.5 km

POWER

DRIVER16,780 kW



CO2: 99.4% (vol.)

1755 kPag

19,290 kPag60 ºC

CO2: 99.4% (vol.) 3480 t/d

PIPELINE6", 1.5 km

78,400 Sm3/h145 t/h

16 kPag17 ºC

18,616 kPag396 t/h9504 t/d

SYNTHESIS GAS

HYDROGEN RICH GAS


HP STEAM

LP STEAM

ABSORPTION

REGENERATION

DRIVER13,620 kW


324,000 Sm3/h149 t/h

2070 kPag38 ºC

CO2: 18% (vol.)H2: 74% (vol.)

MAKEUP WATER

269,000 Sm3/h47 t/h

2060 kPag45 ºC

8.2 t/h

CO2: 1.5% (vol.)H2: 88.5% (vol.)

104,500 Sm3/h182 t/h

26 kPag50 ºC

CO2: 89.3% (vol.)

151 t/h6150 kPag

399 ºC

866 kPag208 ºC

1749 kPag43 ºC

CO2: 99% (vol.)

PIPELINE18", 8 km

SYNTHESIS GAS

HYDROGEN RICH GAS


237,000 Sm3/h109 t/h

2070 kPag38 ºC

197,000 Sm3/h35 t/h

2060 kPag45 ºC

ABSORPTION



GASIFIER OFF GAS


BOILER51 MW

BOILER116.4 MW

FUEL GAS

FUEL GAS

6845 Sm3/h5.1 t/h

15615 Sm3/h11.7 t/h

WATER445 kg/h

PETROCANADA SITE


SHELL SITE


DRIVER15,200 kW

POWER

1369 kPag43 ºC

CO2: 98.9% (vol.)

TITLE


017798-49-03-BFD-001 Rev.A



DOCUMENT NO.


RWSA DM

SYNTHESIS GAS


PRELIMINARY DRAWING

HYDROGEN RICH GAS

TO PETROCANADA PSA PHASE 1 FUEL GAS

CO2 TO INJECTION

HP STEAM

LP STEAM


DRIVER9,420 kW



DEHYDRATION

249,000 Sm3/h114 t/h

2070 kPag38 ºC

CO2: 18% (vol.)H2: 74% (vol.)

MAKEUP WATER

208,000 Sm3/h36.9 t/h

2060 kPag45 ºC

3.7 t/h

CO2: 1.5% (vol.)H2: 88.5% (vol.)

46,400 Sm3/h81 t/h

26 kPag50 ºC

CO2: 89.3% (vol.)

1749 kPag

77.5 t/h6150 kPag

399 ºC

281 kPag142 ºC

13,610 kPag60 ºC

CO2: 99.5% (vol.)

41,770 Sm3/h77.3 t/h

28 Sm3/h21 kg/h

1848 t/d

PIPELINE6", 1.5 km

POWER

DRIVER16,780 kW



CO2: 99.4% (vol.)

1755 kPag

13,870 kPag60 ºC

CO2: 99.4% (vol.) 3480 t/d

PIPELINE6", 1.5 km

78,400 Sm3/h145 t/h

16 kPag17 ºC

18,616 kPag396 t/h9504 t/d

SYNTHESIS GAS

HYDROGEN RICH GAS


FUEL GAS

HP STEAM

LP STEAM

ABSORPTION

REGENERATION

DRIVER21,440 kW



DEHYDRATION

324,000 Sm3/h149 t/h

2070 kPag38 ºC

CO2: 18% (vol.)H2: 74% (vol.)

MAKEUP WATER

269,000 Sm3/h47 t/h

2060 kPag45 ºC

8.2 t/h

CO2: 1.5% (vol.)H2: 88.5% (vol.)

104,500 Sm3/h182 t/h

26 kPag50 ºC

CO2: 89.3% (vol.)

1749 kPag

176.4 t/h6150 kPag

399 ºC

281 kPag142 ºC

14,470 kPag60 ºC

CO2: 99.5% (vol.)

94,100 Sm3/h174 t/h

62 Sm3/h46 kg/h

4176 t/d

PIPELINE8", 8 km

SYNTHESIS GAS

HYDROGEN RICH GAS


237,000 Sm3/h109 t/h

2070 kPag38 ºC

197,000 Sm3/h35 t/h

2060 kPag45 ºC

ABSORPTION



GASIFIER OFF GAS


BOILER59.6 MW

BOILER135.7 MW

FUEL GAS

FUEL GAS

8000 Sm3/h6 t/h

18,210 Sm3/h13.6 t/h

WATER

WATER263 kg/h

117 kg/h

PETROCANADA SITE


SHELL SITE


POWER1,443 kW

12,980 kPag

TITLE


DOCUMENT NO.


RWSA DM

017798-49-04-BFD-001 Rev.A



SYNTHESIS GAS


PRELIMINARY DRAWING

HYDROGEN RICH GAS

TO PETROCANADA PSA PHASE 1

FUEL GAS

CO2 TO INJECTION

HP STEAM

LP STEAM

ABSORPTION

REGENERATION

DRIVER30,880 kW



DEHYDRATION

249,000 Sm3/h114 t/h

2070 kPag38 ºC

CO2: 18% (vol.)H2: 74% (vol.)

MAKEUP WATER

208,000 Sm3/h36.9 t/h

2060 kPag45 ºC

3.7 t/h

CO2: 1.5% (vol.)H2: 88.5% (vol.)

151,000 Sm3/h263 t/h

19 kPag50 ºC

CO2: 89.3% (vol.)1749 kPag

254 t/h6150 kPag

399 ºC

281 kPag142 ºC

135,900 Sm3/h251 t/h

28 Sm3/h21 kg/h

PIPELINE12", 1.5 km

POWER

DRIVER 16,780 kW



CO2: 99.4% (vol.)

1755 kPag

19,290 kPag60 ºC

CO2: 99.4% (vol.)

6024 t/dCO2: 99.5% (VOL.)

PIPELINE6", 1.5 km

78,400 Sm3/h145 t/h

16 kPag17 ºC

18,616 kPag396 t/h9504 t/d

SYNTHESIS GAS

HYDROGEN RICH GAS


ABSORPTION

324,000 Sm3/h149 t/h

2070 kPag38 ºC

CO2: 18% (vol.)H2: 74% (vol.)

MAKEUP WATER

269,000 Sm3/h47 t/h

2060 kPag45 ºC

8.2 t/h

CO2: 1.5% (vol.)H2: 88.5% (vol.)

