PROCESS FOR THE REMOVAL OF CARBON DIOXIDE FROM GAS STREAMS

• US 20100126347A1
• Filed: 05/16/2008
• Published: 05/27/2010
• Est. Priority Date: 05/16/2007
• Status: Abandoned Application

• Current Assignee: Hydrogen Energy International Ltd. (BP PLC)
• Original Assignee: Hydrogen Energy International Ltd. (BP PLC)
• Inventors: Maunder, Anthony Dwight, Skinner, Geoffrey Frederick
• Application Number:
  US12/451,421
• Publication Number:
  US 20100126347A1
• Time in Patent Office: Days
• US Class Current: 95/174
• CPC Class Codes: C10L 3/10 Working-up natural gas or synthetic natural gas
• CPC Class Codes: C10L 3/102 of acid contaminants
• CPC Class Codes: Y02C 20/40 of CO2

Abstract

A process for the removal and recovery of carbon dioxide from a gaseous stream, in particular the removal and recovery of carbon dioxide, and optionally hydrogen sulphide, from a natural and/or synthesis gas stream. Furthermore, the present invention provides for the release of the removed and recovered carbon dioxide, and optionally hydrogen sulphide, at an elevated pressure, thereby reducing the high carbon dioxide compression costs associated with further chemical processing e.g. for under-ground carbon sequestration and/or for subsurface enhanced hydrocarbon recovery and/or for the manufacture of urea.

Claims

1-16. -16. (canceled)

17. A method of removing and recovering carbon dioxide from a gaseous stream characterized by the following consecutive steps:

(i) providing the gaseous feed stream at a temperature of between 20 to −

100°

C. and at a pressure of between 10 to 150 bar; and

(ii) contacting said gaseous stream with a methanol stream that is at a temperature of between 20 to −

100°

C. to produce at least two streams, one being a purified gaseous stream, having less than 5 mol % carbon dioxide, and one being a methanol stream rich in carbon dioxide; and

(iii) treating said methanol steam rich in carbon dioxide at a pressure of from 5 to 100 bar and at a temperature in the range 100 to 220°

C. in a solvent regeneration unit, to separate and recover respectively a carbon dioxide stream and a liquid methanol stream, at high pressure; and

(iv) recovering the purified gaseous stream comprising less than 5 mol % of carbon dioxide from step (ii) at high pressure.

18. A method according to claim 17, wherein the gaseous stream is any of the following natural gas, synthesis gas and synthesis gas containing hydrogen sulphide;

and any combinations thereof.

19. A method according to claim 17, wherein the gaseous feed steam comprises between 5 and 50 mol % of carbon dioxide.

20. A method according to claim 17, wherein the gaseous feed stream is provided at a temperature of less than −

10°

C. and preferably at a temperature of less than −

20°

C.; and

at a temperature of more than −

70°

C. and preferably at a temperature more than −

50°

C.

21. A method according to claim 17, wherein the gaseous feed stream is provided at a pressure of between 20 to 80 bar.

22. A method according to claim 17, wherein the temperature of the methanol introduced into the carbon dioxide absorption unit is less than −

10°

C. and preferably less than −

20°

C.; and

more than −

70°

C. and preferably more than −

50°

C.

23. A method according to claim 17, wherein the pressure of the methanol introduced into the carbon dioxide absorption unit is between 10 to 150 bar and is preferably at a pressure of between 20 to 80 bar.

24. A method according to claim 17, wherein the temperature of the gaseous feed stream is always higher than the temperature of the methanol introduced into the carbon dioxide absorption unit, preferably the temperature of the gaseous feed stream is 10°

C., more preferably 15°

C., higher than the temperature of the methanol introduced into the carbon dioxide absorption unit.

25. A method according to claim 17, wherein the purified gaseous stream exiting the carbon dioxide absorption unit comprises less thin 2 mol % and most preferably less than 0.5 mol % of carbon dioxide.

26. A method according to claim 17, wherein the separated carbon dioxide gaseous stream (from step (iii) of claim 17), is subjected to one of more cooling stages in order to condense the methanol and to yield a purified carbon dioxide stream, which is at a high pressure e.g. 5 to 100 bar.

27. A method according to claim 17, wherein the high pressure carbon dioxide stream is used for carbon dioxide sequestration and/or for subsurface enhanced hydrocarbon recovery and/or for chemical processing e.g. for the manufacture of urea.

28. A method according to claim 17, wherein the process is used for the combined recovery of carbon dioxide and hydrogen sulphide e.g. for use on a coal gasification plant.

29. A method according to claim 17, wherein the liquid regenerated methanol stream (from step (iii) of claim 17), is recycled to form the methanol, stream (of step (ii) of claim 17) used in the carbon dioxide absorption unit.

30. A method according to claim 17, wherein the pressure of the methanol stream rich in carbon dioxide of step (ii) of claim 17 is increased by at least 1 bar, preferably by at least 2 bars prior to being introduced into the solvent regeneration unit of step (iii) of claim 17.