Oxidative coupling of methane implementations for olefin production

Patent metadata

Field	Value
Publication number	US-9701597-B2
Application number	US-201514592668-A
Country	US
Kind code	B2
Filing date	Jan 8, 2015
Priority date	Jan 9, 2014
Publication date	Jul 11, 2017
Grant date	Jul 11, 2017

Abstract

The present disclosure provides oxidative coupling of methane (OCM) systems for small scale and world scale production of olefins. An OCM system may comprise an OCM subsystem that generates a product stream comprising C 2+ compounds and non-C 2+ impurities from methane and an oxidizing agent. At least one separations subsystem downstream of, and fluidically coupled to, the OCM subsystem can be used to separate the non-C 2+ impurities from the C 2+ compounds. A methanation subsystem downstream and fluidically coupled to the OCM subsystem can be used to react H 2 with CO and/or CO 2 in the non-C 2+ impurities to generate methane, which can be recycled to the OCM subsystem. The OCM system can be integrated in a non-OCM system, such as a natural gas liquids system or an existing ethylene cracker.

First claim

What is claimed is:

1. An oxidative coupling of methane (OCM) system, comprising:
(a) an OCM subsystem that (i) takes as input a first feed stream comprising methane (CH 4 ) and a second feed stream comprising an oxidizing agent, and (ii) generates from said methane and said oxidizing agent a product stream comprising hydrocarbon compounds including two or more carbon atoms (C 2+ compounds) and non-C 2+ impurities; and
(b) at least one separations subsystem downstream of, and fluidically coupled to, said OCM subsystem, wherein said separations subsystem comprises a first heat exchanger, a de-methanizer unit downstream of said first heat exchanger, and a second heat exchanger downstream of said de-methanizer unit, wherein
(1) said first heat exchanger cools said product stream,
(2) said de-methanizer unit accepts said product stream from said first heat exchanger and generates an overhead stream comprising methane and at least a portion of said non-C 2+ impurities, and a bottoms stream comprising at least a portion of said C 2+ compounds, and
(3) at least a portion of said overhead stream is cooled in said second heat exchanger and subsequently directed to said first heat exchanger to cool said product stream.

2. The system of claim 1 , wherein said overhead stream is split into at least two streams, and at least one of said two streams is pressurized prior to introduction to said second heat exchanger.

3. The system of claim 1 , further comprising a hydrogenation unit downstream of said de-methanizer, wherein said hydrogenation unit accepts a stream comprising said C 2+ compounds and hydrogenates alkynes in said C 2+ compounds to alkanes and/or alkenes.

4. The system of claim 3 , further comprising a de-ethanizer unit downstream of said hydrogenation unit, wherein said de-ethanizer unit accepts said stream and separates ethane from ethylene.

5. The system of claim 1 , further comprising a methanation subsystem upstream of said OCM subsystem, wherein said methanation subsystem reacts H 2 with CO and/or CO 2 to generate methane, which methane is directed to said OCM subsystem.

6. The system of claim 1 , further comprising a sulfur removal subsystem upstream of said OCM subsystem, wherein said sulfur removal subsystem accepts a feed stream comprising methane and decreases the concentration of sulfur in said feed stream.

7. The system of claim 6 , wherein said sulfur removal subsystem further comprises a heat recovery steam generator unit.

8. The system of claim 1 , further comprising an absorption system downstream of said OCM subsystem, wherein said absorption system decreases the concentration of CO 2 in said product stream.

9. The system of claim 8 , wherein said absorption system comprises an absorption unit and a scrubber downstream of said absorption unit.

10. The system of claim 1 , wherein said OCM subsystem comprises at least one OCM reactor and at least one post-bed cracking unit downstream of said at least one OCM reactor, which post-bed cracking unit is configured to convert at least a portion of alkanes in said product stream to alkenes.

11. The system of claim 1 , wherein said OCM subsystem is adiabatic.

12. The system of claim 1 , further comprising a non-OCM process upstream of said OCM subsystem.

13. The system of claim 12 , wherein said non-OCM process is a natural gas liquids process.

14. The system of claim 1 , wherein said non-C 2+ impurities comprise one or more of nitrogen (N 2 ), oxygen (O 2 ), water (H 2 O), argon (Ar), carbon monoxide (CO), carbon dioxide (CO 2 ) and CH 4 .

