PSA process for removal of bulk carbon dioxide from a wet high-temperature gas

• US 6,322,612 B1
• Filed: 12/23/1999
• Issued: 11/27/2001
• Est. Priority Date: 12/23/1999
• Status: Expired due to Fees

• Current Assignee: Air Products and Chemicals Incorporated (Linde Plc)
• Original Assignee: Air Products and Chemicals Incorporated (Linde Plc)
• Inventors: Sircar, Shivaji, Golden, Catherine Marie Anne
• Primary Examiner(s): Spitzer, Robert H.
• Application Number:
  US09/471,982
• Time in Patent Office: 705 Days
• Field of Search: 95/96--06, 951/39, 961/45
• US Class Current: 95/97
• CPC Class Codes: B01D 2257/504 Carbon dioxide
• CPC Class Codes: B01D 2259/40062 Four
• CPC Class Codes: B01D 2259/40064 Five
• CPC Class Codes: B01D 2259/40079 Co-current
• CPC Class Codes: B01D 2259/40081 Counter-current
• CPC Class Codes: B01D 2259/403 using three beds
• CPC Class Codes: B01D 53/0423 Beds in columns
• CPC Class Codes: B01D 53/047 Pressure swing adsorption
• CPC Class Codes: Y02C 20/20 of methane
• CPC Class Codes: Y02C 20/40 of CO2

Abstract

A pressure or vacuum swing adsorption process and apparatus are used for the separation and recovery of certain gaseous components, such as carbon dioxide from hot gas mixtures containing water vapor. The process comprises introducing the feed gas mixture at an elevated temperature into a feed end of an adsorber column containing an adsorbent. The adsorbent preferentially adsorbs at least one adsorbable component. An adsorber effluent, depleted of the at least one adsorbable component, is withdrawn from a product end of the adsorber column. The adsorber column is depressurized below atmospheric pressure and then purged with steam to withdraw an effluent comprising a mixture of the at least one adsorbable component and H₂O. Next, the adsorber column is pressurized by introducing a gas that is depleted of the at least one adsorbable component. The steps are repeated in a cyclic manner.

Claims

1. A pressure swing adsorption process for the separation of a feed gas mixture containing at least one adsorbable component, comprising the steps of:

(a) introducing at an elevated temperature and at an elevated pressure said feed gas mixture into a feed end of an adsorber column containing an adsorbent which preferentially adsorbs said at least one adsorbable component at said elevated temperature and pressure, withdrawing from a product end of said adsorber column a first adsorber effluent depleted of said at least one adsorbable component;

(b) depressurizing said adsorber column by withdrawing therefrom a depressurization gas enriched in said at least one adsorbable component;

(c) purging said adsorber column at sub-atmospheric pressure by introducing into said adsorber column steam heated to a temperature at or near that of said feed gas mixture and withdrawing from said adsorber column a second adsorber effluent comprising a mixture of said at least one adsorbable component and H₂O;

(d) pressurizing said adsorber column to approximately said elevated pressure by introducing into said adsorber column a repressurizing gas depleted of said at least one adsorbable component; and

,

(e) repeating steps (a) through (d) in a cyclic manner.

2. A process as in claim 1, wherein said at least one adsorbable component is CO₂.

3. A process as in claim 1, wherein said adsorbent is selected from the group consisting of K₂CO₃ promoted hydrotalcite, Na₂O impregnated alumina, and double salt extrudates.

4. A process as in claim 1, wherein said depressurization gas in step (b) flows countercurrent to said feed gas mixture in step (a).

5. A process as in claim 1, wherein said steam in step (c) flows countercurrent to said feed gas mixture in step (a).

6. A process as in claim 1, wherein said gas depleted of said one adsorbable component in pressurization step (d) flows countercurrent to said feed gas mixture in step (a).

7. A process as in claim 1, wherein immediately prior to said depressurizing step (b), said process comprises the further steps of discontinuing the introducing of said feed gas mixture and, at said elevated pressure and elevated temperature, rinsing said adsorber column with a gas stream rich in said at least one adsorbable component, wherein said gas stream flows co-current with said feed gas mixture in step (a).

8. A process as in claim 7, wherein immediately following said purging step (c), said process comprises the further step of removing H₂O from said mixture of said at least one adsorbable component and H₂O by condensation to obtain said gas stream rich in said at least one adsorbable component.

