Process for producing LPG from a heavy hydrocarbon feed

• US 10,639,617 B2
• Filed: 09/15/2016
• Issued: 05/05/2020
• Est. Priority Date: 09/30/2015
• Status: Active Grant

• Current Assignee: SABIC Global Technologies BV (Government of Saudi Arabia)
• Original Assignee: SABIC Global Technologies BV (Government of Saudi Arabia)
• Inventors: Aramburo, Luis, van Iersel, Maikel, Farmer, Dustin, Stevenson, Scott A., van Kimmenade, Emiel
• Primary Examiner(s): Johnson, Edward M
• Application Number:
  US15/762,797
• Publication Number:
  US 20180280944A1
• Time in Patent Office: 1,328 Days
• Field of Search: 502 66
• CPC Class Codes: B01J 2029/081 Increasing the silica/alumina ratio; Desalumination
• CPC Class Codes: B01J 2229/16 to increase the Si/Al ratio; Dealumination
• CPC Class Codes: B01J 2229/186 not in framework positions
• CPC Class Codes: B01J 2229/42 Addition of matrix or binder particles
• CPC Class Codes: B01J 29/126 Y-type faujasite
• CPC Class Codes: C10G 47/18 the catalyst containing platinum group metals or compounds thereof

Abstract

A process comprising contacting said feed in the presence of hydrogen with a M/zeolite catalyst under hydrocracking process conditions.

Claims

1. A process for producing LPG from a hydrocarbon feed comprising polyaromatics, the process comprising contacting the feed in the presence of hydrogen with a M/zeolite catalyst at a pressure of 65-150 bara, a temperature of 350-500°

C., a WHSV of 0.1-10 h<sup>−

1</sup>

wherein said M/zeolite catalyst comprises

0.05-2.5 wt-% of element M, wherein said element M is one or more elements selected from Group 10 of the Periodic Table of Elements; and

an aluminosilicate zeolite having a pore size of 6-8 Å and

a SiO₂/Al₂O₃ ratio of 50-120.

2. The process according to claim 1, wherein the process conditions comprise a pressure of 70-120 bara.

3. The process according to claim 2, wherein the process conditions further comprise a temperature of 400-470°

C.and a WHSV of 1-3 h<sup>−

1</sup>.

4. The process according to claim 1, wherein the M/zeolite catalyst comprises an aluminosilicate zeolite having a SiO₂/Al₂O₃ ratio of 60-100.

5. The process according to claim 1, wherein the M/zeolite catalyst comprises 0.5-2 wt-% of element M.

6. The process according to claim 1, wherein element M is one or more elements selected from the group consisting of Pd and Pt.

7. The process according to claim 1, wherein the aluminosilicate zeolite has a 12-ring structure.

8. The process according to claim 1, wherein the aluminosilicate zeolite comprises super cages having a size of 12-14 Å

.

9. The process according to claim 8, wherein the aluminosilicate zeolite is zeolite Y.

10. The process according to claim 9, wherein the zeolite Y is partially dealuminated.

11. The process according to claim 1, wherein the hydrocarbon feed is selected from the group consisting of heavy cycle oil, light cycle oil, carbon black oil, cracked distillate and pyoil.

12. The process according to claim 1, wherein element M is Pt.

13. The process according to claim 12, wherein the hydrocarbon feed comprises at least 10 wt-% polyaromatics.

14. The process according to claim 13, wherein the aluminosilicate zeolite is zeolite Y.

15. The process according to claim 12, wherein the M/zeolite catalyst comprises 0.5-2 wt-% of Pt.

16. The process according to claim 1, wherein the hydrocarbon feed comprises at least 10 wt-% polyaromatics.

17. The process according to claim 1, wherein an amount of the LPG produced is at least 70 wt-% based on a total product.

18. The process according to claim 17, wherein an amount of methane produced is less than 1 wt-% based on a total product.

19. The process according to claim 1, wherein an amount of methane produced is less than 1 wt-% based on a total product.