SYNTHESIS GAS

HYDROGEN RICH GAS


237,000 Sm3/h109 t/h

2070 kPag38 ºC

197,000 Sm3/h35 t/h

2060 kPag45 ºC

ABSORPTION



GASIFIER OFF GAS


BOILER195.5 MW

FUEL GAS

WATER382 kg/h

PETROCANADA SITE


SHELL SITE


26,235 Nm3/h20 t/h

PIPELINE12", 1.5 km

RICH AMINE

LEAN AMINE

LEAN AMINE

RICH AMINE

PIPELINE20", 8 km

PIPELINE20", 8 km

3480 t/d

TITLE

DATE SCALENOV 2007 NTS

DOCUMENT NO.


RWSA DM

017798-49-01-PFD-001 Rev.A

CASE 1. PROCESS FLOW DIAGRAMPETROCANADA UPGRADER PHASE 1

CARBON DIOXIDE CAPTUREDESIGNED BY CHECKED BY APPROVED

002

SYNTHESIS GAS

FROM SMR/HTS PHASE 1

T-001CO2 ABSORPTION TOWER

CARBON DIOXIDE

TO COMPRESSION

PRELIMINARY DRAWING. DO NOT USE FOR CONSTRUCTION

LP STEAM

STEAM CONDENSATE

T-001

T-002REGENERATION TOWER

T-002

78.2 to/h

142 ºC

281 kPag

3

4

RETURN

1

249 kSm 3/h

38 ºC

2070 kPag

114 to/h

46.4 kSm 3/h

50 ºC

26 kPag

80.8 to/h

NOTES:1. ALL WEIGHT FLOWRATES REPRESENT ACTUAL ON STREAM RATES

HYDROGEN RICH GAS

TO PSA PHASE 1

2

208 kSm 3/h

45 ºC

2060 kPag

36.9 to/h

NN

F

EA-001

EA-002

E-001

E-002

EA-001LEAN AMINE COOLER

EA-002CONDENSER

E-001LEAN-RICH AMINE EXCHANGER

E-002REGENERATION TOWER REBOILER

P-001

P-001LEAN AMINE PUMP

V-001

V-001FLASH

002

MAKEUP WATER5

3.7 to/h

TITLE



RWSA DMDOCUMENT NO.

017798-49-01-PFD-002 Rev. A


CARBON DIOXIDE LOW PRESSURE COMPRESSIONDESIGNED BY CHECKED BY APPROVED

001

FROM CAPTURE

CARBON DIOXIDE

HEADER

WASTE WATER

V-002ALP COMPRESSOR STAGE 1 INLET SEPARATOR

DIMENSIONS: 3048 mm ID x 3048 mm T/T

V-002BLP COMPRESSOR STAGE 2 INLET SEPARATOR


K-001ACO2 LP COMPRESSOR STAGE 1

DIFF. PRESS.: 432 kPa

K-001BCO2 LP COMPRESSOR STAGE 2


EA-003ALP COMPRESSOR STAGE 1 AFTERCOOLER

DUTY: 5476 KW

EA-003BLP COMPRESSOR STAGE 2 AFTERCOOLER

DUTY: 3212 KW


197 ºC

450 kPag

43 ºC

179 ºC

1887 kPag

43 ºC

43 ºC

1756 kPag

HP STEAM

003

TO HIGH PRESSURE COMPRESSION

CARBON DIOXIDE

003

COMMON SHAFT WITH HIGH PRESSURE COMPRESSOR

X-001CO2 COMPRESSOR STEAM TURBINE DRIVER

RATED POWER: 9505 KW (NOTE 3)

VENDOR PACKAGE

PK-001

NN

F

43.7 kAm 3/h

50 ºC

19 kPag

80.8 to/h

NOTE 1 NOTE 1

NOTES:1. ALL DISCHARGE PRESSURES AND TEMPERATURES ARE THE ORETICAL. ACTUAL OPERATION PARAMETERS BY COMPRESSOR VENDOR2. ALL WEIGHT FLOWRATES REPRESENT ACTUAL ON STREAM RATES3. RATED POWER INCLUDES ESTIMATED 3% POWER LOSS. AC TUAL RATED POWER BY VENDOR

DRAWING # 017798-49-00-PFD-003

K-001A X-001K-001B

EA-003A EA-003B

V-002A V-002B V-002C

7

78.2 to/h

399 ºC

6149 kPag

001

LP STEAM

TO CAPTURE

4

142 ºC

281 kPag

GEAR BOX

6

PK-001CO2 COMPRESSOR PACKAGE

CAPACITY: 46500 Sm3/h

V-002CLP COMPRESSOR STAGE 2 OUTLET SEPARATOR


TITLE

DATE SCALENOV 2007 NTS RWSA DM


DOCUMENT NO.017798-49-01-PFD-003 Rev. A


CARBON DIOXIDE HIGH PRESSURE COMPRESSIONDESIGNED BY CHECKED BY APPROVED

002

FROM LOW PRESSURE COMPRESSION

CARBON DIOXIDE004

TO DEHYDRATION

CARBON DIOXIDE

WASTE WATER

V-003HP COMPRESSOR STAGE 1 OUTLET SEPARATOR


K-002ACO2 HIGH PRESSURE COMPRESSOR STAGE 1


K-002BCO2 HIGH PRESSURE COMPRESSOR STAGE 2


EA-004AHP COMPRESSOR STAGE 1 AFTERCOOLER

DUTY: 1846 KW

EA-004BHP COMPRESSOR STAGE 2 AFTERCOOLER

DUTY: 3191 KW

EA-004CHP COMPRESSOR STAGE 3 AFTERCOOLER

DUTY: 2297 KW

004

FROM DEHYDRATION

CARBON DIOXIDE

TO PIPELINE

CARBON DIOXIDE

K-002CCO2 HIGH PRESSURE COMPRESSOR STAGE 3



119 ºC

4104 kPag

43 ºC

8

9

10

11

3.6 to/h

43 ºC

103 ºC

19200 kPag

77.2 to/h

60 ºC

19072 kPag

COMMON SHAFT WITH LOW PRESSURE COMPRESSOR

77.3 to/h

43 ºC

3974 kPag

HEADER

WASTE WATER

002

DRAWING # 017798-49-00-PFD-002

129 ºC

8586 kPag

77.2 to/h

48 ºC

3766 kPag

NOTES:1. ALL DISCHARGE PRESSURES AND TEMPERATURES ARE THE ORETICAL. ACTUAL OPERATION PARAMETERS BY COMPRESSOR VENDOR2. ALL WEIGHT FLOWRATES REPRESENT ACTUAL ON STREAM RATES

K-002A K-002B K-002C

V-003

EA-004A

EA-004C

43 ºC

6

EA-004B

NOTE 1 NOTE 1

NOTE 1

TITLE


017798-49-01-PFD-004 Rev. A


CARBON DIOXIDE DEHYDRATIONDESIGNED BY CHECKED BY APPROVED

SA DM


RW

DOCUMENT NO.

