Methods for dehydrogenating hydrocarbons

Patent metadata

Field	Value
Publication number	US-12344577-B2
Application number	US-202318307619-A
Country	US
Kind code	B2
Filing date	Apr 26, 2023
Priority date	Aug 31, 2018
Publication date	Jul 1, 2025
Grant date	Jul 1, 2025

Abstract

According to one or more embodiments described herein, a method for dehydrogenating hydrocarbons may include passing a hydrocarbon feed comprising one or more alkanes or alkyl aromatics into a fluidized bed reactor, contacting the hydrocarbon feed with a dehydrogenation catalyst in the fluidized bed reactor to produce a dehydrogenated product and hydrogen, and contacting the hydrogen with an oxygen-rich oxygen carrier material in the fluidized bed reactor to combust the hydrogen and form an oxygen-diminished oxygen carrier material. In additional embodiments, a dual-purpose material may be utilized which has dehydrogenation catalyst and oxygen carrying functionality.

First claim

What is claimed is:

1. A method for dehydrogenating hydrocarbons comprising:
passing a hydrocarbon feed comprising one or more alkanes or alkyl aromatics into a fluidized bed reactor, wherein at least 95 wt. % of the hydrocarbon feed has an atmospheric boiling point of less than or equal to 300° C.;
contacting the hydrocarbon feed with a dehydrogenation catalyst in the fluidized bed reactor to produce a dehydrogenated product and hydrogen, wherein the hydrogen is hydrogen gas (H 2 );
contacting the hydrogen with an oxygen-rich oxygen carrier material in the fluidized bed reactor to combust the hydrogen and form an oxygen-diminished oxygen carrier material, wherein the oxygen-rich oxygen carrier material is reducible, wherein the oxygen carrier material exhibits Geldart A properties or Geldart B properties, and wherein the dehydrogenation catalyst and the oxygen-rich oxygen carrier material are separate particles;
passing the oxygen-diminished oxygen carrier material and the dehydrogenation catalyst to a regeneration unit;
oxidizing the oxygen-diminished oxygen carrier material in the regeneration unit to form the oxygen-rich oxygen carrier material; and
passing the oxygen-rich oxygen carrier material to the fluidized bed reactor.

2. The method of claim 1 , wherein the fluidized bed reactor operates at a temperature of greater than 600° C. and less than 850° C.

3. The method of claim 1 , wherein the fluidized bed reactor comprises from 25 wt. % to 75 wt. % of the dehydrogenation catalyst based on the total weight of solids in the fluidized bed reactor.

4. The method of claim 1 , wherein the oxygen-rich oxygen carrier material comprises from 1 wt. % to 20 wt. % releasable oxygen based on a total weight of the oxygen-rich oxygen carrier material.

5. The method of claim 1 , wherein contacting the hydrogen with the oxygen-rich oxygen carrier material removes from 1 wt. % to 50 wt. % of the releasable oxygen from the oxygen-rich oxygen carrier material.

6. The method of claim 1 , wherein contacting the hydrogen with the oxygen-rich oxygen carrier material combusts greater than 50% of the hydrogen.

7. The method of claim 1 , further comprising partially reducing the oxygen-rich oxygen carrier material prior to contacting the hydrocarbon feed, the hydrogen, or both with the oxygen-rich oxygen carrier material in the fluidized bed reactor.

8. The method of claim 1 , wherein a supplemental fuel is combusted in the regeneration unit to produce heat and increase the temperature of one or more of the oxygen-rich oxygen carrier material or the dehydrogenation catalyst.

9. The method of claim 1 , wherein the regeneration unit operates at a temperature of 725° C. to 875° C.

10. The method of claim 1 , wherein the regeneration unit has a temperature of at least 50° C. greater than that of the fluidized bed reactor.

11. The method of claim 1 , wherein enough heat is generated during the re-oxidation of the oxygen-diminished oxygen carrier material to act as a source of heat for the reaction in the fluidized bed reactor.

12. The method of claim 1 , the fluidized bed reactor operates at a temperature of from 625° C. to 770° C.

13. The method of claim 1 , the fluidized bed reactor operates at a temperature of from 650° C. to 770° C.

14. The method of claim 1 , wherein a flue gas is passed into the regeneration unit.

15. The method of claim 14 , wherein the flue gas passed into the regeneration unit is all or a portion of the flue gas exiting the regeneration unit such that it is recycled to the regeneration unit.

16. The method of claim 15 , wherein the flue gas passed into the regeneration unit is mixed with fresh air prior to being passed into the regeneration unit.

17. The method of claim 16 , wherein a mixture of flue gas and fresh air passed into the regeneration unit comprises at least 25 mol % oxygen.

18. The method of claim 16 , wherein a mixture of flue gas and fresh air passed into the regeneration unit comprises from 4 mol % to 25 mol % oxygen.

19. The method of claim 16 , wherein a mixture of flue gas and fresh air passed into the regeneration unit comprises from 10 mol % to 21 mol % oxygen.

Assignees

• Dow Global Technologies Llc

Inventors

• Blann Kevin
• Kirilin Alexey
• Malek Andrzej
• Sussman Victor
• Pretz Matthew T
• Stears Brien A
• Fish Barry B
• Stangland Eric E
• Goodfellow Brian W
• Sharma Manish

Classifications

• C07C2523/42

  Platinum · CPC title

• C07C2523/26

  Chromium · CPC title

• C07C2523/08

  of gallium, indium or thallium · CPC title

• C07C2521/10

  Magnesium; Oxides or hydroxides thereof · CPC title

• C07C2521/06

  Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof · CPC title