SINGLE ABSORBER VESSEL TO CAPTURE CO2

• US 20110120308A1
• Filed: 11/20/2009
• Published: 05/26/2011
• Est. Priority Date: 11/20/2009
• Status: Active Grant

• Current Assignee: General Electric Technology GmbH (GE Vernova, Inc.)
• Original Assignee: Alstom Technology Ltd. (Alstom SA)
• Inventors: Hiwale, Rameshawar S., Koss, Peter U., Dube, Sanjay K., Muraskin, David J.
• Granted Patent: US 8,784,761 B2
• Time in Patent Office: Days
• US Class Current: 95/199
• CPC Class Codes: B01D 2252/102 Ammonia
• CPC Class Codes: B01D 2257/504 Carbon dioxide
• CPC Class Codes: B01D 2258/0291 from waste incineration plants
• CPC Class Codes: B01D 53/1406 Multiple stage absorption
• CPC Class Codes: B01D 53/1425 Regeneration of liquid absorbents
• CPC Class Codes: B01D 53/1475 Removing carbon dioxide
• CPC Class Codes: B01D 53/62 Carbon oxides
• CPC Class Codes: Y02A 50/20 Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
• CPC Class Codes: Y02C 20/40 of CO2

Abstract

A system for removing carbon dioxide from a flue gas stream is provided, the system comprising an absorber vessel configured to receive a flue gas stream, the absorber vessel comprising a first absorption stage configured to receive the flue gas stream and contact it with a first ionic solution, a second absorption stage configured to receive flue gas which has passed the first absorption stage and contact it with a second ionic solution, a first sump vessel, and a second sump vessel. Furthermore, a method for removing CO₂ from a flue gas stream containing CO₂ is provided, the method comprising the steps of a) contacting a flow of a first ionic solution comprising NH₃ with a flue gas stream to remove a first portion of CO₂ from the flue gas stream, b) collecting the used ionic solution from step a) in a first sump vessel, c) recycling ionic solution from the first sump vessel to step a), d) contacting a flow of a second ionic solution comprising NH₃ with the flue gas stream to remove a second portion of CO₂ from the flue gas stream, e) collecting the used ionic solution from step d) in a second sump vessel, and f) recycling ionic solution from the second sump vessel to step d).

Claims

1. A system for removing carbon dioxide from a flue gas stream, the system comprising:

an absorber vessel configured to receive a flue gas stream,

said absorber vessel comprising

a first absorption stage configured to receive the flue gas stream and contact it with a first ionic solution,

a second absorption stage configured to receive flue gas which has passed the first absorption stage and contact it with a second ionic solution,

a first sump vessel, and a

second sump vessel,

wherein said first absorption stage comprises a liquid collection receptacle arranged to collect ionic solution from the first absorption stage and deliver it to the first sump vessel, and said second absorption stage comprises a liquid collection receptacle arranged to collect ionic solution from the second absorption stage and deliver it to the second sump vessel.

2. The system according to claim 1, wherein said absorber vessel comprises a bottom section, in which a first and a second sump vessel is formed by two sub-sections of said bottom section.

3. The system according to claim 1, further comprising a control system configured to maintain the NH₃-to-CO₂ mole ratio (R) of the ionic solution in the first sump vessel in a range of 1.2 to 2.0.

4. The system according to claim 3, further comprising a control system configured to maintain the NH₃-to-CO₂ mole ratio (R) of the ionic solution in the second sump vessel in a range of 2.0 to 4.0.

5. The system according to claim 3, wherein said control system comprises a device configured to introduce NH₃ or a medium having a NH₃-to-CO₂ mole ratio (R) higher than the R of the ionic solution in the sump vessel into the ionic solution.

6. The system according to claim 1, wherein the first absorption stage further comprises

a liquid distribution device and

an ionic solution delivery path configured for delivering ionic solution from the first sump vessel to said liquid distribution device.

7. The system according to claim 1, wherein the second absorption stage further comprises

a liquid distribution device and

an ionic solution delivery path configured for delivering ionic solution from the second sump vessel to said liquid distribution device.

8. The system according to claim 6, wherein the ionic solution delivery path of the first absorption stage comprises a heat exchange device for controlling the temperature of the ionic solution delivered to the liquid distribution device of the first absorption stage.

9. The system according to claim 8, wherein the temperature of the ionic solution delivered to the liquid distribution device is controlled to be in the range of 5 to 20°

C.