CARBON DIOXIDE

FROM HP COMPRESSION

003

003

CARBON DIOXIDE

TO HP COMPRESSION

WATER VAPOR TO ATMOSPHERE

VENTTO ATMOSPHERE


12

21 kg/h

28 Sm3/h FUEL GAS

FLUE GAS TO ATMOSPHERE

CO2 DEHYDRATION VENDOR PACKAGE

NOTE 1

PK-002 CO2 DEHYDRATION PACKAGECAPACITY: 1853 TPD (DRY CO2)

PK-002

NOTES:1. VENDOR PACKAGE INTERNAL CONFIGURATION IS FOR INF ORMATION ONLY. THE ACTUAL CONFIGURATION MAY BE DIFF ERENT.2. ALL WEIGHT FLOWRATES REPRESENT ACTUAL ON STREAM RATES

13

0.4 to/h

TITLE


017798-49-01-PFD-005 Rev.A

PROCESS FLOW DIAGRAMSHELL EXISTING AND PHASE 1 UPGRADERS

CARBON DIOXIDE CAPTUREDESIGNED BY CHECKED BY APPROVED

DOCUMENT NO.


RWSA DM

006

T-003/ACO2 ABSORPTION TOWER

CARBON DIOXIDE

TO COMPRESSION


LP STEAM

STEAM CONDENSATE

T-003A

T-004REGENERATION TOWER

T-004

177 to/h

142 ºC

281 kPag

18

19

20

RETURN

14

324 kSm 3/h

38 ºC

2070 kPag

149 to/h

104.5 kSm 3/h

50 ºC

26 kPag

182 to/h

NOTES:1. ALL WEIGHT FLOWRATES REPRESENT ACTUAL ON STREAM RATES

TO EXISTING PSA

15

269 kSm 3/h

45 ºC

2060 kPag

46.9 to/h

NN

F

EA-005EA-006

E-003

E-004

EA-005LEAN AMINE COOLER

EA-006CONDENSER

E-003LEAN-RICH AMINE EXCHANGER

E-004REGENERATION TOWER REBOILER

P-002

P-002LEAN AMINE PUMP

V-004

V-004FLASH

006

T-003B

16

237 kSm 3/h

38 ºC

2070 kPag

109 to/h

TO PSA PHASE 1

17

197 kSm 3/h

45 ºC

2060 kPag

35 to/h

NN

F

SYNTHESIS GAS

FROM SMR/HTS PHASE 1

HYDROGEN RICH GAS

SYNTHESIS GAS

FROM EXISTING SMR/HTS

HYDROGEN RICH GAS

MAKEUP WATER 8.2 to/h

T-003/BCO2 ABSORPTION TOWER

TITLE



CASE 1. PROCESS FLOW DIAGRAMSHELL EXISTING AND PHASE 1 UPGRADERS



RWSA DM

005

FROM CAPTURE

CARBON DIOXIDE

HEADER

WASTE WATER










DUTY: 12330 KW


DUTY: 7234 KW


197 ºC

450 kPag

43 ºC

179 ºC

1887 kPag

43 ºC

43 ºC

1756 kPag

HP STEAM

007


CARBON DIOXIDE

007


X-002CO2 COMPRESSOR STEAM TURBINE DRIVER


VENDOR PACKAGE

PK-003

NN

F

98.4 kAm 3/h

50 ºC

19 kPag

182 to/h

NOTE 1 NOTE 1

NOTE 1

NOTES:1. ALL DISCHARGE PRESSURES AND TEMPERATURES ARE THE ORETICAL. ACTUAL OPERATION PARAMETERS BY COMPRESSOR VENDOR2. ALL WEIGHT FLOWRATES REPRESENT ACTUAL ON STREAM RATES3. RATED POWER INCLUDES ESTIMATED _ KW POWER LOSS. ACTUAL RATED POWER BY VENDOR

DRAWING # 017798-49-00-PFD-007

K-003A X-002K-003B

EA-007A EA-007B

V-005A V-005B V-005C

22

177 to/h

399 ºC

6149 kPag

005

LP STEAM

TO CAPTURE

19

142 ºC

281 kPag

GEAR BOX

21





18

TITLE





RWSA DM


006


CARBON DIOXIDE

008

TO DEHYDRATION

CARBON DIOXIDE

WASTE WATER








DUTY: 4157 KW


DUTY: 7623 KW


DUTY: 4945 KW

008

FROM DEHYDRATION

CARBON DIOXIDE

TO PIPELINE

CARBON DIOXIDE




119 ºC

4104 kPag

43 ºC

23

24

25

26

8 to/h

43 ºC

101 ºC

19960 kPag

173.8 to/h

60 ºC

19829 kPag


174 to/h

43 ºC

3974 kPag

HEADER

WASTE WATER

006

DRAWING # 017798-49-00-PFD-006

131 ºC

8793 kPag

173.8 to/h

48 ºC

3965 kPag


K-004A K-004B K-004C

V-006

EA-008A

EA-008C

43 ºC

21

EA-008B

TITLE

DATE SCALE#REF! NTS


RW



CARBON DIOXIDE DEHYDRATIONDESIGNED BY CHECKED BY APPROVED

SA DM

CARBON DIOXIDE

FROM HP COMPRESSION

007

007

CARBON DIOXIDE

TO HP COMPRESSION

WATER VAPOR TO ATMOSPHERE

VENTTO ATMOSPHERE


27

46 kg/h

62 Sm3/h FUEL GAS

FLUE GAS TO ATMOSPHERE

CO2 DEHYDRATION VENDOR PACKAGE

NOTE 1

PK-004 CO2 DEHYDRATION PACKAGECAPACITY: 4171 TPD (DRY CO2)

PK-004

NOTES:1. VENDOR PACKAGE INTERNAL CONFIGURATION IS FOR INF ORMATION ONLY. THE ACTUAL CONFIGURATION MAY BE DIFF ERENT.2. ALL WEIGHT FLOWRATES REPRESENT ACTUAL ON STREAM RATES

28

1 to/h

TITLE



RWSA DMDOCUMENT NO.

