Thermal decomposition in chemical looping combustion

Patent metadata

Field	Value
Publication number	US-11549063-B2
Application number	US-202017435088-A
Country	US
Kind code	B2
Filing date	Mar 6, 2020
Priority date	Mar 13, 2019
Publication date	Jan 10, 2023
Grant date	Jan 10, 2023

Abstract

A method is presented of thermal decomposition to crack ethane and/or higher alkane hydrocarbon feed or the mixture of any of these hydrocarbons to break down into component elements or simpler constituents using heat from a hot metal agent from a chemical looping combustion process.

First claim

The invention claimed is:

1. A process, comprising:
passing a moving bed of reduced inorganic particulates having a melting temperature greater than 1500° C. and a particle size from 10 to 300 microns through an oxidation reactor at a temperature from 300° C. to 1200° C. for a period of time less than 2 minutes at a gas hourly space velocity for an oxidant from 500 hr −1 to 6000 hr −1 , and a weight hourly space velocity from 0.5 hr −1 to 60 hr −1 , wherein not less than 20 wt % of said reduced inorganic particulates passing through said oxidation reactor are oxidized to produce oxidized inorganic particulates;
passing said oxidized inorganic particulates to and through a moving bed in a fuel reactor together with a fuel in the absence of a gaseous oxidant for a period of time of less than 2 minutes at a gas hourly space velocity for the fuel from 500 hr −1 to 6000 hr −1 , and a weight hourly space velocity from 0.5 hr −1 to 60 hr −1 , to burn the fuel and any surface carbon on the oxidized inorganic particulates and reduce the oxidized inorganic particulates and heat them to a temperature from 1000° C. to 1200° C. to produce heated reduced inorganic particulates;
passing said heated reduced inorganic particulates as a moving bed through at least a portion of a dehydrogenation reactor while flowing one or more alkanes through the dehydrogenation reactor at a temperature from 750° C. to 1200° C. for a period of time less than 2 minutes at a gas hourly space velocity for the one or more alkanes from 500 hr −1 to 6000 hr −1 , and a weight hourly space velocity from 0.5 hr −1 to 60 hr −1 , to produce a product stream comprising: H 2 , one or more olefins, steam, and mixtures of alkynes, aromatics, di-olefins, heavy hydrocarbons and coke; and
passing the reduced inorganic particulates from said dehydrogenation reactor to said oxidation reactor,
wherein:
after producing the oxidized inorganic particulates and before passing the oxidized inorganic particulates through the fuel reactor, the oxidized inorganic particulates do not pass through the dehydrogenation reactor; and
after producing the heated reduced inorganic particulates and before passing the reduced inorganic particulates from said dehydrogenation reactor to said oxidation reactor, the heated reduced inorganic particulates are not oxidized.

2. The process according to claim 1 , wherein the one or more alkanes in the dehydrogenation reactor comprise one or more C 2 -C 4 alkanes.

3. The process according to claim 1 , wherein the reduced inorganic particulates are selected from at least one promoter selected from the group consisting of Lithium (Li), Sodium (Na), Magnesium (Mg), Phosphorus (P), Potassium (K), Calcium (Ca), Titanium (Ti), Vanadium (V), Chromium (Cr), Manganese (Mn), Iron (Fe), Cobalt (Co), Nickel (Ni), Copper (Cu), Zinc (Zn), Gallium (Ga), Arsenic (As), Rubidium (Rb), Strontium (Sr), Yttrium (Y), Zirconium (Zr), Niobium (Nb), Molybdenum (Mo), Ruthenium (Ru), Tin (Sn), Antimony (Sb), Cesium (Cs), Barium (Ba), Lanthanum (La), Cerium (Ce), Praseodymium (Pr), Samarium (Sm), Tungsten (W), Bismuth (Bi), and combinations thereof.

4. The process according to claim 1 , wherein the oxidation reactor is operated at a temperature from 500° C. to 1300° C.

5. The process according to claim 1 , wherein the oxidation reactor is a riser reactor.

6. The process according to claim 1 , wherein the oxidation reactor is a fluid catalytic cracking reactor.

7. The process according to claim 1 , wherein the oxidation reactor is a circulating bed reactor.

8. The process according to claim 4 , wherein the dehydrogenation reactor has an outlet temperature from 850° C. to 1200° C.

