MULTI-STAGE CO2 REMOVAL SYSTEM AND METHOD FOR PROCESSING A FLUE GAS STREAM

• US 20090101012A1
• Filed: 10/21/2008
• Published: 04/23/2009
• Est. Priority Date: 10/22/2007
• Status: Active Grant

• Current Assignee: General Electric Technology GmbH (GE Vernova, Inc.)
• Original Assignee: Alstom Technology Ltd. (Alstom SA)
• Inventors: Dopatka, Jurgen, Kozak, Frederic Z., Gal, Eli, Laslo, Dennis J., Muraskin, David J., Bade, Otto M.
• Granted Patent: US 8,182,577 B2
• Time in Patent Office: Days
• US Class Current: 95/225
• CPC Class Codes: B01D 2257/504 Carbon dioxide
• CPC Class Codes: B01D 53/1406 Multiple stage absorption
• CPC Class Codes: B01D 53/1475 Removing carbon dioxide
• CPC Class Codes: B01D 53/50 Sulfur oxides B01D53/60 takes precedence
• CPC Class Codes: B01D 53/62 Carbon oxides
• CPC Class Codes: B01D 53/78 with gas-liquid contact
• 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

An ammonia based CO2 capture system and method is provided in which multiple absorption stages are provided. Each absorption stage delivers an ionic solution at a predetermined temperature and contacts it with a flue gas stream.

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;

the absorber vessel comprises;

a first absorption stage;

a second absorption stage; and

a third absorption stage.

2. The system of claim 1 wherein the first absorption stage comprises:

Gas-liquid contact mass transfer device;

liquid distribution device; and

solution delivery path for delivering a supply of ionic solution to the liquid distribution device.

3. The system of claim 2 wherein the second absorption stage comprises:

Gas-liquid contact mass transfer device;

liquid distribution device; and

solution delivery path for delivering a supply of ionic solution to the liquid distribution device.

4. The system of claim 1 wherein the third absorption stage comprises:

Gas-liquid contact mass transfer device;

liquid distribution device; and

solution delivery path for delivering a supply of ionic solution to the liquid distribution device.

5. The system of claim 2 wherein the 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.

6. The system of claim 5 wherein the temperature of the ionic solution delivered to the liquid distribution device is controlled to be between 10°

C. and 20°

C.

7. The system of claim 3 wherein the 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.

8. The system of claim 7 wherein the temperature of the ionic solution delivered to the liquid distribution device of the second absorption stage is controlled to be between 10°

C. and 20°

C.

9. The system of claim 4 wherein the 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 first absorption stage.

10. The system of claim 5 wherein the temperature of the ionic solution delivered to the liquid distribution device of the third absorption stage is controlled to be between 0°

C. and 10°

C.

11. The system of claim 5 wherein the NH3-to-CO2 mole ratio (R) of the ionic solution is in the range from 1.4 to 1.8.

12. The system of claim 11 wherein the ionic solution contains solids of ammonium bicarbonate.

13. The system of claim 7 wherein the NH3-to-CO2 mole ratio (R) of the ionic solution is in the range from 1.8 to 2.0.

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

a first absorber vessel configured to receive a flue gas stream;

the first absorber vessel comprises a first absorption stage;

a second absorber vessel configured to receive a flue gas stream from the first absorber vessel;

the second absorber vessel comprises a second absorption stage;

a third absorber vessel configured to receive a flue gas stream from the second absorber vessel; and

the third absorber vessel comprises a third absorption stage.

15. The system of claim 14 wherein the first absorption stage comprises:

Gas-liquid contact mass transfer device;

liquid distribution device; and

solution delivery path for delivering a supply of ionic solution to the liquid distribution device.

16. The system of claim 15 wherein the second absorption stage comprises:

Gas-liquid contact mass transfer device;

liquid distribution device; and

solution delivery path for delivering a supply of ionic solution to the liquid distribution device.

17. The system of claim 14 wherein the third absorption stage comprises:

Gas-liquid contact mass transfer device;

liquid distribution device; and

solution delivery path for delivering a supply of ionic solution to the liquid distribution device.

18. The system of claim 15 wherein the 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.

19. The system of claim 18 wherein the temperature of the ionic solution delivered to the liquid distribution device is controlled to be between 10°

C. and 20°

C.

20. The system of claim 16 wherein the 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.

21. The system of claim 20 wherein the temperature of the ionic solution delivered to the liquid distribution device of the second absorption stage is controlled to be between 10°

C. and 20°

C.

22. The system of claim 17 wherein the 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 first absorption stage.

23. The system of claim 18 wherein the temperature of the ionic solution delivered to the liquid distribution device of the third absorption stage is controlled to be between 0°

C. and 10°

C.

24. The system of claim 18 wherein the NH3-to-CO2 mole ratio (R) of the ionic solution is in the range from 1.4 to 1.8.

25. The system of claim 24 wherein the ionic solution contains solids of ammonium bicarbonate.

26. The system of claim 20 wherein the NH3-to-CO2 mole ratio (R) of the ionic solution is in the range from 1.8 to 2.0.

27. A method of removing CO2 from a flue gas stream containing carbon dioxide, the method comprising the steps of:

contacting a first ionic solution flow with a flue gas stream to remove a first portion of CO2 from the flue gas stream;

contacting a second ionic solution flow with the flue gas stream to remove a second portion of CO2 from the flue gas stream;

contacting a third ionic solution flow with a flue gas stream to remove a third portion of CO2 from the flue gas stream; and

cooling the third ionic solution flow so as to minimize ammonia slip from the ionic solution.

28. The method of claim 27 wherein the first ionic solution flow is controlled to be within a temperature range of 10°

C.-20°

C.

29. The method of claim 27 wherein the second ionic solution flow is controlled to be within a temperature range of 0°

C.-10°

C.

30. The method of claim 27 wherein the third ionic solution flow is controlled to be within a temperature range of 0°

C.-10°

C.

31. The method of claim 27 wherein the first ionic solution flow is controlled to have an ammonia-to-CO2 mole ratio (R) in the range of 1.4-1.8.

32. The method of claim 27 wherein the second ionic solution flow is controlled to have an ammonia-to-CO2 mole ratio (R) in the range of 1.8-2.0.

33. The method of claim 27 wherein the third ionic solution flow is controlled to have an ammonia-to-CO2 mole ratio (R) in the range of 1.8-2.0.