Process for producing benzene from a C5-C12 hydrocarbon mixture

Patent metadata

Field	Value
Publication number	US-10233136-B2
Application number	US-201816130488-A
Country	US
Kind code	B2
Filing date	Sep 13, 2018
Priority date	Jun 13, 2014
Publication date	Mar 19, 2019
Grant date	Mar 19, 2019

Abstract

The invention relates to a process for producing benzene, comprising the steps of:
(a) providing a hydrocracking feed stream comprising C5-C12 hydrocarbons, (b) contacting the hydrocracking feed stream in the presence of hydrogen with a hydrocracking catalyst comprising 0.01-1 wt-% hydrogenation metal in relation to the total catalyst weight and a zeolite having a pore size of 5-8 Å and a silica (SiO 2 ) to alumina (Al 2 O 3 ) molar ratio of 5-200 under process conditions including a temperature of 425-580° C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-15 h −1 to produce a hydrocracking product stream comprising benzene, toluene and C8+ hydrocarbons, (c) separating benzene, toluene and the C8+ hydrocarbons from the hydrocracking product stream and (d) selectively recycling back at least part of the toluene from the separated products of step (c) to be included in the hydrocracking feed stream.

First claim

The invention claimed is:

1. A process for producing benzene, comprising the steps of:
(a) providing a hydrocracking feed stream comprising C5-C12 hydrocarbons,
(b) contacting the hydrocracking feed stream in the presence of hydrogen with a hydrocracking catalyst to produce a hydrocracking product stream comprising benzene, toluene and C8+ hydrocarbons,
(c) separating benzene, toluene and the C8+ hydrocarbons from the hydrocracking product stream, and
(d) selectively recycling part of the toluene from the separated products of step (c) to the hydrocracking feed stream,
wherein the hydrocracking feed stream has a weight ratio of benzene to toluene of less than 1.58:1.

2. The process according to claim 1 , wherein the hydrocracking feed stream has a weight ratio of benzene to toluene of less than or equal to 1.20:1.

3. The process according to claim 1 , wherein an amount of the toluene recycled to the hydrocracking feed stream is 10-80 wt % of the toluene in the hydrocracking product stream.

4. The process according to claim 1 , wherein the amount of the toluene recycled to the hydrocracking feed stream is 50-70 wt % of the toluene in the hydrocracking product stream.

5. The process according to claim 1 , wherein step (a) involves mixing a fresh feed stream and the recycled toluene, wherein the fresh feed stream comprises at least 10 wt % benzene.

6. The process according to claim 5 , wherein the fresh feed stream is pyrolysis gasoline, straight run naphtha, light coker naphtha, coke oven light oil or mixtures thereof, optionally after being hydrogenated in a hydrogenation reactor.

7. The process according to claim 5 , wherein the fresh feed stream comprises at least 20 wt % benzene.

8. The process according to claim 7 , wherein the fresh feed stream comprises at least 30 wt % benzene.

9. The process according to claim 1 , wherein the hydrocracking feed stream has not been subjected to the step of removing benzene.

10. The process according to claim 1 , wherein the hydrocracking feed stream comprises at least 1 wt % and at most 20 wt % benzene.

11. The process according to claim 1 , wherein the amount of toluene to be recycled to the hydrocracking feed stream is set so that the proportion of benzene in the hydrocracking product stream is 0-5 mol % higher than the proportion of benzene in the hydrocracking feed stream.

12. The process according to claim 1 , wherein xylene is separated from the hydrocracking product stream.

13. The process according to claim 1 , wherein the amount of toluene to be recycled to the hydrocracking feed stream is set so that the ratio of [molar amount of benzene+molar amount of ethylbenzene]*[molar amount of xylene] divided by [molar amount of toluene] 2 in the hydrocracking feed stream is 0.02 to 20.

14. The process according to claim 1 , wherein the amount of toluene to be recycled to the hydrocracking feed stream is set so that the ratio of [molar amount of benzene+molar amount of ethylbenzene]*[molar amount of xylene] divided by [molar amount of toluene] 2 in the hydrocracking feed stream is 0.05 to 0.15.

15. The process according to claim 1 , wherein contacting the hydrocracking feed stream in the presence of hydrogen with the hydrocracking catalyst comprises process conditions including a temperature of 425-580° C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-15 h −1 .

16. The process according to claim 15 , wherein the hydrocracking catalyst comprises 0.01-1 wt-% hydrogenation metal in relation to the total catalyst weight and a zeolite having a pore size of 5-8 Å and a silica (SiO 2 ) to alumina (Al 2 O 3 ) molar ratio of 5-200.

17. The process according to claim 16 , wherein the hydrocracking catalyst comprises less than 0.01 parts tin, less than 0.02 parts lead, and less than 0.01 parts bismuth on the basis of 100 parts by weight of the total catalyst.

18. The process according to claim 16 , wherein the zeolite is a ZSM-5 zeolite.

19. The process according to claim 16 , wherein the hydrogenation metal is platinum.

20. The process according to claim 16 , wherein the hydrocracking catalyst comprises the hydrogenation metal on a zeolite-based support.

Assignees

• Sabic Global Technologies Bv

Inventors

• Davies Andrew
• Fickel Dustin
• Van Iersel Maikel

Classifications

• C10G2400/30

  Aromatics · CPC title

• C10G2300/708

  Coking aspect, coke content and composition of deposits · CPC title

• C10G2300/4081

  Recycling aspects · CPC title

• C10G2300/4056

  Retrofitting operations · CPC title

• C10G2300/301

  Boiling range · CPC title