017798-49-01-PFD-009 Rev. A

CASE 1. PROCESS FLOW DIAGRAMNORTH WEST UPGRADER


FROM RECTISOL UNIT

CARBON DIOXIDE

HEADER

WASTE WATER










DUTY: 4082 KW


DUTY: 5818 KW


151 ºC

409 kPag

43 ºC

189 ºC

1887 kPag

43 ºC

43 ºC

1756 kPag

010


CARBON DIOXIDE

010


KM-005CO2 COMPRESSOR DRIVER


VENDOR PACKAGE

PK-005

NNF

NOTE 1 NOTE 1

NOTE 1

NOTES:1. ALL DISCHARGE PRESSURES AND TEMPERATURES ARE THE ORETICAL. ACTUAL OPERATION PARAMETERS BY COMPRESSOR VENDOR2. ALL WEIGHT FLOWRATES REPRESENT ACTUAL ON STREAM RATES3. RATED POWER INCLUDES ESTIMATED _ KW POWER LOSS. ACTUAL RATED POWER BY VENDOR

DRAWING # 017798-49-00-PFD-010

K-005A K-005B

EA-009A EA-009B

V-007A V-007B V-007C

GEAR BOX

30





29

78.4 kSm 3/h

17 ºC

16 kPag

145 to/h

KM-005

TITLE

DATE SCALENOV 2007 NTS DM



CASE 1. PROCESS FLOW DIAGRAMNORTH WEST UPGRADER


RWSA

009


CARBON DIOXIDE

WASTE WATER








DUTY: 3370 KW


DUTY: 5377 KW


DUTY: 4410 KW

TO PIPELINE

CARBON DIOXIDE




119 ºC

4104 kPag

43 ºC

31

104 ºC

19420 kPag

145 to/h

60 ºC

19290 kPag


HEADER

WASTE WATER

009

DRAWING # 017798-49-00-PFD-009

117 ºC

8586 kPag


K-006A K-006B K-006C

V-008

EA-010A

EA-010C

43 ºC

30

EA-010B

NNF

Rev./Date By Checked ApprovedA /Dec. 2007 RT / RW SA DM

Project:Doc. #:Page

Stream Number Units 1 2 3 4 5 6 7 8 9 10 11 12 13

Stream DescriptionSynthesis gas from SMR/HTS

phase 1

Hydrogen rich gas to PSA

phase 1

Carbon dioxide to compression - Petro-Canada

Upgrader Phase 1

LP steam to capture Petro-

Canada Upgrader Phase

1

Make up water to capture Petro-

Canada Upgrader Phase 1

Carbon dioxide high pressure compression Petro-Canada

Upgrader Phase 1

HP steam to carbon dioxide compression Petro-Canada

Upgrader Phase 1

Carbon dioxide to dehydration - Petro-Canada

Upgrader Phase 1

Carbon dioxide from

dehydration - Petro-Canada

Upgrader Phase 1

Carbon dioxide from

Petrocanada SMR to Pipeline

Waste water from Petro-

Canada Upgrader Phase

1

Fuel gas to dehydration

package - Petro-Canada

Upgrader Phase 1

Flue gas to atmosphere

from dehydration

package - Petro-Canada

Upgrader Phase 1

Vapor Weight Fraction 1.00 1.00 1.00 0.99 0.00 1.00 1.00 1.00 1.00 0.00 0.00 1.00 1.00Temperature ºC 38 45 50.0 135 30.0 43.0 399.0 43.0 48.0 60.0 43.0 40.0 200.0Pressure kPag 2070 2060 25.8 217 2060.0 1756.4 6148.8 3973.7 3766.9 19071.5 25.8 8.7 0.0Molar Rate kg-mol/hr 10550 8785 1963 3990 203.0 1770 3990 1767 1760 1760 197 1.17 14.6Mass Rate Ton/hr 114 36.9 80.8 71.9 3.66 77.3 71.9 77.3 77.2 77.2 3.55 0.021 0.406Actual Volumetric Flow Am3/hr 12700 10900 43689 41565 3.70 2293 3254.021 909 999 116 11.76 27.6 565Standard Volumetric Flow Sm3/hr 249000 208000 46418 94349 3.661 41859 94349 41770 41617 N/A 3.56 27.6 344Enthalpy GJ/h 98.5 83.2 -737.6 -950.9 N/A -692.7 -916.7 -693.7 -691.4 -703.7 -56.0 -0.095 -0.99Molecular Weight 10.8 4.2 41.2 18.0 18.0 43.7 18.0 43.7 43.8 43.8 18.1 17.7 27.9Actual Density kg/m3 9.02 3.38 1.8 1.7 987.60 33.721 22.1 85.045 77.250 667.08 302.12 0.748 0.718Dynamic Viscosity cP 0.014 0.011 0.015 N/A 0.540 0.016 0.025 0.017 0.018 0.049 N/A 0.012 0.023Thermal Conductivity W/m-ºC 0.11 0.15 0.019 N/A N/A 0.020 0.062 0.023 0.023 0.038 N/A 0.034 0.036Specific Heat kJ/kg-ºC 31.5 30.2 0.940 2.234 4.200 0.990 2.579 1.210 1.159 2.726 4.299 2.157 1.151Surface Tension dyne/cm N/A N/A N/A 51.81 N/A N/A N/A N/A N/A 0.01 68.94 N/A N/ACompressibility 1.01 1.01 0.9940 N/A N/A 0.9120 0.9110 0.7959 0.8205 0.4547 N/A 0.9976 0.9997Composition

Carbon dioxide % weight 72.9 15.8 95.44 0.00 0.00 99.71 0.00 99.80 99.95 99.86 0.55 4.74 13.58Water % weight 0.5 1.9 4.5 100.0 100.00 0.25 100.0 0.16 0.01 0.09 99.45 0.00 10.53

Carbon monoxide % weight 2.6 8.0 0.01 0.00 0.00 0.01 0.00 0.01 0.01 0.01 0.00 0.00 0.00

Methane % weight 10.3 31.9 0.02 0.00 0.00 0.02 0.00 0.02 0.02 0.02 0.00 82.79 0.00Hydrogen % weight 13.7 42.4 0.02 0.00 0.00 0.02 0.00 0.02 0.02 0.02 0.00 0.00 0.00

Nitrogen % weight 0.0 0.0 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.32 72.83

Argon % weight 0.0 0.0 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00

Methanol % weight 0.0 0.0 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00

17798017798-49-01-HM-001

HEAT AND MATERIAL BALANCE

1 of 3

Client:



Project:Doc. #:Page

Stream Number Units 14 15 16 17 18 19 20 21 22 23 24 25 26

Stream DescriptionSynthesis gas from existing

SMR/HTS

Hydrogen rich gas to existing

PSA

Synthesis gas from SMR/HTS

phase 1

Hydrogen rich gas to PSA

phase 1

Carbon dioxide to compression from

capture Shell existing and

phase 1 upgraders

LP steam to capture - Shell

existing and phase 1

upgraders

Make up water - Shell existing and phase 1 upgraders

Carbon dioxide to high pressure compression - Shell existing and phase 1 upgraders