9. The process according to claim 1 , wherein not less than 80 wt % of the inorganic particles in the oxidation reactor are oxidized to a higher oxidation state.

10. The process according to claim 1 , wherein the particle size of the reduced inorganic particulates is from 40 to 150 microns.

11. The process according to claim 1 , wherein in the oxidation reactor the gas hourly space velocity for the oxidant is from 1000 hr −1 to 5000 hr −1 , and the weight hourly space velocity is from 0.5 hr −1 to 60 hr −1 .

12. The process according to claim 1 , wherein the fuel for the fuel reactor is natural gas.

13. The process according to claim 1 , wherein in the fuel reactor the gas hourly space velocity for the fuel is from 1000 hr −1 to 5000 hr −1 , and the weight hourly space velocity from 0.5 hr −1 to 60 hr −1 .

14. The process according to claim 1 , wherein in the dehydrogenation reactor the gas hourly space velocity for the alkane and steam is from 1000 hr −1 to 5000 hr 1 , and the weight hourly space velocity from 0.5 hr −1 to 60 hr −1 .

15. The process according to claim 1 , further comprising extracting heat from exhaust from the fuel reactor and providing heat to the one or more alkanes prior to the one or more alkanes entering the dehydrogenation reactor.

16. The process according to claim 1 , where the one or more alkanes comprise one or more C 2 -C 8 alkanes.

17. The process according to claim 1 , wherein the one or more alkanes comprise ethane.

18. The process of claim 1 , further comprising flowing steam through the dehydrogenation reactor while passing said heated reduced inorganic particulates as a moving bed through at least the portion of the dehydrogenation reactor and flowing the one or more alkanes through the dehydrogenation reactor.

19. A process, comprising:
passing a moving bed of reduced inorganic particulates having a melting temperature greater than 1500° C. through an oxidation reactor at a temperature from 300° C. to 1200° C., wherein not less than 20 wt % of the reduced inorganic particulates passing through the oxidation reactor are oxidized to produce oxidized inorganic particulates;
passing the oxidized inorganic particulates to and through a moving bed in a fuel reactor together with natural gas in the absence of a gaseous oxidant to burn the natural gas and any surface carbon on the oxidized inorganic particulates and reduce the oxidized inorganic particulates and heat them to a temperature from 1000° C. to 1200° C. to produce heated reduced inorganic particulates;
passing the heated reduced inorganic particulates as a moving bed through at least a portion of a dehydrogenation reactor while flowing one or more alkanes through the dehydrogenation reactor at a temperature from 750° C. to 1200° C. to produce a product stream comprising H 2 and one or more olefins; and
passing the reduced inorganic particulates from the dehydrogenation reactor to the oxidation reactor.

20. A process, comprising:
passing a moving bed of reduced inorganic particulates having a melting temperature greater than 1500° C. through an oxidation reactor at a temperature from 300° C. to 1200° C., wherein not less than 20 wt % of the reduced inorganic particulates passing through the oxidation reactor are oxidized to produce oxidized inorganic particulates;
passing the oxidized inorganic particulates to and through a moving bed in a fuel reactor together with a fuel in the absence of a gaseous oxidant to burn the fuel and any surface carbon on the oxidized inorganic particulates and reduce the oxidized inorganic particulates and heat them to a temperature from 1000° C. to 1200° C. to produce heated reduced inorganic particulates;
passing the heated reduced inorganic particulates as a moving bed through at least a portion of a dehydrogenation reactor while flowing one or more alkanes through

Assignees

• Nova Chem Int Sa

Inventors

• Simanzhenkov Vasily
• Dey Rabi
• Farag Hany

Classifications

• C10G35/12

  according to the "moving-bed" method · CPC title

• F23C10/01

  in a fluidised bed of catalytic particles · CPC title

• Y02E20/34

  Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery · CPC title

• C10G9/30

  according to the "moving bed" method · CPC title

• C10G9/36 Primary

  with heated gases or vapours · CPC title