Processes for upgrading alkanes and alkyl aromatic hydrocarbons

Patent metadata

Field	Value
Publication number	US-12054456-B2
Application number	US-202217745566-A
Country	US
Kind code	B2
Filing date	May 16, 2022
Priority date	Aug 6, 2020
Publication date	Aug 6, 2024
Grant date	Aug 6, 2024

Abstract

Processes for upgrading a hydrocarbon. The process can include introducing, contacting, and halting introduction of a hydrocarbon-containing feed into a reaction zone. The feed can be contacted with a catalyst within the reaction zone to effect dehydrogenation, dehydroaromatization, and/or dehydrocyclization of the feed to produce a coked catalyst and an effluent. The process can include introducing, contacting, and halting introduction of an oxidant into the reaction zone. The oxidant can be contacted with the coked catalyst to effect combustion of the coke to produce a regenerated catalyst. The process can include introducing, contacting, and halting introduction of a reducing gas into the reaction zone. The reduction gas can be contacted with the regenerated catalyst to produce a regenerated and reduced catalyst. The process can include introducing and contacting an additional quantity of the feed with the regenerated and reduced catalyst to produce a re-coked catalyst and additional first effluent.

First claim

What is claimed is:

1. A process for upgrading a hydrocarbon, comprising:
(I) introducing a hydrocarbon-containing feed comprising one or more of C 2 -C 16 linear or branched alkanes, one or more of C 4 -C 16 cyclic alkanes, one or more of C 8 -C 16 alkyl aromatics, or a mixture thereof into a reaction zone;
(II) contacting the hydrocarbon-containing feed with a catalyst disposed within the reaction zone to effect at least one of dehydrogenation, dehydroaromatization, and dehydrocyclization of at least a portion of the hydrocarbon-containing feed to produce a coked catalyst and a first effluent comprising one or more upgraded hydrocarbons and molecular hydrogen, wherein the hydrocarbon-containing feed and the catalyst are contacted at a temperature in a range from 300° C. to 900° C., for a time period of 1 minute to 90 minutes, and under a hydrocarbon partial pressure of at least 20 kPa-absolute, wherein the hydrocarbon partial pressure is the total partial pressure of any C 2 -C 16 alkanes and any C 8 -C 16 alkyl aromatics in the hydrocarbon-containing feed, wherein the hydrocarbon-containing feed and the catalyst are contacted in the presence of steam in an amount from 0.1 vol % to 40 vol %, based on a total volume of any C 2 -C 16 alkanes, and any C 8 -C 16 alkyl aromatics in the hydrocarbon-containing feed, wherein the catalyst comprises a Group 8-10 element or a compound thereof disposed on a support, and wherein the support comprises a mixed Mg/Al metal oxide having a molar ratio of Mg to Al in a range from 1:1 to 10:1;
(III) halting introduction of the hydrocarbon-containing feed into the reaction zone;
(IV) introducing an oxidant into the reaction zone;
(V) contacting the oxidant with the coked catalyst to effect combustion of at least a portion of the coke to produce a regenerated catalyst lean in coke and a second effluent comprising a combustion gas, wherein the oxidant and the coked catalyst are contacted for a time period of 1 minute to 90 minutes;
(VI) halting introduction of the oxidant into the reaction zone;
(VII) introducing a reducing gas into the reaction zone;
(VIII) contacting the reducing gas with the regenerated catalyst to produce a regenerated and reduced catalyst and a third effluent, wherein the reducing gas and the regenerated catalyst are contacted for a time period of 0.1 seconds to 90 minutes;
(IX) halting introduction of the reducing gas into the reaction zone;
(X) introducing an additional quantity of the hydrocarbon-containing feed into the reaction zone; and
(XI) contacting the additional quantity of the hydrocarbon-containing feed with the regenerated and reduced catalyst to produce a re-coked catalyst and additional first effluent, wherein the additional quantity of the hydrocarbon-containing feed and the regenerated and reduced catalyst are contacted at a temperature in a range from 300° C. to 900° C., for a time period of 1 minute to 90 minutes, under a hydrocarbon partial pressure of at least 20 kPa-absolute, wherein the hydrocarbon partial pressure is the total partial pressure of any C 2 -C 16 alkanes and any C 8 -C 16 alkyl aromatics in the hydrocarbon-containing feed, wherein the additional quantity of the hydrocarbon-containing feed and the catalyst are contacted in the presence of steam in an amount from 0.1 vol % to 40 vol %, based on a total volume of any C 2 -C 16 alkanes, and any C 8 -C 16 alkyl aromatics in the additional quantity of the hydrocarbon-containing feed.