HP steam - Shell existing and phase 1 upgraders

Carbon dioxide from

Petrocanada SMR to

Dehydration

Carbon dioxide from

dehydration - Shell existing and phase 1 upgraders

Cabon dioxide to pipeline from Shell existing and phase 1 upgraders

Waste water from Shell

existing and phase 1

upgraders

Vapor Weight Fraction 1.00 1.00 1.00 1.00 1.00 1.00 0.00 1.00 1.00 1.00 1.00 0.00 0.00Temperature ºC 38 45 38 45 50.0 134 30.0 43.0 399.0 43.0 48.0 60.0 43.0Pressure kPag 2070 2060 2070 2060 25.8 214 2060.0 1756.4 6148.8 3973.7 3766.9 19829.3 25.8Molar Rate kg-mol/hr 13700 11390 10000 8340 4422 8996 457 3988 8996 3979 3965 3965 443Mass Rate Ton/hr 149.0 46.9 109.0 35.0 182.0 162 8.24 174.2 162.1 174.0 173.8 173.8 8.00Actual Volumetric Flow Am3/hr 16500 14200 12000 10400 98409 94528 8.34 5166 7336 2046 2250 255 26Standard Volumetric Flow Sm3/hr 324000 269000 237000 197000 104555 212704.38 8.25 94286 212704 94087 93741 93741 8.01Enthalpy GJ/h 128.0 108.0 93.6 79.0 -1661.32 -2143.93 N/A -1560.4 -2066.6 -1562.4 -1557.4 -1585.6 -126.2Molecular Weight 10.8 4.2 10.8 4.2 41.2 18.02 18.0 43.7 18.0 43.7 43.8 43.8 18.1Actual Density kg/m3 9.02 3.38 9.02 3.38 1.8 1.71 987.60 33.7 22.1 85.0 77.3 682.8 302.1Dynamic Viscosity cP 0.014 0.011 0.014 0.011 0.01 N/A 0.540 0.016 0.025 0.017 0.018 0.050 N/AThermal Conductivity W/m-ºC 0.11 0.15 0.11 0.15 0.02 N/A N/A 0.020 0.062 0.023 0.023 0.038 N/ASpecific Heat kJ/kg-ºC 31.5 30.2 31.5 30.2 0.940 2.23 4.200 0.990 2.579 1.210 1.159 2.652 4.299Surface Tension dyne/cm N/A 51.87 N/A N/A N/A N/A N/A 0.01 68.94Compressibility 1.01 1.01 1.01 1.01 0.99 N/A N/A 0.9120 0.9110 0.7959 0.8205 0.4617 N/AComposition

Carbon dioxide % weight 72.9 15.8 72.9 15.8 95.44 0.00 0.00 99.7 0.0 99.8 99.95 99.95 0.55Water % weight 0.5 1.9 0.5 1.9 4.5 100.00 100.0 0.2 100.0 0.2 0.01 0.01 99.45

Carbon monoxide % weight 2.6 8.0 2.6 8.0 0.01 0.00 0.00 0.01 0.00 0.01 0.01 0.01 0.00

Methane % weight 10.3 31.9 10.3 31.9 0.02 0.00 0.00 0.02 0.00 0.02 0.02 0.02 0.00Hydrogen % weight 13.7 42.4 13.7 42.4 0.02 0.00 0.00 0.02 0.00 0.02 0.02 0.02 0.00

Nitrogen % weight 0.0 0.0 0.0 0.0 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00

Argon % weight 0.0 0.0 0.0 0.0 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00

Methanol % weight 0.0 0.0 0.0 0.0 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00

2 of 3


17798017798-49-01-HM-001

Client:HEAT AND MATERIAL BALANCE


Project:Doc. #:Page

Stream Number Units 27 28 29 30 31

Stream Description

Fuel gas to dehydration

package - Shell existing and

phase 1 upgraders

Flue gas to atmosphere

from dehydration

package - Shell existing and

phase 1 upgraders

Carbon dioxide from rectisol

unit

Carbon dioxide to high pressure compression -

North West Upgrader

Carbon dioxide to pipeline from North West Upgrader

Vapor Weight Fraction 1.00 1.00 1.00 1.00 0.00Temperature ºC 40.0 200.0 16.5 43.0 60.0Pressure kPag 8.7 0.0 15.8 1756 19290Molar Rate kg-mol/hr 2.63 32.8 3316 3316 3316Mass Rate Ton/hr 0.046 0.915 145.2 145.2 145.168Actual Volumetric Flow Am3/hr 62.1 1274 72113 4301 217Standard Volumetric Flow Sm3/hr 62.2 776 78394 78394 N/AEnthalpy GJ/h -0.213 -2.23 -1299.4 -1298.3 -1323.8Molecular Weight 17.7 27.9 43.8 43.8 43.8Actual Density kg/m3 0.748 0.718 2.0 33.8 669.1Dynamic Viscosity cP 0.012 0.023 0.014 0.016 0.049Thermal Conductivity W/m-ºC 0.034 0.036 0.017 0.020 0.038Specific Heat kJ/kg-ºC 2.157 1.151 0.873 0.987 2.705Surface Tension dyne/cm N/A N/A N/A N/A 0.00Compressibility 0.9976 0.9997 0.9935 0.9133 0.4580Composition

Carbon dioxide % weight 4.74 13.58 99.91 99.9 99.9Water % weight 0.00 10.53 0.00 0.0 0.0

Carbon monoxide % weight 0.00 0.00 0.03 0.03 0.03

Methane % weight 82.79 0.00 0.02 0.02 0.02Hydrogen % weight 0.00 0.00 0.02 0.02 0.02

Nitrogen % weight 0.32 72.83 0.00 0.00 0.00

Argon % weight 0.00 0.00 0.00 0.00 0.00

Methanol % weight 0.00 0.00 0.01 0.01 0.01

17798017798-49-01-HM-001

HEAT AND MATERIAL BALANCE

3 of 3


Client:

Project No.:

Document #:Date By Checked Approved

Dec. 2007 VC SA DM

Rev.: A Page 1 of 5

POWER Sm3/hr DUTY Sm3/hr

kW kW kW kW V kW kWP-001 339 424 339EA-001 42 52 42EA-002 14 17 14EA-003 A 14 17 14EA-003 B 9 11 9EA-004 A 7 9 7EA-004 B 6 7 6EA-004 C 20 24 20PK-02 11 14 11

460 575 46015% 86 86

661 546

P-002 764 955 764EA-005 28 35 28EA-005 25 31 25EA-006 21 26 21EA-007 A 17 22 17EA-007 B 13 17 13EA-008 A 9 11 9EA-008 B 18 22 18EA-008 C 23 29 23PK-04 25 32 25

944 1180 94415% 177 177

1356 1121

EA-009 A 9 11 9EA-009 B 17 22 17EA-010 A 8 10 8EA-010 B 22 28 22EA-010 C 18 23 18KM-005 16780 20975 16780

17798 23781 1909615% 3567 3567

27348 22663

25536 20500

15% 3830 383029370 24330

NOTES:1. Electrical Power for Air Coolers include a 80% efficiency factor.2. All the design values include a design margin (20%).3. Preliminary Issue. To be updated based on vendor data

