Removal of Acid Gases From A Gas Stream

• US 20110168019A1
• Filed: 08/27/2009
• Published: 07/14/2011
• Est. Priority Date: 10/14/2008
• Status: Abandoned Application

• Current Assignee: Edward J. Grave, John T. Cullinane, Paul Scott Northrop
• Original Assignee: Edward J. Grave, John T. Cullinane, Paul Scott Northrop
• Inventors: Grave, Edward J., Cullinane, John T., Northrop, Paul Scott
• Application Number:
  US13/119,356
• Publication Number:
  US 20110168019A1
• Time in Patent Office: Days
• US Class Current: 95/186
• CPC Class Codes: B01D 2251/206 Ammonium compounds
• CPC Class Codes: B01D 2257/304 Hydrogen sulfide
• CPC Class Codes: B01D 2257/504 Carbon dioxide
• CPC Class Codes: B01D 53/1406 Multiple stage absorption
• CPC Class Codes: B01D 53/1468 Removing hydrogen sulfide
• CPC Class Codes: B01D 53/1475 Removing carbon dioxide
• CPC Class Codes: B01D 53/77 Liquid phase processes
• CPC Class Codes: Y02C 20/40 of CO2

Abstract

A gas processing facility for the separation of fluids is provided. The facility includes co-current contactors placed in series. Each co-current contactor receives a gas stream that includes a non-absorbing gas such as a hydrocarbon gas or nitrogen. The gas stream also includes an acid gas or other contaminant. Each co-current contactor also receives a liquid solvent stream. The co-current contactors then each release a sweetened gas stream and a gas-treating solution. In one processing direction, the contactors are arranged to deliver progressively sweetened gas streams. In the opposite processing direction, the contactors are arranged to deliver progressively richer gas-treating solutions. In one aspect, the facility includes at least a first co-current contactor, a second co-current contactor and a final co-current contactor. However, any number of at least two co-current separators may be employed. Methods and processes for separating a gas stream are also provided.

Claims

1. A gas processing facility for the separation of a fluid stream, the facility comprising:

a first co-current contactor configured to receive (i) an initial gas stream comprising a non-absorbing gas and an acid gas and (ii) a second liquid solvent, the first co-current contactor also being configured to release (iii) a first partially-sweetened gas stream and (iv) a first partially-loaded gas-treating solution; and

a final co-current contactor configured to receive (i) a previous partially-sweetened gas stream and (ii) a regenerated liquid solvent, and configured to release (iii) a final sweetened gas stream and (iv) a final lightly-loaded gas-treating solution, wherein the initial gas stream is at least one of;

a tail gas stream from a Claus sulfur recovery process,

an acid gas stream from a solvent regeneration process requiring H₂S enrichment,

a synthesis-gas stream,

an acid gas from a cement plant, and

a gas stream created internally within the gas processing facility.

2. The gas processing facility of claim 1, wherein the gas stream created internally within the gas processing facility is:

a flash gas stream from a flash drum, or

an impurities stream from a regenerator.

3. The gas processing facility of claim 1, wherein:

the acid gas received by the first co-current contactor comprises primarily carbon dioxide; and

the second liquid solvent and the regenerated liquid solvent are selected to preferentially remove carbon dioxide from a gas stream comprising hydrocarbons.

4. The gas processing facility of claim 1, wherein:

the acid gas received by the first co-current contactor comprises primarily hydrogen sulfide; and

the second liquid solvent and the regenerated liquid solvent are selected to preferentially remove hydrogen sulfide from a gas stream comprising hydrocarbons.

5. The gas processing facility of claim 1, further comprising:

a second co-current contactor configured to receive (i) the first partially-sweetened gas stream and (ii) a third liquid solvent, and is configured to release (iii) a second partially-sweetened gas stream and (iv) a second partially-loaded gas-treating solution; and

the regenerated liquid solvent is comprised at least in part of a regenerated solvent stream whereby an acid gas has been substantially removed from at least the first partially-loaded gas-treating solution.

