Chemical looping processes for catalytic hydrocarbon cracking

Patent metadata

Field	Value
Publication number	US-10844289-B2
Application number	US-201816113184-A
Country	US
Kind code	B2
Filing date	Aug 27, 2018
Priority date	Aug 28, 2017
Publication date	Nov 24, 2020
Grant date	Nov 24, 2020

Abstract

Methods of chemical looping include introducing a hydrocarbon-containing feed stream into a first reaction zone. The first reaction zone includes a moving catalyst bed reactor. The moving catalyst bed reactor includes a heterogeneous catalyst, and the heterogeneous catalyst includes a heat-generating metal oxide component. The method further includes cracking the hydrocarbon-containing feed stream in the presence of the heterogeneous catalyst of the moving catalyst bed reactor, reducing the metal oxide heat-generating component of the heterogeneous catalyst with hydrogen from a product stream to generate heat, and utilizing the heat to drive additional cracking of the hydrocarbon-containing feed stream. A chemical looping system includes at least one reduction reactor, which includes a moving catalyst bed reactor and a heterogeneous catalyst, and at least one oxidation reactor fluidly coupled to the reduction reactor.

First claim

What is claimed is:

1. A method of chemical looping comprising:
introducing a hydrocarbon-containing feed stream into a first reaction zone, the first reaction zone comprising a moving catalyst bed reactor, where the moving catalyst bed reactor comprises a heterogeneous catalyst, where the heterogeneous catalyst comprises a heat-generating metal oxide component;
cracking the hydrocarbon-containing feed stream in the presence of the heterogeneous catalyst of the moving catalyst bed reactor to yield a product stream comprising olefins, aromatics, and hydrogen;
reducing the heat-generating metal oxide component of the heterogeneous catalyst with at least one of the olefins, aromatics, and hydrogen from the product stream to generate heat; and
utilizing the heat to drive additional cracking of the hydrocarbon-containing feed stream.

2. The method of claim 1 , further comprising removing a portion of the heterogeneous catalyst from the first reaction zone to a second reaction zone;
oxidizing the portion of the heterogeneous catalyst in the second reaction zone to form an oxidized heterogeneous catalyst; and
transferring the oxidized heterogeneous catalyst from the second reaction zone to the first reaction zone.

3. The method of claim 2 , further comprising generating additional heat by oxidizing the portion of the heterogeneous catalyst in the second reaction zone to form an oxidized heterogeneous catalyst, and
transferring the additional heat to the first reaction zone.

4. The method of claim 1 , further comprising introducing one or more cracking assistants into the first reaction zone.

5. The method of claim 4 , where the one or more cracking assistants are selected from the group consisting of steam, carbon dioxide, methanol, ethanol, formaldehydes, and mixtures thereof.

6. The method of claim 4 , where the one or more cracking assistants comprise steam, the steam being introduced in an amount such that a weight ratio of the steam to hydrocarbons in the hydrocarbon-containing feed stream is from 0.1 to 2.0.

7. The method of claim 1 , further comprising introducing at least one of hydrogen and oxygen into the first reaction zone.

8. The method of claim 1 , further comprising:
removing unreacted hydrocarbons from the first reaction zone; and
recycling the unreacted hydrocarbons by re-introducing the unreacted hydrocarbons into the first reaction zone as a recycle stream.

9. The method of claim 8 , where a weight ratio of hydrocarbons in the recycle stream to hydrocarbons in the hydrocarbon-containing feed stream is from 0.10 to 0.75.

10. The method of claim 1 , where a weight ratio of olefins and aromatics in the product stream to hydrocarbons introduced into the first reaction zone is from 0.2 to 0.75.

11. The method of claim 1 , where a product stream comprises from 5 wt % to 70 wt % C 2 to C 3 olefins.

12. The method of claim 11 , where the C 2 to C 3 olefins comprise ethylene and propylene, and
a weight ratio of ethylene to propylene is from 0.2 to 5.0.

13. The method of claim 1 , where the first reaction zone comprises at least a first fixed temperature zone and a second fixed temperature zone,
the first fixed temperature zone is proximate to a position where the hydrocarbon-containing feed stream is introduced to the first reaction zone,
the second fixed temperature zone is proximate to a position where the product stream is removed from the first reaction zone, and
a temperature in the second fixed temperature zone is greater than a temperature in the second fixed temperature zone.

14. The method of claim 1 , where the first reaction zone comprises a constant temperature gradient from a position where the hydrocarbon-containing feed stream is introduced into the first reaction zone to a position where the product stream is removed from the first reaction zone,
a maximum temperature is at the position where the product stream is removed from the first reaction zone, and
a minimum temperature is at the position where the hydrocarbon-containing feed stream is introduced into the first reaction zone.

15. The method of claim 1 , where the hydrocarbon-containing feed stream is crude oil.

16. A chemical looping system comprising:
a first reaction zone comprising a moving catalyst bed reactor that comprises a heterogeneous catalyst, where the heterogeneous catalyst comprises a heat-generating metal oxide component, where the first reaction zone is configured to:
crack a hydrocarbon-containing feed stream to produce a product stream comprising olefins, aromatics, and hydrogen; and
reduce the heat-generating metal oxide component of the heterogeneous catalyst with the hydrogen from the product stream to generate heat;

a second reaction zone fluidly coupled to the first reaction zone, where the second reaction zone is configured to:
receive reduced heterogeneous catalyst from the first reaction zone;
oxidize the reduced heterogeneous catalyst to form an oxidized heterogeneous catalyst and generate heat; and

transfer the oxidized heterogeneous catalyst to the first reaction zone.

17. The chemical looping system of claim 16 , further comprising at least one separator fluidly coupled to the first reaction zone, where the at least one separator is configured to separate spent heterogeneous catalyst from the olefins, aromatics, and hydrogen in the product stream.

18. The chemical looping system of claim 16 , further comprising at least one hydrocarbon separation unit fluidly coupled to the first reaction zone, where the at least one hydrocarbon separation unit is configured to separate hydrocarbons in the product stream.

19. The chemical looping system of claim 16 , further comprising a second separator fluidly coupled to the second reaction zone, where the second separator is configured to separate the oxidized heterogeneous catalyst from gasses exiting the second reaction zone.

20. The chemical looping system of claim 16 , further comprising a catalytic cooler fluidly coupled to one or more of the first reaction zone and the second reaction zone.

Assignees

• Saudi Arabian Oil Co

Inventors

• Xu Wei
• Abba Ibrahim
• Rivera Rodrigo Sandoval
• Ali Ola

Classifications

• C10G2300/4006

  Temperature · CPC title

• C10G11/16

  according to the "moving bed" method · CPC title

• C10G11/14 Primary

  with preheated moving solid catalysts · CPC title

• C10G11/04

  Oxides · CPC title

• B01J29/48

  containing arsenic, antimony, bismuth, vanadium, niobium tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium · CPC title