LEAN AMINE COOLER - SHELL

CO2 COMPRESSOR DRIVER - NORTH WEST

TOTAL SHELL

HP COMPRESSOR 2ND STAGE AFTERCOOLER - SHELLHP COMPRESSOR 3RD STAGE AFTERCOOLER - SHELL

LP COMPRESSOR 1ST STAGE AFTERCOOLER - NORTH WEST

CONTINGENCY

CO2 DEHYDRATION PACKAGE - SHELL

SUBTOTAL SHELL

CONTINGENCY

HP COMPRESSOR 1ST STAGE AFTERCOOLER - NORTH WESTHP COMPRESSOR 2ND STAGE AFTERCOOLER - NORTH WESTHP COMPRESSOR 3RD STAGE AFTERCOOLER - NORTH WEST

SUBTOTAL NORTH WEST

CONDENSER - SHELLLP COMPRESSOR 1ST STAGE AFTERCOOLER - SHELLLP COMPRESSOR 2ND STAGE AFTERCOOLER - SHELLHP COMPRESSOR 1ST STAGE AFTERCOOLER - SHELL

HP COMPRESSOR 1ST STAGE AFTERCOOLER - PETROCANADAHP COMPRESSOR 2ND STAGE AFTERCOOLER - PETROCANADAHP COMPRESSOR 3RD STAGE AFTERCOOLER - PETROCANADA


CO2 DEHYDRATION PACKAGE - PETROCANADA

CONTINGENCYTOTAL PETROCANADA

SUBTOTAL PETROCANADA

LEAN AMINE COOLER - PETROCANADACONDENSER - PETROCANADALP COMPRESSOR 1ST STAGE AFTERCOOLER - PETROCANADALP COMPRESSOR 2ND STAGE AFTERCOOLER - PETROCANADA

017798

DESIGNNORMAL

EQUIPMENT DESCRIPTION REMARKS

LEAN AMINE PUMP - SHELL

LP COMPRESSOR 2ND STAGE AFTERCOOLER - NORTH WEST

INTERMITTENTTAG NUMBER

VOLTAGE CONTINUOUS

PTAC CO2 ENHANCED HYDROCARBON RECOVERY STUDY Case 1

Utility Balance Electrical Power

017798-49-01-UB-001

LEAN AMINE PUMP - PETROCANADA

TOTAL NORTH WEST

TOTALCONTINGENCY

TOTAL MAIN OPERATION AREA

Project No.:Document #:

Date By Checked ApprovedDec. 2007 VC SA DM

Rev.: A Page 2 of 5

Sm3/hr Sm3/hr

PK-02 27.60 33.12 27.607733.00 9279.60 7733.00

7760.60 9312.72 7760.60

PK-04 62.20 74.64 62.2016734.00 20080.80 16734.00

16796.20 20155.44 16796.20

24556.80 0.00

NOTES:1. All the design values include a design margin (20%)2. Preliminary Issue. To be updated based on vendor data.

017798

CONTINUOUS INTERMITTENT


Utility Balance Natural Gas

REMARKS

017798-49-UB-001

TAG NUMBER EQUIPMENT DESCRIPTION



BOILER PACKAGE - PETROCANADA

TOTAL 24556.80 29468.16

SUBTOTAL SHELL

BOILER PACKAGE - SHELL

NORMAL DESIGN (1)

Sm3/hr Sm3/hr




Rev.: A Page 3 of 5

Sm3/hr Rate Sm3/hr Rate Sm3/hr Sm3/hr Mass Flow Rate

Ton/hr SCMH Ton/hr SCMH Ton/hr SCMH Ton/hr SCMHX-001 71.9 94349

71.9 94349

X-002 162.1 212704

162.1 212704

0.00 0.00 0.00 0.00 0.00 0.00 234.00 307053NOTES:

SHUTDOWN

SUBTOTAL SHELL

TOTAL


CO2 STEAM TURBINE DRIVER - PETROCANADA

CO2 STEAM TURBINE DRIVER - SHELL


REMARKSEMERGENCY

INTERMITENT REQUIREMENTS

STARTUP

017798-49-UB-001PTAC CO2 ENHANCED HYDROCARBON RECOVERY STUDY Case 1

Utility Balance HP Steam

017798

NORMAL



Rev.: A Page 4 of 5


Ton/d SCMH Ton/d SCMH Ton/d SCMH Ton/hr SCMH

E-002 71.9 94349

71.9 94349

E-004 162.1 212704

162.1 212704

0.00 0.00 0.00 0.00 0.00 0.00 234.00 307053NOTES:

TOTAL

SUBTOTAL SHELL

REGENERATION TOWER REBOILER - PETROCANADA

REGENERATION TOWER REBOILER - SHELL




STARTUP SHUTDOWN EMERGENCY


Utility Balance LP Steam

017798-49-UB-001

REMARKS

NORMAL

017798



Rev.: A Page 5 of 5


Ton/d SCMH Ton/d SCMH Ton/d SCMH Ton/hr ACMH

3.66 3.70

3.66 3.70

8.24 8.34

8.24 8.34

0.00 0.00 0.00 0.00 0.00 0.00 11.90 12NOTES:


Utility Balance Make-up Water

017798017798-49-UB-001


INTERMITENT REQUIREMENTSNORMAL

REMARKSSTARTUP SHUTDOWN EMERGENCY

CO2 CAPTURE - PETROCANADA


CO2 CAPTURE - SHELL

SUBTOTAL SHELL

TOTAL

Project No.:


Dec. 2007 RT SA DM

Rev.: A Page 1 of 5

POWER Sm3/hr DUTY Sm3/hrkW kW kW kW V kW kW

P-001 339 424 339EA-001 42 52 42EA-002 14 17 14EA-003 A 14 17 14EA-003 B 9 11 9

416 521 41615% 78 78

599 495

P-002 764 955 764EA-005 28 35 28EA-005 25 31 25EA-006 21 26 21EA-007 A 17 22 17EA-007 B 13 17 13

868 1085 86815% 163 163

1248 1031

EA-008 A 19 23 19EA-008 B 21 26 21EA-008 C 75 94 75PK-04 43 53 43

15200 19000 15200

15357 19196 1535715% 2879 2879

22076 18236


16875 21093 1687515% 3164 3164

24257 20039

41895 33516

15% 6284 628448184 39801


TOTAL NORTH WEST

TOTALCONTINGENCY



VOLTAGE CONTINUOUS



017798-49-02-UB-001



017798

DESIGNNORMAL


LEAN AMINE COOLER - PETROCANADACONDENSER - PETROCANADALP COMPRESSOR 1ST STAGE AFTERCOOLER - PETROCANADALP COMPRESSOR 2ND STAGE AFTERCOOLER - PETROCANADA





HP COMPRESSOR 3RD STAGE AFTERCOOLER - COMMON DEL. PT.

