Methanol process

Patent metadata

Field	Value
Publication number	US-10640440-B2
Application number	US-201616067927-A
Country	US
Kind code	B2
Filing date	Dec 16, 2016
Priority date	Jan 15, 2016
Publication date	May 5, 2020
Grant date	May 5, 2020

Abstract

A process is described for the synthesis of methanol comprising the steps of: (i) passing a first synthesis gas mixture comprising a make-up gas and a first loop recycle gas stream through a first synthesis reactor containing a cooled methanol synthesis catalyst to form a first product gas stream, (ii) recovering methanol from the first product gas stream thereby forming a first methanol-depleted gas mixture, (iii) combining the first methanol-depleted gas mixture with a second loop recycle gas stream to form a second synthesis gas mixture, (iv) passing the second synthesis gas mixture through a second synthesis reactor containing a cooled methanol synthesis catalyst to form a second product gas stream, (v) recovering methanol from the second product gas stream thereby forming a second methanol-depleted gas mixture, and (vi) forming the first and second loop recycle gas streams from the second methanol-depleted gas mixture, wherein the first synthesis reactor has a higher heat transfer per cubic metre of catalyst than the second synthesis reactor and the recycle ratio of the first loop recycle gas stream to form the first synthesis gas mixture is in the range 0.1 to 1:1, and the recycle ratio of the second loop recycle gas stream to form the second synthesis gas mixture is in the range 1.1:1 to 6:1.

First claim

The invention claimed is:

1. A process for synthesizing methanol comprising the steps of:
(i) passing a first synthesis gas mixture comprising a make-up gas and a first loop recycle gas stream through a first synthesis reactor containing a first cooled methanol synthesis catalyst to form a first product gas stream,
(ii) recovering methanol from the first product gas stream to form a first methanol-depleted gas mixture,
(iii) combining the first methanol-depleted gas mixture with a second loop recycle gas stream to form a second synthesis gas mixture,
(iv) passing the second synthesis gas mixture through a second synthesis reactor containing a second cooled methanol synthesis catalyst to form a second product gas stream,
(v) recovering methanol from the second product gas stream to form a second methanol-depleted gas mixture, and
(vi) forming the first and second loop recycle gas streams from the second methanol-depleted gas mixture,
wherein the first synthesis reactor has a higher heat transfer per cubic metre of catalyst than the second synthesis reactor and the recycle ratio of the first loop recycle gas stream to form the first synthesis gas mixture is in the range of from 0.1 to 1:1, and the recycle ratio of the second loop recycle gas stream to form the second synthesis gas mixture is in the range of from 1.1:1 to 6:1.

2. The process according to claim 1 wherein the recycle ratio of the loop recycle gas stream to form the second synthesis gas mixture is in the range of from 1.5:1 to 6:1.

3. The process according to claim 1 wherein the make-up gas contains carbon monoxide in the range of from 20 to 35% vol.

4. The process according to claim 1 wherein the loop recycle gas streams are circulated by means of a two-stage circulator comprising a first stage and a second stage, or two separate circulators.

5. The process according to claim 4 wherein a circulator comprises a first stage and a second stage, the first stage is fed with the first methanol-depleted gas mixture and the second stage is fed with the second recycle loop gas stream, and the first methanol-depleted gas mixture and the second recycle loop gas stream are combined in the circulator to provide the second synthesis gas.

6. The process according to claim 5 wherein the methanol-depleted gases fed to the circulator are enriched by a portion of the make-up gas.

7. The process according to claim 4 wherein a circulator comprises a first stage and a second stage, the first stage is fed with the second methanol-depleted gas stream minus any purge gas and produces two separate loop recycle gas streams; one from the circulator first stage, which is combined with the first methanol-depleted gas mixture and fed to the second synthesis reactor, and one from the circulator second stage, which is fed to the first synthesis reactor.

8. The process according to claim 7 wherein the first methanol-depleted gas mixture contains a portion of the make-up gas.

9. The process according to claim 4 wherein two separate circulators are used, a first circulator is fed with the first methanol-depleted gas mixture and a second circulator is fed with the second methanol-depleted gas stream, minus any purge stream, the second circulator product is divided into the first and second recycle loop gas streams, and the second recycle loop gas stream is mixed with the first methanol-depleted gas stream product of the first circulator.

10. The process according to claim 9 where the first methanol-depleted gas stream product of the first circulator is diluted with a portion of the make-up gas.

11. The process according to claim 1 wherein the first synthesis reactor comprises the first methanol synthesis catalyst disposed in tubes that are cooled by water under pressure, and the second synthesis reactor comprises a fixed bed of the second methanol synthesis catalyst that is cooled in heat exchange with either water under pressure or a synthesis gas mixture that is the first synthesis gas mixture or the second synthesis gas mixture.

12. The process according to claim 1 wherein the first synthesis reactor is an axial flow steam-raising converter.

13. The process according to claim 1 wherein the second synthesis reactor is a radial flow steam-raising converter, a tube-cooled converter, a gas-cooled converter or a quench reactor.

14. The process according to claim 1 wherein the first, second, or first and second cooled methanol synthesis catalysts are copper-containing methanol synthesis catalysts.

15. The process according to claim 1 wherein methanol synthesis in the first and second reactors is performed at pressures in the range of from 20 to 120 bar abs and temperatures in the range of from 130° C. to 350° C.

16. The process according to claim 15 wherein the pressure in the second synthesis reactor is higher than the pressure in the first synthesis reactor.

17. The process according to claim 1 wherein the gas mixtures fed to the first and/or second synthesis reactors are heated in gas-gas heat exchangers using the product gases from the reactors.

18. The process according to claim 1 wherein the product gas streams from the first and second synthesis reactors are cooled in one or more stages of heat exchange to condense methanol therefrom.

19. The process according to claim 1 wherein a purge gas stream is recovered from the second methanol depleted gas mixture and is used for hydrogen recovery, or is subjected to one or more further processing stages including autothermal reforming, water-gas shift, or methanol synthesis.

20. The process according to claim 1 wherein the recycle ratio of the loop recycle gas stream to form the second synthesis gas mixture is in the range of from 2:1 to 6:1.

21. The process according to claim 1 wherein the loop recycle gas streams are circulated by means of two circulators arranged either in a single casing having one inlet and two outlets at different pressures, a single casing having two inlets at different pressures and one outlet, or in two separate casings.

22. The process according to claim 1 wherein the first, second, or first and second cooled methanol synthesis catalysts are compositions comprising copper, zinc oxide and alumina.

23. The process according to claim 18 , wherein the condensed methanol is recovered and subjected to further processing by one or more stages of distillation to produce a purified methanol product.

Assignees

• Johnson Matthey Davy Technologies Ltd

Inventors

• Yiu Kar Chi

Classifications

• C07C29/151 Primary

  with hydrogen or hydrogen-containing gases · CPC title

• C07C29/152 Primary

  characterised by the reactor used · CPC title

• C07C29/1516

  Multisteps · CPC title

• C07C31/04

  Methanol · CPC title

• C07C29/15

  by reduction of oxides of carbon exclusively · CPC title