Process for maximizing xylenes production from heavy aromatics for use therein

Patent metadata

Field	Value
Publication number	US-10308573-B2
Application number	US-201816018394-A
Country	US
Kind code	B2
Filing date	Jun 26, 2018
Priority date	May 26, 2017
Publication date	Jun 4, 2019
Grant date	Jun 4, 2019

Abstract

A method for producing xylenes from a heavy reformate feed includes the steps of introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, reacting the heavy reformate feed with the hydrogen gas in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, introducing the dealkylation effluent to a splitter unit, separating the dealkylation effluent into a light gas stream, a toluene stream, a benzene stream, a C9 aromatics stream, a C10+ aromatics stream, and a mixed xylene stream in the splitter unit, introducing the toluene stream, the C9 aromatics stream, and a hydrogen stream into a transalkylation reactor, reacting the toluene stream and the C9 aromatics stream in the presence of the transalkylation catalyst to produce a transalkylation effluent, introducing the transalkylation effluent to the splitter unit, and separating the transalkylation effluent in the splitter unit.

First claim

That which is claimed is:

1. A method for producing mixed xylenes from a heavy reformate feed, the method comprising the steps of:
introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, wherein the dealkylation reactor comprises a dealkylation catalyst, wherein the heavy reformate comprises toluene and aromatic hydrocarbons with nine or more carbon atoms (C9+ aromatics), wherein the hydrogen feed comprises hydrogen gas;
reacting the heavy reformate feed with the hydrogen gas in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, wherein the dealkylation reactor is at a dealkylation temperature, wherein the dealkylation reactor is at a dealkylation pressure, wherein the dealkylation reactor has a liquid hourly space velocity;
introducing the dealkylation effluent to a splitter unit, where the dealkylation effluent comprises light gases, toluene, benzene, mixed xylenes, and C9+ aromatics;
separating the dealkylation effluent into a light gas stream, a toluene stream, a benzene stream, a C9 aromatics stream, a C10+ aromatics stream, and a mixed xylene stream in the splitter unit, wherein the light gas stream comprises light hydrocarbons and hydrogen, wherein the toluene stream comprises toluene, wherein the benzene stream comprises benzene, wherein the mixed xylene stream comprises mixed xylenes, wherein the C9 stream comprises C9 aromatics, wherein the C10+ aromatics stream comprises C10+ aromatics;
introducing the toluene stream, the C9 aromatics stream, and a hydrogen stream into a transalkylation reactor, wherein the transalkylation reactor comprises a transalkylation catalyst, wherein the hydrogen stream comprises hydrogen gas;
reacting the toluene stream and the C9 aromatics stream in the presence of the transalkylation catalyst to produce a transalkylation effluent, wherein the transalkylation reactor is at a transalkylation temperature, wherein the transalkylation reactor is at a transalkylation pressure, wherein the transalkylation reactor has a liquid hourly space velocity;
introducing the transalkylation effluent to the splitter unit, wherein the transalkylation effluent comprises light gases, toluene, benzene, mixed xylenes, and C9+ aromatics; and
separating the transalkylation effluent in the splitter unit such that mixed xylenes in the transalkylation effluent exit the splitter unit as part of the mixed xylene stream.

2. The method of claim 1 , wherein the heavy reformate feed contains between 0 wt % and 60 wt % toluene.

3. The method of claim 1 further comprising the steps of:
introducing the light gas stream to a gas separator; and
separating the light gas stream into a produced hydrogen and a light gas product.

4. The method of claim 3 , where the gas separator comprises a pressure swing adsorption unit.

5. The method of claim 1 further comprising the step of introducing the benzene stream to the transalkylation reactor.

6. The method of claim 1 further comprising the step of supplying an added aromatic stream to the transalkylation reactor, such that there is an excess of toluene for transalkylation reactions in the transalkylation reactor.

7. The method of claim 1 , wherein the dealkylation temperature is between 200 deg C. and 500 deg C.

8. The method of claim 1 , wherein the dealkylation pressure is between 5 bar and 40 bar.

9. The method of claim 1 , wherein the liquid hourly space velocity in the dealkylation reactor is between 1 hr-1 and 10 hr-1.

