Air purification process

• US 5,980,611 A
• Filed: 09/25/1997
• Issued: 11/09/1999
• Est. Priority Date: 09/25/1997
• Status: Expired due to Fees

• Current Assignee: BOC Group Pty Limited (Linde Plc)
• Original Assignee: BOC Group Pty Limited (Linde Plc)
• Inventors: Gittleman, Craig S., Kumar, Ravi, Bulow, Martin, Fitch, Frank, Deng, Shuguang, Ojo, Adeola Florence
• Primary Examiner(s): SPITZER, ROBERT H
• Application Number:
  US08/937,713
• Time in Patent Office: 775 Days
• Field of Search: 95/96, 95/98, 95/100-105, 95/117, 95/122, 95/139
• US Class Current: 95/101
• CPC Class Codes: B01D 2253/108 Zeolites
• CPC Class Codes: B01D 2253/30 Physical properties of adsorbents
• CPC Class Codes: B01D 2257/504 Carbon dioxide
• CPC Class Codes: B01D 2257/702 Hydrocarbons
• CPC Class Codes: B01D 2257/80 Water
• CPC Class Codes: B01D 2259/40052 Recycled product or process gas
• CPC Class Codes: B01D 2259/416 involving cryogenic temperature treatment
• CPC Class Codes: B01D 53/047 Pressure swing adsorption
• CPC Class Codes: Y02C 20/40 of CO2

Abstract

Substantially all of the carbon dioxide is removed from a gas containing up to about 1% by volume carbon dioxide by subjecting the gas to a pressure swing adsorption process using as the adsorbent a single layer of zeolite having a silicon to aluminum atomic ratio in the range of 1.5 to 70. The process is particularly suitable for removing substantially all carbon dioxide and water vapor contained in air prior to subjecting the air to cryogenic distillation.

Claims

1. A method of removing carbon dioxide from air containing up to about 1000 ppm carbon dioxide by a pressure swing adsorption process having an adsorption step and an adsorbent regeneration step, the adsorption step of which comprises passing said gas through an adsorption zone containing an adsorbent comprising a layer of a zeolite selected from the group consisting of type Y zeolite, ferrierite, type EMT zeolite, beta, ZSM-5, ZSM-11, ZSM-12, ZSM-57, NU-87 and combinations of these, said zeolite having a silicon/aluminum atomic ratio in the range of about 1.5 to about 70, thereby producing a substantially carbon dioxide-free gas stream.

2. The method of claim 1, wherein said silicon/aluminum atomic ratio is in the range of about 1.6 to about 50.

3. The method of claim 1, wherein said gas additionally contains water vapor and said water vapor is removed from said gas during said adsorption step, thereby producing a substantially water vapor- and carbon dioxide-free gas stream.

4. The method of claim 3, wherein said adsorption zone contains only one layer of adsorbent.

5. The method of claim 3, wherein said substantially carbon dioxide-free gas stream is subjected to cryogenic distillation.

6. The method of claim 5, wherein said adsorbent is purged with a waste stream produced during said cryogenic distillation during at least part of said adsorbent regeneration step.

7. The method of claim 1 or claim 3, wherein said zeolite has as exchangeable cations hydrogen ions, lithium ions, sodium ions, potassium ions or mixtures of these.

8. The method of claim 7, wherein said zeolite has sodium ions as the predominant exchangeable cation.

9. The method of claim 8, wherein said zeolite is sodium Y zeolite.

10. The method of claim 7, wherein said silicon/aluminum atomic ratio is in the range of about 1.6 to about 10.

11. The method of claim 1 or claim 3, wherein said zeolite is ZSM-5, ZSM-11, ZSM-12, ferrierite, beta, NU-87 or combinations of these.

12. The method of claim 11, wherein said silicon/aluminum atomic ratio is in the range of about 15 to about 40.

13. The method of claim 1 or claim 3, wherein said adsorption step is carried out at a temperature in the range of about 0 to about 50°

C.

14. The method of claim 13, wherein said adsorption step is carried out at a pressure in the range of about 0.9 to about 50 bara.

15. The method of claim 13, wherein said adsorbent regeneration step is carried out a pressure in the range of about 0.1 to about 2 bara.

16. The method of claim 1 or claim 3, wherein said adsorbent regeneration step is carried out at a temperature in the range of about 0 to about 100°

C.

17. The method of claim 1 or claim 3, wherein said adsorbent is purged with a substantially water vapor- and carbon dioxide-free gas during at least part of said adsorbent regeneration step.