Claims
- 1. A process for kinetic separation of a light hydrocarbon mixture comprising at least two components, by preferentially adsorbing one of said two components on a zeolite adsorbent, said zeolite phase containing 8-member rings of tetrahedra as the pore opening controlling hydrocarbon diffusion, the other of said two components being non-preferentially adsorbed, said process comprising the steps of:
(a) contacting said light hydrocarbon mixture with a zeolite adsorbent, characterized by having a diffusion rate which is at least 50 times greater for the preferentially adsorbed component as compared to said non-preferentially adsorbed component; and (b) recovering said preferentially adsorbed component.
- 2. A process as claimed in claim 1, wherein said hydrocarbon mixture includes an olefin as said preferentially adsorbed component and a paraffin as said non-preferentially adsorbed component.
- 3. A process as claimed in claim 2, wherein said olefin is propylene and said paraffin is propane.
- 4. A process as claimed in claim 3, wherein said zeolite has a diffusion rate which is at least 200 times greater for propylene than for propane.
- 5. A process as claimed in claim 1, wherein said zeolite has a silica-to-alumina ratio greater than about 200.
- 6. A process as claimed in claim 1, wherein said zeolite has a silica-to-alumina ratio greater than about 500.
- 7. A process as claimed in claim 1, wherein said zeolite has a silica-to-alumina ratio greater than about 1000.
- 8. A process as claimed in claim 1, wherein said zeolite has a silica-to-alumina ratio greater than about 2000.
- 9. A process as claimed in claim 1, wherein said zeolite has alkali metal cations as the ions balancing the framework charge.
- 10. A process as claimed in claim 1, wherein said zeolite has a propylene adsorption capacity greater than 40 mg/g.
- 11. A process as claimed in claim 1, wherein said zeolite is of CHA structure type.
- 12. A process as claimed in claim 11, wherein said zeolite has a silica-to-alumina ratio greater than about 200 and contains alkali metal ions as the cations balancing the framework charge.
- 13. A process as claimed in claim 11, wherein said zeolite has a silica-to-alumina ratio greater than about 500 and contains alkali metal ions as the cations balancing the framework charge.
- 14. A process as claimed in claim 11, wherein said zeolite has a silica-to-alumina ratio greater than about 1000 and contains alkali metal ions as the cations balancing the framework charge.
- 15. A process as claimed in claim 11, wherein said zeolite has a silica-to-alumina ratio greater than about 2000 and contains alkali metal ions as the cations balancing the framework charge.
- 16. A process as claimed in claim 11, wherein said CHA structure type 8-member rings zeolite is selected from the group consisting of Si-CHA, high silica chabazite, AlPO4-(CHA), CaAPO-44, CaAPO-47, GaPO4-34, LZ-218, Linde D, Linde R, MeAPO-47, MeAPSO-47, Phi, SAPO-34, SAPO-47, Si-CHA, SSZ-13, Wilhendersonite, ZK-14 and ZYT-6 and mixtures thereof.
- 17. A process as claimed in claim 1, wherein the zeolite has the ITE structure type.
- 18. A process as claimed in claim 17, wherein the zeolite has the ITE structure type, a silica-to-alumina ratio greater than about 200 and contains alkali metal ions as the cations balancing the framework charge.
- 19. A process as claimed in claim 17, wherein the zeolite has the ITE structure type, a silica-to-alumina ratio greater than about 500 and contains alkali metal ions as the cations balancing the framework charge.
- 20. A process as claimed in claim 17, wherein the zeolite has the ITE structure type, a silica-to-alumina ratio greater than about 1000 and contains alkali metal ions as the cations balancing the framework charge.
- 21. A process as claimed in claim 17, wherein the zeolite has the ITE structure type, a silica-to-alumina ratio greater than about 2000 and contains alkali metal ions as the cations balancing the framework charge.
- 22. A process as claimed in claim 17, wherein said ITE structure type is ITQ-3.
- 23. A process as claimed in claim 17, wherein the zeolite has the SAPO-34 structure type, and contains alkali metal ions as the cations balancing the framework charge.
- 24. A process for kinetic separation of a light hydrocarbon mixture comprising at least two components, by preferentially adsorbing one of said two components on a zeolite adsorbent, said zeolite phase containing 8-member rings of tetrahedra as the pore opening controlling hydrocarbon diffusion, the other of said two components being non-preferentially adsorbed, said process comprising the steps of:
(a) contacting said light hydrocarbon mixture with a zeolite adsorbent, characterized by having a diffusion rate which is at least 50 times greater for the preferentially adsorbed component as compared to said non-preferentially adsorbed component; and (b) recovering said non-preferentially adsorbed component.
CROSS-REFERENCE TO RELATED APPLICATIONS
[0001] This Application is a continuation-in-part of my co-pending application Ser. No. 09/768,943, filed on Jan. 23, 2001, the disclosure of which is incorporated herein by specific reference.
Continuation in Parts (1)
|
Number |
Date |
Country |
Parent |
09768943 |
Jan 2001 |
US |
Child |
09844314 |
Apr 2001 |
US |