CONDENSER - SHELLLP COMPRESSOR 1ST STAGE AFTERCOOLER - SHELLLP COMPRESSOR 2ND STAGE AFTERCOOLER - SHELL

TOTAL SHELL

CONTINGENCY

HP COMPRESSOR 1ST STAGE AFTERCOOLER - NORTH WESTHP COMPRESSOR 2ND STAGE AFTERCOOLER - NORTH WESTHP COMPRESSOR 3RD STAGE AFTERCOOLER - NORTH WEST

SUBTOTAL NORTH WEST



HP COMPRESSOR 1ST STAGE AFTERCOOLER - COMMON DEL. PT.HP COMPRESSOR 2ND STAGE AFTERCOOLER - COMMON DEL. PT.

SUBTOTAL COMMON DELIVERY POINTCONTINGENCYTOTAL COMMON DELIVERY POINT

CO2 COMPRESSOR DRIVER - COMMON DELIVERY POINT


CONTINGENCYSUBTOTAL SHELL

CO2 DEHYDRATION PACKAGE - COMMON DELIVERY POINT


Date By Checked ApprovedDec. 2007 RT SA DM

Rev.: A Page 2 of 5

Sm3/hr Sm3/hr

PK-02 6845 8214 6845

PK-04 15615 18738 15615

90 108 90

22550.00 0.00



NORMAL DESIGN (1)

Sm3/hr Sm3/hr

27060.0022550.00TOTAL


CO2 DEHYDRATION PACKAGE - COMMON DEL. PT.


017798




017798-49-02-UB-001

REMARKS



Rev.: A Page 3 of 5



66.0 86533

X-002 151.0 197978

151.0 197978

0.00 0.00 0.00 0.00 0.00 0.00 217.00 284511NOTES:

NORMAL

017798-49-02-UB-001PTAC CO2 ENHANCED HYDROCARBON RECOVERY STUDY Case 2


017798

REMARKSEMERGENCY


STARTUPTAG NUMBER EQUIPMENT DESCRIPTION




TOTAL

SHUTDOWN

SUBTOTAL SHELL



Rev.: A Page 4 of 5



E-002 66.0 86533

66.0 86533

E-004 151.0 197978

151.0 197978

0.00 0.00 0.00 0.00 0.00 0.00 217.00 284511NOTES:

017798-49-02-UB-001

REMARKS

NORMAL

017798









SUBTOTAL SHELL

TOTAL



Rev.: A Page 5 of 5



3.70 3.70

3.70 3.70

8.20 8.20

8.20 8.20

0.00 0.00 0.00 0.00 0.00 0.00 11.90 12NOTES:

TOTAL

SUBTOTAL SHELL

CO2 CAPTURE - SHELL








017798017798-49-02-UB-001

Project No.:


Dec. 2007 RT SA DM

Rev.: A Page 1 of 5


kW kW kW kW V kW kWP-001 339 424 339EA-001 42 52 42EA-002 14 17 14EA-003 A 14 17 14EA-003 B 9 11 9EA-004 A 10 12 10EA-004 B 7 9 7PK-02 11 14 11

445 556 44515% 83 83

639 528

P-002 764 955 764EA-005 28 35 28EA-005 25 31 25EA-006 21 26 21EA-007 A 17 22 17EA-007 B 13 17 13EA-008 A 13 16 13EA-008 B 22 28 22PK-04 25 32 25

928 1160 92815% 174 174

1334 1102

EA-009 A 9 11 9EA-009 B 17 22 17EA-010 A 11 13 11EA-010 B 30 37 30KM-005 16800 21000 16800

16867 21083 1686715% 3162 3162

24246 20029

1443 1804 144315% 271 271

2074 1714

24603 19683

15% 3690 369028298 23373


TOTAL NORTH WEST

TOTALCONTINGENCY


CO2 INJECTION PUMP


VOLTAGE CONTINUOUS



017798-49-03-UB-001



017798

DESIGNNORMAL


LEAN AMINE COOLER - PETROCANADACONDENSER - PETROCANADALP COMPRESSOR 1ST STAGE AFTERCOOLER - PETROCANADALP COMPRESSOR 2ND STAGE AFTERCOOLER - PETROCANADAHP COMPRESSOR 1ST STAGE AFTERCOOLER - PETROCANADAHP COMPRESSOR 2ND STAGE AFTERCOOLER - PETROCANADA







SUBTOTAL SHELL

CONDENSER - SHELLLP COMPRESSOR 1ST STAGE AFTERCOOLER - SHELLLP COMPRESSOR 2ND STAGE AFTERCOOLER - SHELLHP COMPRESSOR 1ST STAGE AFTERCOOLER - SHELL

CONTINGENCY

HP COMPRESSOR 1ST STAGE AFTERCOOLER - NORTH WESTHP COMPRESSOR 2ND STAGE AFTERCOOLER - NORTH WEST

SUBTOTAL NORTH WEST

CONTINGENCYTOTAL COMMON DELIVERY POINT



TOTAL SHELL

HP COMPRESSOR 2ND STAGE AFTERCOOLER - SHELL


CONTINGENCY



Rev.: A Page 2 of 5

Sm3/hr Sm3/hr

PK-02 27.60 33.12 27.608000.00 9600.00 8000.00

8027.60 9633.12 8027.60

PK-04 62.20 74.64 62.2018210.00 21852.00 18210.00

18272.20 21926.64 18272.20

26299.80 0.00


SUBTOTAL SHELL


NORMAL DESIGN (1)

Sm3/hr Sm3/hr


31559.7626299.80TOTAL

REMARKS

017798-49-03-UB-001





017798






Rev.: A Page 3 of 5



77.5 101611

X-002 176.4 231280

176.4 231280

0.00 0.00 0.00 0.00 0.00 0.00 253.90 332891NOTES:

NORMAL



017798

REMARKSEMERGENCY


STARTUPTAG NUMBER EQUIPMENT DESCRIPTION




TOTAL

SHUTDOWN

SUBTOTAL SHELL



Rev.: A Page 4 of 5



E-002 77.5 101611

77.5 101611

E-004 176.4 231280

176.4 231280

0.00 0.00 0.00 0.00 0.00 0.00 253.90 332891NOTES:

017798-49-03-UB-001

REMARKS

NORMAL

017798









SUBTOTAL SHELL

TOTAL



Rev.: A Page 5 of 5



3.66 3.70

3.66 3.70

8.24 8.34

8.24 8.34

0.00 0.00 0.00 0.00 0.00 0.00 11.90 12NOTES:

TOTAL

SUBTOTAL SHELL

CO2 CAPTURE - SHELL








017798017798-49-03-UB-001

Project No.:


Dec. 2007 RT SA DM

Rev.: A Page 1 of 5


kW kW kW kW V kW kWP-001 809 1011 809EA-001 42 52 42

47 59 47

897 1122 89715% 168 168

1290 1066

P-002 2211 2764 2211EA-005 28 35 28EA-005 25 31 25

836 1046 836

3100 3875 310015% 581 581

4456 3681


16855 21068 1685515% 3160 3160

24229 20015

27 34 2719 24 1914 18 1417 21 1741 51 4128 35 2888 110 88

234 292 23415% 44 44

336 278

26358 21086

15% 3954 395430315 25040


LP COMPRESSOR 2ND STAGE AFTERCOOLER - COMMON DEL. PT.HP COMPRESSOR 1ST STAGE AFTERCOOLER - COMMON DEL. PT.HP COMPRESSOR 2ND STAGE AFTERCOOLER - COMMON DEL PT.HP COMPRESSOR 3RD STAGE AFTERCOOLER - COMMON DEL PT.


