Method for removing heat stable base salts from a contaminated basic solution, and use thereof in a process for recovering acid gas from an acid gas stream

• US 10,232,314 B2
• Filed: 01/22/2018
• Issued: 03/19/2019
• Est. Priority Date: 01/24/2011
• Status: Active Grant

• Current Assignee: Electrosep Technologies Inc.
• Original Assignee: Electrosep Technologies Inc.
• Inventors: Parisi, Paul
• Primary Examiner(s): Nassiri-Motlagh, Anita
• Application Number:
  US15/876,755
• Publication Number:
  US 20180141002A1
• Time in Patent Office: 421 Days
• Field of Search: None
• CPC Class Codes: B01D 2252/103 Water
• CPC Class Codes: B01D 2252/204 Amines
• 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 53/62 Carbon oxides
• CPC Class Codes: B01D 53/96 Regeneration, reactivation or recycling of reactants

Abstract

A method for removing heat stable base salts, such as amine salts, is disclosed. The method of the present invention can be used to reduce the level of heat stable salts in a solvent gas stream in an acid gas removal process. A solvent in which the lean acid gas loading is high is first stripped to achieve an acceptable lean gas loading. The lean solution is then reclaimed using one or more methods. The purified base or amine solution can be used again to remove acid gases from a gas stream. A process for recovering acid gas from an acid gas stream is also disclosed. The process also comprises a reduction of the level of heat stable salts in the solvent gas stream.

Claims

1. A method of enhancing operation of a reclamation unit comprising an electrodialysis unit or an ion exchange unit and receiving a regenerated slipstream withdrawn from a regenerated amine solution produced by a regenerator that is part of a CO₂ absorption system comprising an absorber that receives CO₂ containing gas and a lean amine solution and produces a CO₂ depleted gas and a loaded amine solution, the loaded amine solution being supplied to the regenerator which produces a CO₂ gas stream and the regenerated amine solution, the regenerated slipstream being fed into a reclamation unit to remove heat-stable salts therefrom and produce a reclaimed stream that is fed back along with the regenerated amine solution to form at least part of the lean amine solution supplied to the absorber, the method comprising operating a supplementary regenerator to receive the regenerated slipstream prior to the reclamation unit to remove further CO₂ therefrom prior the reclamation unit.

2. The method of claim 1, wherein the lean amine solution comprises monoethanolamine, methyldiethanolamine, diethanolamine, aminoethoxyethanol, diisopropyl amine or a mixture thereof.

3. The method of claim 1, wherein the regenerator is a stripping column.

4. The method of claim 1, wherein the reclamation unit is an electrodialysis unit.

5. The method of claim 1, wherein the reclamation unit is an ion exchange unit.

6. The method of claim 1, wherein the regenerated slipstream fed into the supplementary regenerator has a CO₂ loading greater than 10,000 ppm.

7. The method of claim 6, wherein the supplementary regenerator is operated such that the CO₂ loading of the regenerated slipstream withdrawn therefrom and fed into the reclamation unit is lower than 1,000 ppm.

8. The method of claim 1, wherein the regenerated slipstream fed into the supplementary regenerator has a CO₂ loading greater than 1,000 ppm, and the supplementary regenerator is operated such that the CO₂ loading of the regenerated slipstream withdrawn therefrom and fed into the reclamation unit is lower than 1,000 ppm.

9. The method of claim 1, wherein the regenerated slipstream is fed directly from the regenerated amine solution into the supplementary regenerator.

10. The method of claim 1, wherein the regenerated slipstream withdrawn from the supplementary regenerator is fed directly into the reclamation unit.

21. The method of claim 1, wherein the supplementary regenerator operates by stripping.

22. The method of claim 1, wherein the supplementary regenerator is a stripping column.

11. A method of enhancing heat-stable salt removal from a contaminated stream subjected to electrodialysis or ion exchange, the contaminated stream being derived from a regenerated slipstream withdrawn from a regenerated solution produced by a regenerator that is part of an acid gas absorption system comprising an absorber that receives a gas stream containing the acid gas and a lean solution and produces an acid gas depleted stream and a loaded solution, the loaded solution being supplied to the regenerator which produces an acid gas stream and the regenerated solution, the regenerated slipstream being subjected to the heat-stable salt removal to produce a reclaimed stream, the method comprising providing a supplementary regenerator configured to receive the regenerated slipstream prior to heat-stable salt removal to remove further acid gas therefrom prior the prior to subjecting the contaminated stream to the electrodialysis or the ion exchange.

12. The method of claim 11, wherein the lean solution of the acid gas absorption system comprises amides.

13. The method of claim 11, wherein the lean solution of the acid gas absorption system comprises an organic base or an inorganic base.

14. The method of claim 11, wherein the lean solution of the acid gas absorption system comprises amines.

15. The method of claim 11, wherein the acid gas comprises CO₂.

16. The method of claim 11, wherein the regenerated slipstream fed into the supplementary regenerator has an acid gas loading greater than 10,000 ppm.

17. The method of claim 16, wherein the supplementary regenerator is operated such that the acid gas loading of the regenerated slipstream withdrawn therefrom and subjected to the heat-stable salt removal by electrodialysis or ion exchange is lower than 1,000 ppm.

18. The method of claim 11, wherein the regenerated slipstream fed into the supplementary regenerator has an acid gas loading greater than 1,000 ppm, and the supplementary regenerator is operated such that the CO₂ loading of the regenerated slipstream withdrawn therefrom and subjected to the heat-stable salt removal by electrodialysis or ion exchange is lower than 1,000 ppm.

19. The method of claim 15, wherein the regenerator and the supplemental regenerator are operated at temperatures of 75°

C. to 150°

C., and the absorber is operated at a temperature of 20°

C. to 60°

C.

23. The method of claim 19, wherein the supplementary regenerator is a stripping column.

20. A method of enhancing operation of a reclamation unit comprising an electrodialysis unit or an ion exchange unit and receiving a regenerated slipstream withdrawn from a regenerated solution produced by a regenerator that is part of an acid gas absorption system comprising an absorber that receives a gas containing the acid gas and a lean solution and produces an acid gas depleted stream and a loaded solution, the loaded solution being supplied to the regenerator which produces an acid gas stream and the regenerated solution, the regenerated slipstream being fed into the reclamation unit to remove heat-stable salts therefrom and produce a reclaimed stream, the method comprising adding a supplementary regenerator in between the regenerator and the reclamation unit in order to receive the regenerated slipstream prior to the reclamation unit to remove further acid gas therefrom prior to the reclamation unit.

24. The method of claim 20, wherein the supplementary regenerator is a stripping column.