9. A process as in claim 7, wherein said depressurization gas is essentially pure CO₂ suitable for use in a subsequent rinse step.

10. A process as in claim 7, wherein said gas stream rich in said at least one adsorbable component is CO₂ that is suitable for use in a subsequent rinse step.

11. A process as in claim 1, wherein immediately following said depressurizing step (b), said process comprises the further step of rinsing said adsorber column at elevated temperature with a gas stream rich in said at least one adsorbable component, wherein said gas stream flows co-current with said feed gas mixture in step (a).

12. A process as in claim 11, wherein immediately following said purge step (c), said process comprises the further step of removing H₂O from said mixture of said at least one adsorbable component and H₂O by condensation to obtain said gas stream rich in said at least one adsorbable component.

13. A process as in claim 11, wherein said step (a) has a duration of about 60 seconds, step (b) has a duration of about 15 seconds, said rinsing step has a duration of about 15 seconds, step (c) has a duration of about 60 seconds, and step (d) has a duration of about 30 seconds.

14. A process as in claim 11, wherein said gas stream rich in said at least one adsorbable component is CO₂ that is suitable for use in a subsequent rinse step.

15. A process as in claim 1, wherein said feed gas contains principally CO₂, CO, H₂, N₂, H₂O, H₂S+COS, said elevated temperature is about 300°

C. to 400°

C., and said at least one adsorbable component is CO₂.

16. A process as in claim 15, wherein said pressure of said feed gas mixture in step (a) is between 100 and 400 p.s.i.g.

17. A process as in claim 1, wherein said feed gas contains principally CO₂, CO, H₂, N₂, H₂O, CH₄, N₂, and H₂S, said elevated temperature is about 260°

C., and said at least one adsorbable component is CO₂.

18. A process as in claim 17, wherein said pressure of said feed gas mixture in step (a) is between about 5 p.s.i.g. and about 60 p.s.i.g.

19. A process as in claim 1, wherein said adsorber column is depressurized during step (b) to a final pressure near an ambient pressure.

20. A process as in claim 1, wherein said feed gas mixture is maintained at about a near ambient superatmospheric pressure during step (a).

21. A process as in claim 1, wherein said feed gas mixture is maintained at a superatmospheric pressure during step (a) of between about 5 p.s.i.g. and about 60 p.s.i.g.

22. A process as in claim 21, wherein said superatmospheric pressure is between about 10 p.s.i.g. and about 500 p.s.i.g.

23. A process as in claim 21, wherein said superatmospheric pressure is approximately 300 p.s.i.g.

24. A process as in claim 1, wherein said feed gas mixture contains principally CO₂ and N₂ at a pressure of approximately 8.62 bar, said elevated temperature is about 200°

C., said at least one adsorbable component is CO₂ and said adsorbent is Na₂O impregnated alumina.

25. A process as in claim 1, wherein said repressurizing gas is an adsorber effluent resulting from step (a).

26. A process as in claim 1 wherein during said step of purging, said adsorber column is maintained at a sub-atmospheric pressure between approximately 1.5 p.s.i.a. and 11.5 p.s.i.a.

27. A pressure swing adsorption apparatus for the separation of a feed gas mixture containing at least one adsorbable component, said apparatus comprising:

(a) an adsorber column containing an adsorbent which preferentially adsorbs said at least one adsorbable component at an elevated temperature and pressure, the adsorber column having a feed end and a product end;

(b) means for introducing at said elevated temperature and at said elevated pressure said feed gas mixture into the feed end of said adsorber column and withdrawing from the product end of said adsorber column a first adsorber effluent depleted of said at least one adsorbable component;

(c) means for depressurizing said adsorber column by withdrawing therefrom a depressurization gas enriched in said at least one adsorbable component;

(d) means for purging said adsorber column by introducing into said adsorber column steam heated to a temperature at or near that of said feed gas mixture and withdrawing from said adsorber column a second adsorber effluent comprising a mixture of said at least one adsorbable component and H₂O;

(e) means for pressurizing said adsorber column to approximately said elevated pressure by introducing into said adsorber column a repressurizing gas depleted of said at least one adsorbable component.