2. The process of claim 1 , wherein an inverse temperature profile or an isothermal temperature profile is maintained within the reaction zone during step (II).

3. The process of claim 1 , wherein the catalyst is disposed in a fixed bed within the reaction zone.

4. The process of claim 1 , wherein step (IV) further comprises:
introducing a fuel with the oxidant into the reaction zone; and
combusting at least a portion of the fuel within the reaction zone to produce heat that heats the reaction zone to a temperature of ≥ 580° C.

5. The process of claim 1 , wherein the oxidant is at a temperature in a range from 580° C. to 1,100° C. and at a pressure in a range from 20 kPa-absolute to 1,000 kPa-absolute when contacted with the coked catalyst, and wherein the reducing gas is at a temperature in a range from 450° C. to 900° C. when contacted with the regenerated catalyst.

6. The process of claim 1 , wherein the catalyst further comprises up to 10 wt % of a promoter disposed on the support based on the weight of the support, and wherein the promoter comprises Sn.

7. The process of claim 1 , wherein the catalyst further comprises up to 5 wt % of an alkali metal element disposed on the support based on the weight of the support.

8. The process of claim 1 , wherein, during normal operation, the oxidant contacts the coked catalyst in step (V) at a normal temperature, a normal pressure, and for a normal period of time, the process further comprising every 12 hours to 90 days modifying step (V) by increasing the normal temperature, increasing the normal pressure, increasing the normal period of time, or a combination thereof to effect a re-activation of the coked catalyst.

9. The process of claim 1 , wherein the reaction zone is a first reaction zone and the catalyst is a first catalyst, the process further comprising:
carrying out steps (I)-(XI) within a second reaction zone comprising a second catalyst; and
carrying out steps (I)-(XI) within a third reaction zone comprising a third catalyst, wherein the first reaction zone, the second reaction zone, and the third reaction zone are operated in parallel, and wherein a timing of the steps (I)-(XI) between the first, second, and third reaction zones is such that there is a continuous production of the one or more upgraded hydrocarbons and molecular hydrogen across the first, second, and third reaction zones.

10. The process of claim 1 , wherein:
the time period the hydrocarbon-containing feed and the catalyst are contacted in step (II) is from 1 minute to 30 minutes,
the time period the oxidant and the coked catalyst are contacted in step (V) is from 1 minute to 30 minutes,
the time period the reducing gas and the regenerated catalyst are contacted in step (VIII) is from 0.1 seconds to 30 minutes, and
the time period the additional quantity of the hydrocarbon-containing feed and the regenerated and reduced catalyst are contacted in step (XI) is from 1 minute to 30 minutes.

11. The process of claim 10 , wherein a cycle time from the contacting the hydrocarbon-containing feed with the catalyst in step (II) to the contacting the additional quantity of the hydrocarbon-containing feed with the regenerated and reduced catalyst in step (XI) is <90 minutes.

12. The process of claim 11 , wherein:
the catalyst further comprises up to 10 wt % of a promoter disposed on the support based on the weight of the support,
the promoter comprises Sn,
the catalyst comprises 0.001 wt % to 6 wt % of the Group 8-10 element or the compound thereof based on the weight of the support,
the Group 8-10 element comprises Pt, and
the molar ratio of Mg to Al is in a range from 2:1 to 10:1.

13. The process of claim 1 , wherein the hydrocarbon-containing feed and the catalyst are contacted in the presence of steam in an amount from 0.1 vol % to 30 vol %, based on a total volume of any C 2 -C 16 alkanes and any C 8 -C 16 alkyl aromatics in the hydrocarbon-containing feed.

14. The process of claim 1 , wherein the hydrocarbon-containing feed and the catalyst are contacted in the presence of steam in an amount from 0.1 vol % to 20 vol %, based on a total volume of any C 2 -C 16 alkanes and

Assignees

• Exxonmobil Chemical Patents Inc

Inventors

• Bao Xiaoying
• Coleman John S

Classifications

• C07C2523/42

  Platinum · CPC title

• C07C2523/14

  of germanium, tin or lead · CPC title

• C07C2523/10

  of rare earths · CPC title

• C07C2521/10

  Magnesium; Oxides or hydroxides thereof · CPC title

• C07C2521/04

  Alumina · CPC title