Process for producing short-chain olefins with prolonged cycle time

Patent metadata

Field	Value
Publication number	US-9624141-B2
Application number	US-201314399980-A
Country	US
Kind code	B2
Filing date	May 6, 2013
Priority date	May 11, 2012
Publication date	Apr 18, 2017
Grant date	Apr 18, 2017

Abstract

A process for producing short-chain olefins by conversion of oxygenates in a multi-stage fixed-bed reactor, in which the individual stages for reaction zones are covered with beds of a granular, form-selective zeolite catalyst and the feed mixture containing oxygenates is added distributed over the reaction stages. An increase of the availability of the fixed-bed reactor for the olefin production with the same or an increased yield of short-chain olefins is achieved in that one or more reaction zones are charged with a distinctly reduced mass flow of the feed mixture containing oxygenates, wherein the reduced mass flow fraction is distributed over other reaction zones.

First claim

The invention claimed is:

1. A process for producing a hydrocarbon product comprising one or more olefins, by converting a starting material mixture comprising steam and an oxygenate to one or more olefins under oxygenate conversion conditions in a reactor, the process comprising the steps of:
i) dividing the starting material mixture into a first partial stream, at least one succeeding partial stream, and a final partial stream;
ii) charging a first reaction zone of the reactor with steam and the first partial stream, the reactor comprising a plurality of series-connected reaction zones in fluid connection with each other, the reactor comprising the first reaction zone, at least one succeeding reaction zone disposed downstream the first reaction zone, and a final reaction zone disposed downstream the at least one succeeding reaction zone;
iii) charging the at least one succeeding reaction zone with the at least one succeeding partial stream;
iv) additionally charging each of the at least one succeeding reaction zones and the last reaction zone with a product stream from an upstream reaction zone; and
v) further charging the final reaction zone with the final partial stream,
wherein the final partial stream comprises a mass flow rate smaller than a next larger partial stream selected from the group consisting of the first partial stream, the at least one succeeding partial stream, and combinations thereof.

2. The process of claim 1 , wherein the final partial stream is not more than 70% of the next larger partial stream.

3. The process of claim 1 , wherein the process of claim 1 operates according to a first mode, wherein the process may further comprise a second mode of operation, such that during the second mode of operation, the final partial stream charged to the final reaction zone during step v) has a mass flow rate of zero such that the final reaction zone receives no flow of the starting material mixture attributable to the final partial stream.

4. The process of claim 1 , comprising:
supplying at least one recirculation stream to the first reaction zone, the at least one succeeding reaction zone, or a combination thereof,
wherein the at least one recirculation stream is obtained in further processing of a reactor product.

5. The process of claim 1 , wherein the at least one succeeding reaction zone comprises a first succeeding reaction zone, a second succeeding reaction zone, a third succeeding reaction zone, and a fourth succeeding reaction zone.

6. The process of claim 1 , comprising:
reducing the mass flow rate of the final partial stream charged during step v) by a first amount;
increasing the mass flow rate of at least one of the partial streams of steps ii) and iii) such that the overall mass flow of the starting material mixture supplied to the reactor is maintained constant.

7. The process of claim 1 , comprising:
reducing the mass flow rate of the final partial stream charged during step v) by a first amount;
increasing the mass flow rate of at least one of the partial streams of steps ii) and iii) by a second amount that is lower than the first amount such that the overall mass flow of the starting material mixture supplied to the reactor is reduced.

8. The process of claim 1 wherein the converting is carried out in a temperature range from 300° C. to 600° C.

9. The process of claim 1 , wherein the converting is carried out in a temperature range from 360° C. to 550° C.

10. The process of claim 1 wherein the converting is carried out in a pressure range from 0.1 bar to 20 bar, absolute.

11. The process of claim 1 , wherein the converting is carried out in a pressure range from 0.5 bar to 5 bar, absolute.

12. The process of claim 1 , wherein the converting is carried out in a pressure range from 1 bar to 3 bar, absolute.

13. The process of claim 1 wherein the reaction zones comprise a granular, form-selective zeolite catalyst of the pentasil type in the form of a fixed bed.

14. The process of claim 1 , wherein the oxygenate comprises methanol, dimethyl ether, or both.

15. The process of claim 1 , wherein the first reaction zone is additionally charged with at least one recirculation stream.

16. The process of claim 13 , wherein the reaction zones comprise a ZSM-5 catalyst.

17. A process for producing a hydrocarbon product comprising one or more olefins, the process comprising the steps of:
converting a starting material mixture comprising steam and an oxygenate to one or more olefins under oxygenate conversion conditions in a reactor, the reactor comprising a plurality of series-connected reaction zones in fluid connection with each other, wherein each reaction zone produces a respective product stream,
wherein the step of converting the starting material mixture further comprises a first mode of operation having the steps of:
dividing the starting material mixture into a first partial stream, at least one intermediate partial stream, and a final partial stream;
charging a first reaction zone of the reactor with steam and the first partial stream, wherein the plurality of series-connected reaction zones comprise the first reaction zone, at least one intermediate reaction zone located downstream the first reaction zone, and a final reaction zone located downstream the at least one intermediate reaction zone;
charging the at least one intermediate reaction zone with the intermediate partial stream, wherein each of the at least one intermediate reaction zones is charged with the product stream from the reaction zone immediately upstream each intermediate reaction zone; and
charging the final reaction zone with the final partial stream, wherein the final partial stream has a mass flow rate smaller than the mass flow rate of a partial stream selected from the group consisting of the first partial stream, each of the at least one intermediate partial streams, and combinations thereof.

18. The process of claim 17 , wherein the process comprises a second mode of operation having the steps of:
reducing the mass flow rate of the final partial stream charged to the final reaction zone by a first amount such that the mass flow rate of the final partial stream to the final reaction zone is zero; and
increasing the mass flow rate of a remaining partial stream by the first amount such that the total flow rate of starting material mixture remains constant for both the first mode and second mode of operation, wherein the remaining partial stream is selected from the group consisting of the first partial stream, each of the at least one intermediate partial streams, and combinations thereof.

19. The process of claim 17 , wherein the process comprises a second mode of operation having the steps of:
reducing the mass flow rate of the final partial stream charged to the final reaction zone by a first amount such that the mass flow rate of the final partial stream to the final reaction zone is zero; and
increasing the mass flow rate of a remaining partial stream by the first amount such that the total flow rate of starting material mixture is higher in the first mode as compared to the second mode of operation, wherein the remaining partial stream is selected from the group consisting of the first partial stream, each of the at least one intermediate partial streams, and combinations thereof.

20. A process for producing a hydrocarbon product comprising one or more olefins, by converting a starting material mixture comprising steam and an oxygenate to one or more olefins under oxygenate convers

Assignees

• Air Liquide
• L'Air Liquide Société Anonyme Pour L'Étude Et L'Exploitation Des Procedes Georges Claude

Inventors

• Renner Thomas
• Castillo-Welter Frank
• Haag Stephane
• Gorny Martin
• Ohlhaver Theis
• Olindo Roberta

Classifications

• B01J8/0492 Primary

  Feeding reactive fluids (for solid material, see B01J8/0015) · CPC title

• C07C1/20

  starting from organic compounds containing only oxygen atoms as heteroatoms · CPC title

• B01J8/0453

  the beds being superimposed one above the other · CPC title

• C07C1/22 Primary

  by reduction · CPC title

• C07C2529/40

  of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11 · CPC title