CONTINGENCY

RICH AMINE PUMP - SHELL

SUBTOTAL SHELL

HP COMPRESSOR 3RD STAGE AFTERCOOLER - NORTH WEST

SUBTOTAL NORTH WEST



TOTAL SHELL

TOTAL PETROCANADA


CONDENSER - COMMON DELIVERY POINT

SUBTOTAL NORTH COMMON DELIVERY POINT


CO2 DEHYDRATION PACKAGE - COMMON DELIVERY POINT

CONTINGENCY

HP COMPRESSOR 1ST STAGE AFTERCOOLER - NORTH WESTHP COMPRESSOR 2ND STAGE AFTERCOOLER - NORTH WEST

LEAN AMINE COOLER - PETROCANADA

CONTINGENCYTOTAL NORTH COMMON DELIVERY POINT

RICH AMINE PUMP - PETROCANADA



LP COMPRESSOR 1ST STAGE AFTERCOOLER - COMMON DEL. PT.

CONTINGENCY

017798

DESIGNNORMAL

EQUIPMENT DESCRIPTION REMARKSINTERMITTENT

TAG NUMBERVOLTAGE CONTINUOUS



017798-49-04-UB-001


TOTAL NORTH WEST

TOTALCONTINGENCY




Rev.: A Page 2 of 5

Sm3/hr Sm3/hr

PK-02 28.00 33.60 28.0026235.00 31482.00 26235.00

26263.00 31515.60 26263.00

26263.00 0.00


017798




REMARKS

017798-49-04-UB-001


CO2 DEHYDRATION PACKAGE - COMMON DEL. PT.BOILER PACKAGE - COMMON DELIVERY POINT

TOTAL 26263.00 31515.60

NORMAL DESIGN (1)

Sm3/hr Sm3/hr

SUBTOTAL COMMON DELIVERY POINT



Rev.: A Page 3 of 5



254.0 333022

0.00 0.00 0.00 0.00 0.00 0.00 254.00 333022NOTES:

SHUTDOWN

TOTAL


CO2 STEAM TURBINE DRIVER - COMMON DEL. PT.


REMARKSEMERGENCY


STARTUP



017798

NORMAL



Rev.: A Page 4 of 5



E-002 254.0 333022

254.0 333022

0.00 0.00 0.00 0.00 0.00 0.00 254.00 333022NOTES:

TOTAL

REGENERATION TOWER REBOILER - COMMON DEL.







017798-49-04-UB-001

REMARKS

NORMAL

017798



Rev.: A Page 5 of 5



3.66 3.70

3.66 3.70

8.24 8.34

8.24 8.34

0.00 0.00 0.00 0.00 0.00 0.00 11.90 12NOTES:



017798017798-49-04-UB-001






CO2 CAPTURE - SHELL

SUBTOTAL SHELL

TOTAL

Absorber Lean-Rich Exch OH Drum Flash Drum Regenerator Regen ReboilerT-001 E-001 (2 x 2) V-001 T-002 E-002

3.0 m Dia 32.25 MW 4.3 m Dia 4.3 m Dia 42.75 MW

Lean Amine PumpsP-001 A/B

849 M3/Hr, 250 m Head

Solvent MU PumpsLean Amine Cooler Regen O/H Cond

EA-001 EA-00232.25 MW 2.25MW

Solvent Tank

LP Comp LP Comp HP Comp HP Comp HP Comp 1st Aftercooler 2nd Aftercooler 1st Aftercooler 2nd Aftercooler 3rd Aftercooler

EA-003A EA-003B EA-004A EA-004B EA-004C

4.83 MW 3.48 MW 3.20 MW 3.20 MW 6.20 MW

LP 1st Inlet LP 2nd Inlet LP 2nd Outlet HP 1st OutletSeparator Separator Separator Separator

3.05 m Dia 2.29 m Dia 1.68 m Dia 1.37 m Dia

COMPRESSION PACKAGEPK-001

PK-002

PTAC CO2 ENHANCED HYDROCARBON RECOVERY STUDY PLOT PLAN STUDY - PETROCANADA SITE

T-001 T-002V-001

DEHYDRATION PACKAGE

BFW TANK

TREATEDWATERTANK

DEAREATOR

AUXILIARYBOILER

PACKAGE

TREATEDWATER

PACKAGE

DEMINERALIZEDWATER

PACKAGE

CO2 CAPTURE AREA32m x 27m

CO2 COMPRESSION AND DEHYDRATION AREA

40m x 40m UTILITY AREA

35m x 40m

K-001 A / BLP Compressors

X-001Steam Turbine

V002A

V002B

V002C

K-002 A / B / CHP Compressors

V003


Absorber Lean-Rich Exch OH Drum Flash Drum Regenerator Regen ReboilerT-003A E-003 (4 x 4) V-004 T-004 E-004

3.8 m Dia 72.70 MW 6.5 m Dia 6.5 m Dia 96.38 MW

Lean Amine PumpsP-002 A/B

1914 M3/Hr, 250 m Head

Lean Amine Cooler Lean Amine Cooler Regen O/H CondEA-005A EA-005B EA-006

48.40 MW 35.5 MW 5.08 MW

Solvent MU Pumps

AbsorberT-003A Solvent Tank

3.2 m Dia



10.8 MW 7.7 MW 4.04 MW 7.60 MW 7.04 MW




PK-004

PTAC CO2 ENHANCED HYDROCARBON RECOVERY STUDY PLOT PLAN STUDY - SHELL SITE

T-003A T-004V-004

DEHYDRATION PACKAGE

BFW TANK

TREATEDWATERTANK

DEAREATOR

AUXILIARYBOILER

PACKAGE

TREATEDWATER

PACKAGE

DEMINERALIZEDWATER

PACKAGE

CO2 CAPTURE AREA

CO2 COMPRESSION AND DEHYDRATION AREA

UTILITY AREA


X-002Steam Turbine

V005A

V005B

V005C


V006

T-003B




4.1 MW 5.8 MW 3.2 MW 5.4 MW 6.2 MW




PTAC CO2 ENHANCED HYDROCARBON RECOVERY STUDY PLOT PLAN STUDY - NWU SITE


KM-005Motor

V007A

V007B

V007C


V008

CO2 COMPRESSION AREA


appendix 4 technical design parameters and drawings · document no. ptac co2 enhanced hydrocarbon...

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