Configurations And Methods Of High Pressure Acid Gas Removal

• US 20110203314A1
• Filed: 09/30/2009
• Published: 08/25/2011
• Est. Priority Date: 10/02/2008
• Status: Active Grant

• Current Assignee: Fluor Technologies Corporation (Fluor Corporation)
• Original Assignee: Fluor Technologies Corporation (Fluor Corporation)
• Inventors: Mak, John
• Granted Patent: US 8,696,798 B2
• Time in Patent Office: Days
• US Class Current: 62/617
• CPC Class Codes: B01D 2257/504 Carbon dioxide
• CPC Class Codes: B01D 53/1425 Regeneration of liquid absorbents
• CPC Class Codes: B01D 53/1456 Removing acid components
• CPC Class Codes: B01D 53/1475 Removing carbon dioxide
• CPC Class Codes: B01D 53/77 Liquid phase processes
• CPC Class Codes: Y02C 20/40 of CO2

Abstract

Acid gas is removed from a feed gas using a physical solvent that is regenerated using successive flashing stages after heating of the rich solvent using low-level waste heat that is preferably produced or available within the acid gas removal plant. Especially preferred waste heat sources include compressor discharges of the refrigeration system and/or recompression system for CO2, and/or (low level) heat content from the feed gas.

Claims

1. A method of regenerating a CO2-rich physical solvent that is formed by absorption of CO2 from a gas having a CO2 content of at least 10 mol % and a pressure of at least 1000 psig, comprising a step of heating the CO2-rich solvent using heat from flash-regenerated lean solvent and heat recovered from at least one of a feed gas, and a compressor discharge.

2. The method of claim 1 wherein the heated CO2-rich solvent has a temperature that is sufficient to allow flashing of between 20% to 40% of CO2 in the CO2-rich solvent at a pressure between 300 and 500 psig and flashing of between 20% to 40% of CO2 in the CO2-rich solvent at a pressure between 50 and 300 psig.

3. The method of claim 1 wherein the heated CO2-rich solvent has a temperature that is sufficient to limit flashing of CO2 from the CO2-rich solvent at a pressure at or near atmospheric pressure to between 5% to 20% of CO2 in the CO2-rich solvent.

4. The method of claim 1 wherein the heated CO2-rich solvent has a temperature that is sufficient to allow flashing of between 20% to 40% of CO2 in the CO2-rich solvent at a pressure between 300 and 500 psig.

5. The method of claim 1 wherein at least 80% of CO2 is removed from the CO2-rich solvent by heating the CO2-rich solvent to a temperature of between 100°

F. to 300°

F. using waste heat, and wherein the heated CO2-rich solvent is flashed to produce at least two separate CO2 streams at a pressure of between 50 psig to 500 psig.

6. The method of claim 1 wherein the flash-regenerated lean solvent has a temperature of at least 60°

F.

7. The method of claim 1 wherein the flash-regenerated lean solvent is produced by flashing the CO2-rich solvent across at least two expansion devices.

8. The method of claim 7 wherein the flash-regenerated lean solvent is produced by flashing the CO2-rich solvent to a pressure below atmospheric pressure.

9. The method of claim 1 wherein the compressor discharge is a refrigeration compressor discharge or a CO2 compressor discharge.

10. A method of removing CO2 from a feed gas, comprising:

absorbing CO2 in an absorber from the feed gas using a lean physical solvent to produce a treated gas depleted in CO2 and a CO2-rich solvent;

heating the CO2-rich solvent in a plurality of heat exchangers using waste heat that is produced in the process of removing CO2 from the feed gas;

separating a first CO2-rich stream from the heated CO2-rich solvent at a pressure of at least 300 psig, and separating a second CO2-rich stream from the heated CO2-rich solvent at a pressure of at least 100 psig to so form a flashed solvent, wherein first and second CO2-rich streams comprise at least 70% of total CO2 of the CO2-rich solvent; and

cooling the flashed solvent using refrigeration generated by partial expansion of the CO2-rich solvent.

11. The method of claim 10 wherein the waste heat is produced by at least one of the flashed solvent, the feed gas, and a compressor discharge.

12. The method of claim 10 wherein CO2 is present in the feed gas at a concentration of at least 10 mol %, and wherein the CO2 is absorbed in the absorber at a pressure of at least 1000 psi.

13. The method of claim 10 wherein the feed gas is syngas.

14. The method of claim 10 wherein the first and second CO2-rich streams comprise at least 90% CO2.

15. An acid gas removal plant, comprising:

a source of a feed gas that is configured to provide a feed gas having a pressure of at least 1000 psi and a CO2 content of at least 10 mol %;

an absorber fluidly coupled to the source and configured to allow absorption of CO2 from the feed gas using a lean physical solvent to thereby produce a lean gas stream and a CO2-rich solvent;

a plurality of heat exchangers configured to heat the CO2-rich solvent using waste heat to thereby form a heated CO2-rich solvent;

a plurality of pressure reduction devices and flash vessels arranged such as to allow sequential flashing of the heated CO2-rich solvent such that a first CO2-rich stream is formed from heated the CO2-rich solvent at a pressure of at least 300 psig, and such that a second CO2-rich stream is formed from the heated CO2-rich solvent at a pressure of at least 100 psig;

wherein first and second CO2-rich streams comprise at least 70% of total CO2 of the CO2-rich solvent.

16. The acid gas removal plant of claim 15 wherein the plurality of heat exchangers are thermally coupled to at least one of a CO2-rich feed gas, the lean solvent, and a compressor discharge stream.

17. The acid gas removal plant of claim 15 wherein the source is a natural gas well or a syngas production plant.

18. The acid gas removal plant of claim 15 further comprising a compressor that is configured to compress the first and second CO2-rich streams to a pressure suitable for injection into a formation.

19. The acid gas removal plant of claim 15 further comprising an expansion turbine that is fluidly coupled to the absorber and upstream of the plurality of heat exchangers.

20. The acid gas removal plant of claim 15 wherein the plurality of heat exchangers allow heating of the CO2-rich solvent to a temperature of at least 200°

F.