Removal of water and carbon dioxide from air

• US 4,249,915 A
• Filed: 05/30/1979
• Issued: 02/10/1981
• Est. Priority Date: 05/30/1979
• Status: Expired due to Term

• Current Assignee: Air Products and Chemicals Incorporated (Linde Plc)
• Original Assignee: Air Products and Chemicals Incorporated (Linde Plc)
• Inventors: Sircar, Shivaji, Kratz, Wilbur C.
• Primary Examiner(s): Spitzer, Robert H.
• Application Number:
  US06/043,770
• Time in Patent Office: 622 Days
• Field of Search: 55/25, 55/26, 55/33, 55/58, 55/62, 55/68, 55/74, 55/75, 62/18
• US Class Current: 95/99
• CPC Class Codes: B01D 2253/104 Alumina
• CPC Class Codes: B01D 2253/106 Silica or silicates
• CPC Class Codes: B01D 2253/108 Zeolites
• CPC Class Codes: B01D 2257/504 Carbon dioxide
• CPC Class Codes: B01D 2257/80 Water
• CPC Class Codes: B01D 2259/40062 Four
• CPC Class Codes: B01D 2259/40064 Five
• CPC Class Codes: B01D 2259/402 using two beds
• CPC Class Codes: B01D 2259/416 involving cryogenic temperature treatment
• CPC Class Codes: B01D 53/0462 Temperature swing adsorption
• CPC Class Codes: B01D 53/047 Pressure swing adsorption
• CPC Class Codes: B01D 53/0473 Rapid pressure swing adsorption
• CPC Class Codes: B01D 53/261 by adsorption
• CPC Class Codes: Y02C 20/40 of CO2

Abstract

Moisture and CO₂ are removed from atmospheric air by adsorption of these respectively in separate beds. The moisture laden bed is regenerated by pressure swing adsorption in a relatively short operating cycle while the CO₂ -laden bed is regenerated thermally at considerably longer time intervals. The described method is of particular advantage in connection with the pretreatment of air prior to cryogenic distillation for separation of oxygen and nitrogen therein.

Claims

1. The process of removing water and CO₂ from an air feed stream containing the same, which comprises the steps of:

introducing the air stream at superatmospheric pressure into a first bed of solid adsorbent effective in adsorption of water from said feed air stream,

discharging the dried air from the first bed and introducing a major portion thereof into an initial second bed containing adsorbent effective in retention of CO₂,

collecting the clean dry air thus obtained as product gas;

regenerating said first bed after a relatively short on-stream operating period and, during said regenerating of said first bed, introducing the air feed stream into a companion parallel bed of similar composition as said first bed and operated in alternating sequence therewith, the regeneration of said first bed being effected by the sequential steps of;

(a) reducing the pressure at the air feed inlet of the bed thus venting at least voids gas from the bed,

(b) purging the bed at the reduced pressure with a dry gas, and

(c) introducing dried air discharged from said companion bed into the purged bed to bring said bed to initial superatmospheric pressure for further adsorption of water;

said alternating introduction of feed air into said first bed and said companion bed being continued for a relatively long period while continuing to discharge dried air from said first bed and said companion bed each in turn to said initial second bed;

independently regenerating said initial second bed after said relatively long on-stream period by the sequential steps of

(d) depressurizing the CO₂ -laden bed by venting therefrom a gas effluent including voids gas,

(e) elevating the temperature of the bed to drive off adsorbed CO₂,

(f) introducing cool gas into the bed to restore the same to near ambient temperature, and

(g) bringing the cooled bed to its initial adsorption pressure level by introduction of dry CO₂ -free product gas.

2. The process as defined in claim 1 wherein the regeneration of said first bed is carried out after on-stream adsorption of water for not more than fifteen minutes, and said second bed continues adsorption of CO₂ for at least several hours before being subjected to regeneration.

3. The process as defined in claim 1 wherein the air is introduced into said first bed at near ambient temperature.

4. The process as defined in claim 3 wherein the feed air is introduced into said first bed at an absolute pressure of 40 to 300 pounds per square inch.

5. The process as defined in claim 1 wherein the dry, CO₂ -free product air obtained, is subjected to separation of oxygen and nitrogen therein by cryogenic distillation and the obtained nitrogen from said cryogenic distillation is employed as purge gas in step (b).

6. The process as defined in claim 5 wherein nitrogen gas from said cryogenic distillation is employed after heating said gas for elevating the temperature of the second bed during step (e).

7. The process as defined in claim 5 wherein nitrogen gas from said cryogenic distillation is employed for cooling the second bed in step (f).

8. The process as defined in claim 1 wherein said purging in step (b) is effected with a gas stream comprising, at least in part, effluent gas discharged from the second bed during regeneration of such second bed, said gas being flowed through said first bed in a direction counter to initial feed air flow therein.

9. The process as defined in claim 1 wherein introduction of feed air into said first bed and into said companion parallel bed is switched alternately at time periods of less than every 10 minutes.

10. The process as defined in claim 1 wherein during the period of regeneration of said second bed, dried air effluent from the first bed and from its parallel companion bed in alternate turns is introduced into another CO₂ -adsorbent bed operated in parallel to said second bed and similar in composition to that of said second bed.

11. The method as defined in claim 10 wherein during depressuring of said second bed in step (d), at least part of the effluent gas is employed as purge gas in a first bed undergoing step (b).

12. The method as defined in claim 10 wherein during depressuring of said second bed in step (d) at least part of the effluent is employed in pressuring a first bed undergoing step (c).

13. The method as defined in claim 10 wherein said second bed is brought to its initial adsorption pressure level in step (g) by admission into said bed of compressed CO₂ -free effluent from another CO₂ -adsorbent bed operated in parallel to said second bed.

14. The method as defined in claim 10 wherein said second bed continues to receive dried air effluent alternately from the first bed and from the parallel companion to the first bed during a period of at least several hours before said second bed is subjected to regeneration.