15. The system of claim 5 , wherein said methanation subsystem is isothermal.

16. A method, comprising:
(a) directing a first feed stream comprising methane (CH 4 ) and a second feed stream comprising an oxidizing agent into an oxidative coupling of methane (OCM) subsystem that generates from said methane and said oxidizing agent a product stream comprising hydrocarbon compounds including two or more carbon atoms (C 2+ compounds) and non-C 2+ impurities;
(b) directing said product stream from said OCM subsystem into a first heat exchanger downstream of said OCM subsystem, which first heat exchanger cools said product stream;
(c) directing said product stream from said first heat exchanger into a de-methanizer unit downstream of said first heat exchanger, which de-methanizer unit generates an overhead stream comprising methane and at least a portion of said non-C 2+ impurities, and a bottom stream comprising at least a portion of said C 2+ compounds;
(d) directing at least a portion of said overhead stream from said de-methanizer unit into a second heat exchanger downstream of said de-methanizer unit, which second heat exchanger cools said at least said portion of said overhead stream; and
(e) directing said at least said portion of said overhead stream from said second heat exchanger into said first heat exchanger to cool said product stream,
wherein said first heat exchanger, said de-methanizer unit and said second heat exchanger are comprised in at least one separations subsystem that is downstream of and fluidically coupled to said OCM subsystem.

17. The method of claim 16 , furthering comprising splitting said overhead stream into at least two streams, and pressurizing at least one of said two streams prior to introduction to said second heat exchanger.

18. The method of claim 16 , further comprising directing a stream comprising said C 2+ compounds to a hydrogenation unit downstream of said de-methanizer unit, which hydrogenation unit hydrogenates alkynes in said C 2+ compounds to alkanes and/or alkenes.

19. The method of claim 18 , further comprising directing said stream from said hydrogenation unit to a de-ethanizer unit downstream of said hydrogenation unit, which de-ethanizer unit separates ethane from ethylene.

20. The method of claim 16 , further comprising reacting hydrogen (H 2 ) with carbon monoxide (CO) and/or carbon dioxide (CO 2 ) in a methanation subsystem upstream of said OCM subsystem to generate methane, which methane is directed to said OCM subsystem.

21. The method of claim 16 , further comprising directing a feed stream comprising methane into a sulfur removal subsystem upstream of said OCM subsystem, which sulfur removal subsystem decreases the concentration of sulfur in said feed stream.

22. The method of claim 21 , wherein said sulfur removal subsystem further comprises a heat recovery steam generator unit.

23. The method of claim 16 , further comprising decreasing the concentration of CO 2 in said product stream in an absorption system downstream of said OCM subsystem.

24. The method of claim 23 , wherein said absorption system comprises an absorption unit and a scrubber downstream of said absorption unit.

25. The method of claim 16 , wherein said OCM subsystem comprises at least one OCM reactor and at least one post-bed cracking unit downstream of said at least one OCM reactor, which post-bed cracking unit is configured to convert at least a portion of alkanes in said product stream to alkenes.

26. The method of claim 16 , wherein said OCM subsystem is adiabatic.

27. The method of claim 16 , wherein said methanation subsystem is isothermal.

Assignees

• Siluria Technologies Inc

Inventors

• Rafique Humera A
• Vuddagiri Srinivas
• Harraz Hatem
• Radaelli Guido
• Scher Erik C
• Mccormick Jarod
• Iyer Rahul
• Duggal Suchia
• Cizeron Joel
• Hong Jin Ki

Classifications

• C07C2/84 Primary

  catalytic · CPC title

• B01J23/00

  Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 (B01J21/16 takes precedence) · CPC title

• B01J21/04

  Alumina · CPC title

• C07C1/0485

  Set-up of reactors or accessories; Multi-step processes · CPC title

• C07C5/327

  Formation of non-aromatic carbon-to-carbon double bonds only · CPC title