System for removal of carbon dioxide from a process gas

• US 8,673,227 B2
• Filed: 10/08/2012
• Issued: 03/18/2014
• Est. Priority Date: 09/15/2009
• Status: Expired due to Fees

• Current Assignee: General Electric Technology GmbH (GE Aerospace)
• Original Assignee: Alstom Technology Ltd. (Alstom SA)
• Inventors: Black, Sean E., Dube, Sanjay K., Muraskin, David J., Kozak, Frederic Z.
• Primary Examiner(s): Warden, Jill
• Assistant Examiner(s): Woodard, Joye L
• Application Number:
  US13/647,046
• Publication Number:
  US 20130028807A1
• Time in Patent Office: 526 Days
• Field of Search: 422/168, 422/169, 422/170, 422/171, 422/235, 962/42
• US Class Current: 422/168
• 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 53/18 Absorbing units; Liquid distributors therefor B01D3/16, B01D3/26, B01D3/30 take precedence; packing elements B01J19/30, B01J19/32
• CPC Class Codes: B01D 53/62 Carbon oxides
• CPC Class Codes: Y02C 20/40 of CO2

Abstract

A system for removal of carbon dioxide from a process gas includes an absorption arrangement arranged to allow contact between the process gas and an ammoniated solution within the absorption arrangement such that at least a part of the carbon dioxide of the process gas is captured by the ammoniated solution. The absorption arrangement is arranged to, with regard to the ammoniated solution, only accommodate ammoniated solution without solids. A first heat exchanger is arranged to cool the ammoniated solution including captured carbon dioxide after it has exited the absorption arrangement. A separator is arranged to remove at least a part of any solids in the cooled ammoniated solution. A second heat exchanger is arranged to heat the ammoniated solution after it has exited the separator and returned to the absorption arrangement.

Claims

1. A system for removal of carbon dioxide from a process gas, the system comprising:

an absorption vessel that receives a process gas and an ammoniated solution for contacting the process gas and the ammoniated solution in the absorption vessel such that at least a part of the CO₂ of the process gas is captured by the ammoniated solution to provide a CO₂ lean process gas and an ammoniated solution rich in CO₂ without precipitation;

a first heat exchanger to cool the ammoniated solution rich in CO₂ including captured carbon dioxide after it has exited the absorption vessel to precipitate solids from the ammoniated solution rich in CO₂;

a separator to remove at least a part of any solids in the cooled ammoniated solution; and

a second heat exchanger to heat the ammoniated solution after it has exited the separator, wherein the heated ammoniated solution is returned to the lower portion of the absorption vessel.

2. The system according to claim 1, further comprising:

a pump for providing ammoniated solution to an upper portion of the absorption vessel; and

a third heat exchanger for cooling ammoniated solution pumped to the upper portion of the absorption vessel to a temperature between about 10°

C. and 20°

C.

3. The system according to claim 1, wherein the first heat exchanger cools the ammoniated solution to a temperature between about 0°

C. and 10°

C.

4. The system according to claim 1, wherein the first heat exchanger cools the ammoniated solution to a temperature between about 7°

C. and 15°

C.

5. The system according to claim 1, wherein the separator is a hydrocyclone.

6. The system according to claim 1, wherein the first and second heat exchangers are arranged to cooperate with each other such that the ammoniated solution being cooled in the first heat exchanger is at least partly cooled by the ammoniated solution being heated in the second heat exchanger as cooling medium, and the ammoniated solution being heated in the second heat exchanger is at least partly heated by the ammoniated solution being cooled in the first heat exchanger as heating medium.

7. The system of claim 1, further comprising a control system configured to control the NH₃-to-CO₂ mole ratio (R) of the ammoniated solution such that substantially no precipitation of solids occurs within the absorption vessel when the absorption vessel is in use.

8. The system according to claim 7, wherein the control system automatically controls the molar ratio (R).

9. The system according to claim 7, wherein the control system the molar ratio (R) in the absorption arrangement within a desired range.

10. The system according to claim 9, further comprising a sensor providing a signal indicative of the molar ratio within the absorption vessel, wherein the control system adjusts the molar ratio in response to the signal.

11. The system according to claim 10, further comprising actuating a fluid flow device that adjusts the flow of the ammoniated solution in response to the signal received from the sensor.

12. A system for removal of carbon dioxide from a process gas, the system comprising:

an absorption vessel that receives a process gas and an ammoniated solution for contacting the process gas and the ammoniated solution in the absorption vessel such that at least a part of the CO₂ of the process gas is captured by the ammoniated solution to provide a CO₂ lean process gas and an ammoniated solution rich in CO₂ without precipitation;

the absorption vessel includes;

a first absorption stage arranged to receive the process gas and contact it with a first part of the ammoniated solution;

a second absorption stage arranged to receive process gas which has passed the first absorption stage and contact it with a second part of the ammoniated solution;

a first sump vessel; and

a second sump vessel;

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

a first heat exchanger to cool the ammoniated solution rich in CO₂ including captured carbon dioxide after it has exited the absorption vessel to precipitate solids from the ammoniated solution rich in CO₂;

a separator to remove at least a part of any solids in the cooled ammoniated solution; and

a second heat exchanger to heat the ammoniated solution after it has exited the separator, wherein the heated ammoniated solution is returned to the absorption vessel.

13. The system of claim 12, further comprising a control system configured to maintain the NH₃-to-CO₂ mole ratio (R) of the ammoniated solution in the first sump vessel within a range of 1.8 to 2.5, and to maintain the temperature of the first sump vessel within a range of 10 to 25°

C.

14. The system of claim 12, further comprising a control system configured to maintain the NH₃-to-CO₂ mole ratio (R) of the ammoniated solution in the second sump vessel within a range of 2.0 to 4.5, and to maintain the temperature of the second sump vessel within a range of 10 to 25°

C.

15. The system according to claim 13, wherein said control system comprises a device configured to introduce NH₃ or a medium having an NH₃-to-CO₂ mole ratio (R) higher than the R of the ammoniated solution in one of the sump vessels into said sump vessel.