6. The gas processing facility of claim 5, further comprising:

a flash drum for releasing hydrocarbon and H₂O vapors from the second partially-loaded gas-treating solution; and

a pump for increasing pressure of the second partially-loaded gas-treating solution before the second partially-loaded gas-treating solution enters the first co-current contactor.

7. The gas processing facility of claim 5, wherein:

the first co-current contactor, the second co-current contactor, the final co-current contactor, or combinations thereof, comprise a short-contact time mixing device having at least one of a centrifugal mixer, a static mixer, a mist eliminator, a venturi tube, an electrostatic precipitator, and an eductor.

8. The gas processing facility of claim 5, wherein:

the first co-current contactor and the second co-current contactor reside within a shell; and

the shell is refrigerated.

9. The gas processing facility of claim 5, wherein:

a jacket is placed around the first co-current contactor, the second co-current contactor, or both; and

a cooling medium is circulated within the jacket.

10. The gas processing facility of claim 5, further comprising:

a third co-current contactor configured to receive (i) the second partially-sweetened gas stream and (ii) a fourth liquid solvent, and configured to release (iii) a third partially-sweetened gas stream and (iv) a third partially-loaded gas-treating solution; and

wherein;

the third liquid solvent received by the second co-current contactor comprises the third partially-loaded gas-treating solution released by the third co-current contactor; and

the second partially-loaded gas-treating solution is heavily loaded with acid gases.

11. The gas processing facility of claim 5, wherein the regenerated liquid solvent received by the final co-current contactor comprises the regenerated first partially-loaded gas-treating solution.

12. The gas processing facility of claim 11, wherein the regenerated liquid solvent received by the final co-current contactor further comprises the second partially-loaded gas-treating solution such that the first and second partially-loaded gas-treating solutions are together regenerated to form the regenerated liquid solvent received by the final co-current contactor.

13. The gas processing facility of claim 5, wherein the second liquid solvent received by the first contactor at least partially comprises a regenerated solvent stream.

14. The gas processing facility of claim 5, further comprising:

a cooler for cooling the second partially-loaded gas-treating solution.

15. The gas processing facility of claim 5, wherein:

an operating temperature of the first co-current contactor is different than the operating temperatures of the second co-current contactor, the final co-current contactor, or both.

16. The gas processing facility of claim 1, wherein:

an inlet pressure of the fluid stream into the first co-current contactor is about 15 to 100 psig.

17. The gas processing facility of claim 1, wherein:

the second liquid solvent and the regenerated liquid solvent comprise amine.

18. The gas processing facility of claim 17, wherein:

the amine comprises a secondary amine, a primary amine, a tertiary amine, or combinations thereof.

19. The gas processing facility of claim 1, wherein the second liquid solvent and the regenerated liquid solvent comprise physical solvents or solvents comprising a mixture of physical and chemical solvents.

20. A method of separating an initial gas stream in a gas processing facility, the gas stream comprising a non-absorbing gas and an acid gas, and the method comprising:

providing at least a first co-current contactor, a second co-current contactor and a final co-current contactor, each of these co-current contactors being configured (i) to receive a gas stream and a liquid solvent, and (ii) to release a sweetened gas stream and a separate loaded gas-treating solution;

arranging the first co-current contactor, the second co-current contactor and the final co-current contactor to deliver the respective sweetened gas streams as progressively sweetened gas streams in series;

further arranging the final co-current contactor, the second co-current contactor and the first co-current contactor to deliver the respective gas-treating solutions as progressively richer gas-treating solutions in series;

delivering a regenerated liquid solvent to the final co-current contactor; and

operating the gas processing facility in order to remove acid gas from the initial gas stream and deliver a final sweetened gas stream.