10. The system according to claim 7, wherein the ionic solution delivery path of the second absorption stage comprises a heat exchange device for controlling the temperature of the ionic solution delivered to the liquid distribution device of the second absorption stage.

11. The system according to claim 10, wherein the temperature of the ionic solution delivered to the liquid distribution device is controlled to be in the range of 5 to 20°

C.

12. The system according to claim 1, wherein the first absorption stage is configured for operating with an ionic solution containing solid particles.

13. The system according to claim 1, wherein said absorber vessel further comprises a third absorption stage configured to receive flue gas which has passed the first and the second absorption stages and contact it with an ionic solution.

14. The system according to claim 13, wherein said third absorption stage comprises a liquid collection receptacle arranged to collect ionic solution from the third absorption stage and deliver it to the first sump vessel.

15. The system according to claim 13, wherein the third absorption stage comprises

a liquid distribution device, and

an ionic solution delivery path configured for delivering ionic solution from the first sump vessel to said liquid distribution device.

16. The system according to claim 15, wherein the ionic solution delivery path of the third absorption stage comprises a heat exchange device for controlling the temperature of the ionic solution delivered to the liquid distribution device of the third absorption stage.

17. The system according to claim 16, wherein the temperature of the ionic solution delivered to the liquid distribution device is controlled to be in the range of 10°

C. or lower.

18. The system according to claim 13, wherein the third absorption stage is configured for operating with an ionic solution containing solid particles.

19. Method for removing CO₂ from a flue gas stream containing CO₂, the method comprising the steps of:

a) contacting a flow of a first ionic solution comprising NH₃ with a flue gas stream to remove a first portion of CO₂ from the flue gas stream,

b) collecting the used ionic solution from step a) in a first sump vessel,

c) recycling ionic solution from said first sump vessel to step a),

d) contacting a flow of a second ionic solution comprising NH₃ with the flue gas stream to remove a second portion of CO₂ from the flue gas stream,

e) collecting the used ionic solution from step d) in a second sump vessel, and

f) recycling ionic solution from said second sump vessel to step d).

20. The method according to claim 19, wherein step a) is performed under conditions such that solid ammonium bicarbonate is formed.

21. The method according to claim 19, wherein said first ionic solution has a NH₃-to-CO₂ mole ratio (R) in the range of 1.2 to 2.0.

22. The method according to claim 19, further comprising the step of adjusting the NH₃-to-CO₂ mole ratio (R) of the ionic solution in the first sump vessel to be in the range of 1.2 to 2.0.

23. The method according to claim 22, wherein the adjustment of the NH₃-to-CO₂ mole ratio (R) is achieved by introducing NH₃ and/or a medium having a NH₃-to-CO₂ mole ratio (R) higher than the R of the ionic solution in the first sump vessel into the second sump vessel.

24. The method according to claim 23, wherein said medium is ionic solution from the second sump vessel.

25. The method according to claim 19, wherein step d) is performed under conditions such that essentially no solid ammonium bicarbonate is formed.

26. The method according to claim 19, wherein said second ionic solution has a NH₃-to-CO₂ mole ratio (R) in the range of 2.0 to 4.0.

27. The method according to claim 19, further comprising the step of adjusting the NH₃-to-CO₂ mole ratio (R) of the ionic solution in the second sump vessel to be in the range of 2.0 to 4.0.

28. The method according to claim 27, wherein the adjustment of the NH₃-to-CO₂ mole ratio (R) is achieved by introducing NH₃ and/or a medium having a NH₃-to-CO₂ mole ratio (R) higher than the R of the ionic solution in the second sump vessel into the second sump vessel.

29. The method according to claim 19, wherein the temperature of the first ionic solution in step a) is controlled to be in the range of 5 to 20°

C.

30. The method according to claim 19, wherein the temperature of the second ionic solution in step d) is controlled to be in the range of 5 to 20°

C.

31. The method according to claim 19, further comprising the step of contacting a flow of a third ionic solution comprising NH₃ and having a NH₃-to-CO₂ mole ratio (R) in the range of 1.2 to 2.0 with the flue gas stream to remove a third portion of CO₂ from the flue gas stream.

32. The method according to claim 31, wherein said flow of a third ionic solution is delivered from the first sump vessel.

33. The method according to claim 32, wherein said flow of a third ionic solution is delivered via a device configured to reduce the amount of solids in the ionic solution.

34. The method according to claim 31, wherein the temperature of the third ionic solution is controlled to be in the range of 10°

C. or lower.