Methanol loop revamp by co intensification

Patent metadata

Field	Value
Publication number	US-2025109086-A1
Application number	US-202318834483-A
Country	US
Kind code	A1
Filing date	Apr 3, 2023
Priority date	Apr 8, 2022
Publication date	Apr 3, 2025
Grant date	—

Abstract

A methanol plant is provided in which a first feed comprising CO2 and a second feed comprising H2 are provided, the combined feed is shifted in a CO2 shift unit so as to provide a first synthesis gas stream. Water is removed in a water removal unit, to provide a second synthesis gas stream. A methanol synthesis section receives the second synthesis gas stream, and provides a product stream comprising methanol. A process for producing a product stream comprising methanol, and a process for upgrading a methanol plant are also provided.

First claim

The invention claimed is:

1 . A methanol plant, said methanol plant comprising:
a first feed comprising CO2 to said plant, a second feed comprising H 2 to said plant, a CO2 shift unit, being an electrically heated Reverse Water Gas Shift unit, and being arranged to receive the first feed and the second feed and provide a first synthesis gas stream, a water removal unit arranged to remove water from said first synthesis gas stream and provide a second synthesis gas stream, a methanol synthesis section, arranged to receive at least a portion of said second synthesis gas stream, and—optionally—a portion of said second feed and/or said first feed, and provide a product stream comprising methanol and an off-gas stream.

2 . The methanol plant according to claim 1 , wherein a compressor is located between the water removal unit and the methanol synthesis section, and arranged to compress said second synthesis gas stream and provide a compressed second synthesis gas stream to the methanol synthesis section.

3 . The methanol plant according to claim 1 , wherein the first feed and the second feed are combined to a combined feed prior to being fed to the CO2 shift unit.

4 . The methanol plant according to claim 1 , wherein the water removal unit is a flash separation unit.

5 . The methanol plant according to claim 1 , wherein at least a portion of the off-gas stream from the methanol synthesis section is arranged to be fed to the inlet of the CO2 shift unit.

6 . The methanol plant according to claim 3 , further comprising a feed compressor, wherein the feed compressor is arranged to receive the first feed, the second feed or the combined feed and to output a compressed stream, upstream the CO2 shift unit.

7 . The methanol plant according to claim 1 , further comprising a first heat exchanger, arranged to cool the first synthesis gas stream from the CO2 shift unit to provide a cooled first synthesis gas stream.

8 . The methanol plant according to any one of the preceding claim 1 , further comprising a feed-effluent heat exchanger, arranged to receive the compressed stream from the feed compressor and heat it to a heated stream in heat exchange with the first synthesis gas stream or the cooled first synthesis gas stream, which is cooled to form a further cooled first synthesis gas stream.

9 . The methanol plant according to claim 8 , further comprising an additional heat exchanger arranged downstream the feed-effluent heat exchanger and arranged to cool the further cooled first synthesis gas stream.

10 . The methanol plant according to claim 1 , further comprising a hydrogen recovery unit arranged to receive at least a portion of the off-gas stream from the methanol synthesis section and to output a hydrogen rich gas stream and a reject stream.

11 . The methanol plant according to claim 1 , further comprising a low pressure separator arranged to receive at least a portion of the product stream comprising methanol from the methanol synthesis section and to output a purified methanol stream and a carbon-rich stream).

12 . The methanol plant according to claim 1 , further comprising a methanol distillation section arranged to receive at least a portion of the product stream comprising methanol from the methanol synthesis section or at least a portion of the purified methanol stream from the low pressure separator and to output a high-purity methanol stream and a higher alcohols stream.

13 . The methanol plant according to claim 12 , wherein at least a portion of the heat required for the methanol distillation section is arranged to be provided from the first heat exchanger.

14 . A process for producing a product stream comprising methanol, in a methanol plant according to claim 1 , said process comprising the steps of:
providing the methanol plant, supplying first feed and second feed to the CO2 shift unit, and providing a first synthesis gas stream, supplying the first synthesis gas stream to the water removal unit and removing water from said first synthesis gas stream so as to provide a second synthesis gas stream, supplying at least a portion of said second synthesis gas stream, and—optionally—a portion of said second feed and/or said first feed, to the methanol synthesis section, and providing a product stream comprising methanol and an off-gas stream.

15 . The process according to claim 14 , wherein said first feed additionally comprises up to 20%, such as up to 10% hydrocarbons.

16 . The process according to claim 15 , wherein said first feed additionally comprises steam.

17 . A process for retrofitting a carbon dioxide-to-methanol plant, said plant comprising:
a first feed comprising CO2 to said plant, and a second feed comprising H2 to said plant; or a combined feed comprising CO2 and H2 to said plant; a methanol synthesis section; wherein said retrofitting process comprises the steps of: incorporating a CO2 shift unit, being an electrically heated Reverse Water Gas Shift unit, and a water removal unit in said plant, upstream said methanol synthesis section, arranging at least a portion of said first feed and said second feed, or of said combined feed comprising CO2 and H2, to be supplied to the CO2 shift unit so as to provide a first synthesis gas stream, feeding at least a portion of said first synthesis gas stream from the CO2 shift unit to the water removal unit, to remove water from said first synthesis gas stream and provide a second synthesis gas stream, arranging at least a portion of the second synthesis gas stream to be supplied to a compressor and compressing it, so as to provide a compressed second synthesis gas stream, arranging at least a portion of the compressed second synthesis gas stream to be supplied to the methanol synthesis section, and providing a product stream comprising methanol.

18 . The process according to claim 17 , wherein said carbon dioxide-to-methanol plant comprises a compressor, wherein—before the retrofitting process—said compressor is arranged to compress the combined feed, and wherein—after said retrofitting process—said compressor is arranged to compress at least a portion of the second synthesis gas stream and provide a compressed second synthesis gas stream.

19 . The process according to claim 17 , wherein said combined feed also comprises hydrocarbons.

20 . The process according to claim 19 , said combined stream is obtained by mixing a biogas with hydrogen.

21 . The process according to claim 17 , wherein said methanol synthesis section of said carbon dioxide-to-methanol plant remains unchanged under said retrofitting process.

22 . The process according to claim 21 , wherein the production of methanol from the carbon dioxide-to-methanol plant after the retrofitting process is at least 10% higher, 20% higher, 33% higher, 50% higher, 100% higher or 250% higher than the methanol production from the carbon dioxide-to-methanol plant prior to the retrofitting process, when evaluated on the flow of methanol molecules from the methanol synthesis section.

23 . The process according to claim 17 , wherein the methanol synthesis section comprises a recycle compressor, a heat exchanger, a flash separation vessel, and/or a cooling unit, wherein said refitting process further comprises one or more further steps of upgrading one or more of said recycle compressor, heat exchanger, flash separation vessel and cooling unit.

24 . The process according to clai

Assignees

• Topsoe As

Inventors

• Mortensen Peter Mølgaard
• Hansen John Bøgild
• Jørgensen Mathias
• Eskesen Søren Grønborg

Classifications

• C07C29/152

  characterised by the reactor used · CPC title

• C01B3/02

  Production of hydrogen; Production of gaseous mixtures containing hydrogen · CPC title

• B01J2219/00103

  in a heat exchanger separate from the reactor · CPC title

• B01J2219/00024

  Revamping, retrofitting or modernisation of existing plants · CPC title

• B01J19/245

  placed in series · CPC title