21. The method of claim 20, wherein the non-absorbing gas comprises a hydrocarbon gas or nitrogen.

22. The method of claim 21, wherein:

the first co-current contactor receives (i) the initial gas stream and a (ii) second liquid solvent, and releases (iii) a first partially-sweetened gas stream and (iv) a first partially-loaded gas-treating solution;

the second co-current contactor receives (i) the first partially-sweetened gas stream from the first co-current contactor and (ii) a third liquid solvent, and releases (iii) a second partially-sweetened gas stream and (iv) a second partially-loaded gas-treating solution, and

the final co-current contactor receives (i) a previous partially-sweetened gas stream and (ii) a regenerated liquid solvent, and releases (iii) a final sweetened gas stream and (iv) a final lightly-loaded gas-treating solution.

23. The method of claim 20, wherein the initial gas stream is at least one of:

a tail gas stream from a Claus sulfur recovery process,

an acid gas stream from a solvent regeneration process requiring H₂S enrichment,

an acid gas from a cement plant, and

a gas stream created internally within the gas processing facility.

24. The method of claim 23, wherein the gas stream created internally within the gas processing facility is:

a flash gas stream from a flash drum, or

an impurities stream from a regenerator.

25. The method of claim 21, wherein:

the acid gas comprises primarily carbon dioxide; and

the second liquid solvent and the regenerated liquid solvent are selected to remove carbon dioxide from a gas stream comprising hydrocarbons.

26. The method of claim 21, wherein:

the acid gas comprises primarily hydrogen sulfide; and

the second liquid solvent and the regenerated liquid solvent are selected to remove hydrogen sulfide from a gas stream comprising hydrocarbons.

27. The method of claim 21, wherein:

the initial gas stream is a flue gas stream;

the non-absorbing gas comprises nitrogen;

the acid gas comprises primarily carbon dioxide; and

the second liquid solvent and the regenerated liquid solvent are selected to preferentially remove carbon dioxide.

28. The method of claim 22, wherein:

the previous sweetened gas stream received by the final co-current contactor comprises the second partially-sweetened gas stream released from the second co-current contactor; and

the third liquid solvent received by the second co-current contactor comprises the final lightly-loaded gas-treating solution released by the final co-current contactor.

29. The method of claim 22, further comprising:

using a flash drum, releasing hydrocarbon and H₂O vapors from the second partially-loaded gas-treating solution; and

thereafter

boosting the pressure of the second partially-loaded gas-treating solution before it enters the first co-current contactor.

30. The method of claim 22, wherein:

the first co-current contactor, the second co-current contactor, the final co-current contactor, or combinations thereof, comprise a centrifugal mixer, a static mixer, a mist eliminator, a venturi tube, an electrostatic precipitator, or combinations thereof.

31. The method of claim 20, wherein:

an inlet pressure of the initial gas stream into the first co-current contactor is about 15 to 1,000 psig.

32. The method of claim 20, wherein:

the second liquid solvent and the regenerated liquid solvent comprise amine.

33. The method of claim 32, wherein:

the amine comprises a secondary amine, a primary amine, a tertiary amine, or combinations thereof.

34. The method of claim 20, wherein:

the second liquid solvent and the regenerated liquid solvent comprise physical solvents or solvents comprising a mixture of physical solvents and chemical solvents.

35. The method of claim 22, further comprising:

operating the first co-current contactor at a temperature that is different than operating temperatures of the second co-current contactor, the final co-current contactor, or both.

36. The method of claim 20, further comprising:

operating the gas processing facility for a period of time;

analyzing composition of the initial gas stream; and

in response to changes in composition of the initial gas stream, modifying the gas processing facility.

37. The method of claim 36, wherein modifying the gas processing facility comprises at least one of (i) adding an additional co-current contactor, (ii) changing an operating temperature of at least one of the co-current contactors, or (iii) combinations thereof

38. The method of claim 20, wherein the liquid solvent received by the first contactor is comprised at least in part of a semi-lean solvent obtained from a separate gas sweetening process.