10. The method of claim 1 , wherein the transalkylation temperature is between 300 deg C. and 500 deg C.

11. The method of claim 1 , wherein the transalkylation pressure is between 10 bar and 40 bar.

12. The method of claim 1 , wherein the liquid hourly space velocity in the transalkylation reactor is between 0.5 hr-1 and 6 hr-1.

13. The method of claim 1 , wherein an overall yield of the mixed xylenes in the mixed xylene stream is between 30 wt % and 89 wt %.

14. A method for producing mixed xylenes from a heavy reformate feed, the method comprising the steps of:
introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, wherein the dealkylation reactor comprises a dealkylation catalyst, wherein the heavy reformate comprises aromatic hydrocarbons with nine or more carbon atoms (C9+ aromatics), wherein the hydrogen feed comprises hydrogen gas;
reacting the heavy reformate feed with the hydrogen gas in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, wherein the dealkylation reactor is at a dealkylation temperature, wherein the dealkylation reactor is at a dealkylation pressure, wherein the dealkylation reactor has a liquid hourly space velocity;
introducing the dealkylation effluent to a splitter unit, where the dealkylation effluent comprises light gases, toluene, benzene, mixed xylenes, and C9+ aromatics, where the splitter unit comprises multiple splitter columns;
separating the dealkylation effluent into a light gas stream, a toluene stream, a benzene stream, a C9 aromatics stream, a C10+ aromatics stream, and a mixed xylene stream in the splitter unit, wherein the light gas stream comprises light hydrocarbons and hydrogen, wherein the toluene stream comprises toluene, wherein the benzene stream comprises benzene, wherein the mixed xylene stream comprises mixed xylenes, wherein the C9 stream comprises C9 aromatics, wherein the C10+ aromatics stream comprises C10+ aromatics;
introducing the toluene stream, the C9 aromatics stream, and a hydrogen stream into a transalkylation reactor, wherein the transalkylation reactor comprises a transalkylation catalyst, wherein the hydrogen stream comprises hydrogen gas;
reacting the toluene stream and the C9 aromatics stream in the presence of the transalkylation catalyst to produce a transalkylation effluent, wherein the transalkylation reactor is at a transalkylation temperature, wherein the transalkylation reactor is at a transalkylation pressure, wherein the transalkylation reactor has a liquid hourly space velocity;
introducing the transalkylation effluent to the splitter unit, wherein the transalkylation effluent comprises light gases, toluene, benzene, mixed xylenes, and C9+ aromatics; and
separating the transalkylation effluent in the splitter unit such that mixed xylenes in the transalkylation effluent exit the splitter unit as part of the mixed xylene stream.

15. The method of claim 14 further comprising the steps of:
introducing the light gas stream to a gas separator; and
separating the light gas stream into a produced hydrogen and a light gas product.

16. The method of claim 15 , where the gas separator comprises a pressure swing adsorption unit.

17. The method of claim 14 further comprising the step of introducing the benzene stream to the transalkylation reactor.

18. The method of claim 14 further comprising the step of supplying an added aromatic stream to the transalkylation reactor, such that there is an excess of toluene for transalkylation reactions in the transalkylation reactor.

19. The method of claim 14 , wherein the dealkylation temperature is between 200 deg C. and 500 deg C.

20. The method of claim 14 , wherein the dealkylation pressure is between 5 bar and 40 bar.

21. The method of claim 14 , wherein the liquid hourly space velocity in the dealkylation reactor is between 1 hr-1 and 10 hr-1.

22. The method of claim 14 , where the step of separating the dealkylati

Assignees

• Saudi Arabian Oil Co

Inventors

• Xu Qi
• Abudawoud Raed
• Jazzar Ahmad A
• Zhang Zhonglin

Classifications

• C10G45/72

  Controlling or regulating · CPC title

• C10G45/46

  characterised by the catalyst used · CPC title

• C10G47/00

  Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions (C10G15/00 takes precedence; destructive hydrogenation of non-melting solid carbonaceous or similar materials C10G1/06) · CPC title

• C10G45/44

  Hydrogenation of the aromatic hydrocarbons · CPC title

• C10G2400/30

  Aromatics · CPC title