39. A process for removing a gaseous component from a gas stream, comprising:

(a) passing the gas stream through a first contactor and subsequently passing the gas stream through a second contactor;

(b) commingling and contacting the gas stream in the second contactor with a third absorbent liquid, wherein the third absorbent liquid and the gas stream flow co-currently in the second contactor, thereby producing a partially-loaded second absorbent liquid having a second concentration of the gaseous component and producing a gas stream depleted of the gaseous component;

(c) recovering the partially-loaded second absorbent liquid from the second contactor;

(d) passing a second absorbent liquid to the first contactor and commingling and contacting the gas stream in the first contactor with the second absorbent liquid,

wherein;

the second absorbent liquid and the gas stream flow co-currently through the first contactor, and

the first absorbent liquid comprises at least a portion of the partially-loaded second absorbent liquid, thereby producing a first absorbent liquid having a first concentration of gaseous component, the first concentration of the gaseous component in the first absorbent liquid being higher than the second concentration of the gaseous component in the second absorbent liquid; and

(e) recovering the first absorbent liquid from the first contactor.

40. The process of claim 39, wherein the partially-loaded second absorbent liquid recovered in step (c) is passed to the first contactor as the second absorbent liquid.

41. The process of claim 39, further comprising

(f) passing the first absorbent liquid to a regenerator system;

(g) producing in the regenerator system a partially-lean absorbent liquid and a lean absorbent liquid, the partially-lean absorbent liquid having a higher concentration of the gaseous component than a concentration of the gaseous component in the lean absorbent liquid;

(h) recycling the lean absorbent liquid to the final contactor in step (b); and

(i) passing the partially-lean absorbent liquid to the first contactor as the second absorbent liquid.

42. The process of claim 39, further comprising:

as part of step (a), passing the gas stream through a third contactor before the gas stream is passed through the first contactor, and, subsequent to step (c),

passing a fourth absorbent liquid to the third contactor and commingling and contacting the gas stream in the third contactor with the fourth absorbent liquid, wherein the fourth absorbent liquid and the gas stream flow co-currently through at least a portion of the third contactor, and wherein the third absorbent liquid comprises at least a portion of the partially loaded fourth absorbent liquid, thereby producing a third absorbent liquid having a third concentration of gaseous component, the third concentration of the gaseous component in the third absorbent liquid being higher than the fourth concentration of the gaseous component in the fourth absorbent liquid; and

subsequently removing the third absorbent liquid from the first contactor.

43. The process of claim 39, further comprising

regenerating the second absorbent liquid in a regenerator system, thereby producing a lean absorbent liquid, and

recycling the lean absorbent liquid as the third absorbent liquid.

44. The process of claim 39, wherein the absorbent liquid comprises a desiccating liquid containing at least one chemical compound selected from the group comprising monoethylene glycol (MEG), diethylene glycol (DEG), or triethylene glycol (TEG).

45. A process for removing a gaseous component from a gas stream, the process comprising:

(a) sequentially flowing the gas stream through a series of two or more contactors in a downstream direction; and

(b) passing an absorbent liquid through each of the two or more contactors co-currently with the flow of the gas stream in an opposite upstream direction, and recovering from each of the two or more contactors an absorbent liquid effluent stream comprising the gaseous component,

wherein;

the gas stream is progressively depleted of the gaseous component as the gas stream passes through each of the two or more contactors in the downstream direction,

the recovered absorbent liquid from each of the two or more contactors has a progressively higher concentration of the gaseous component in the upstream direction; and

at least a portion of the absorbent liquid recovered from one of the two or more contactors is used as the absorbent liquid for at least one contactor upstream of the flow of the gas stream.

46. The process of claim 45, wherein sequentially flowing the gas stream comprises:

passing the gas stream through a first contactor,

then through at least one additional contactor, and

then through a final contactor.

47. The process of claim 46, wherein passing an absorbent liquid comprises:

passing absorbent liquid recovered from the final contactor to a penultimate contactor,

passing absorbent liquid recovered from the penultimate contactor to an antepenultimate contactor, and

continuing recovery of the absorbent liquid from sequential contactors in the upstream direction, except that the absorbent liquid recovered from the first contactor is passed to a regeneration system, thereby producing a lean absorbent liquid, and

wherein the process further comprises recycling the lean absorbent liquid as the absorbent liquid for passing to the final contactor.