PROCESS AND DEVICE FOR MEMBRANE SEPARATION OF A MIXTURE CONTAINING HYDROGEN AND CARBON DIOXIDE AS MAIN COMPONENTS

Abstract

A process for membrane separation of a mixture containing as main, or even major, components hydrogen and carbon dioxide and also at least one other component, for example chosen from the following group: carbon monoxide, methane and nitrogen, including: heating of the mixture in the heat exchanger, permeation of the reheated mixture in a first membrane separation unit making it possible to obtain a first permeate which is a hydrogen and carbon dioxide enriched relative to the mixture, and a first residue which is hydrogen and carbon dioxide lean, permeation of the first residue in a second membrane separation unit making it possible to obtain a second residue, at least one portion of the first permeate is compressed in a booster compressor and the second residue is expanded in a turbine, the booster compressor being driven by the turbine.

Claims

1. A process for membrane separation of a mixture containing hydrogen and carbon dioxide and also at least one other component chosen from the following group: carbon monoxide, methane and nitrogen, said process comprising: i) heating of the mixture in a heat exchanger up to a first temperature; ii) separating the mixture reheated to the first temperature in a first membrane separation unit thereby obtaining a first permeate which is hydrogen and carbon dioxide enriched relative to the mixture and a first residue which is hydrogen and carbon dioxide lean relative to the mixture; iii) cooling of at least one portion of the first permeate in the heat exchanger; iv) separating the first residue in a second membrane separation unit thereby obtaining a second permeate and a second residue which is hydrogen and carbon dioxide lean relative to the second permeate, and v) cooling at least one portion of the first permeate, in the heat exchanger, compressing the cooled first permeate in a booster compressor, expanding the second residue is expanded in a turbine and the booster compressor is driven by the turbine.

2. The process as claimed in claim 1, wherein at least one portion of the first permeate compressed in the booster compressor is sent to a pressure swing adsorption separation unit in order to extract the hydrogen therefrom.

3. The process as claimed in claim 2, wherein the at least one portion of the first permeate compressed in the booster compressor is cooled in the heat exchanger before being sent to the adsorption separation unit.

4. The process as claimed in claim 1, wherein the mixture is reheated in the exchanger only by at least one flow produced by the membrane separation, or by the first membrane separation unit.

5. The process as claimed in claim 1, wherein the heat exchanger has a first end and a second end, the second end being colder than the first and wherein the at least one portion of the first permeate is cooled up to the second end before being sent to the booster compressor.

6. The process as claimed in claim 1, wherein the inlet temperature of the turbine is substantially equal to the temperature at which the second residue leaves the second membrane separation unit.

7. The process as claimed in claim 1, wherein the reheated mixture enters the first membrane separation unit at a temperature substantially equal to the temperature at which it leaves the heat exchanger.

8. The process as claimed in claim 1, wherein a variable portion of the mixture is not reheated in the heat exchanger and mixes with the reheated mixture upstream of the first membrane separation unit.

9. The process as claimed in claim 8, wherein at least one variable portion of the first permeate from the first membrane separation unit is sent directly to the booster compressor without passing through the heat exchanger.

10. The process as claimed in claim 7, wherein only one portion of the first permeate compressed in the booster compressor is sent to the heat exchanger.

11. The process as claimed in claim 1, comprising a separation step operating at a temperature below 0° C. by distillation and/or by partial condensation in order to produce the mixture to be separated and wherein the cold produced by the expansion in the turbine is used in the separation unit operating at a temperature below 0° C. or in a refrigeration cycle.

12. The process as claimed in claim 1, comprising a separation step operating at a temperature below 0° C. by distillation and/or by partial condensation in order to separate a gas compressed in a compressor and to produce the mixture to be separated.

13. The process as claimed in claim 12, wherein at least one portion of the second permeate is sent to the gas compressor.

14. The process as claimed in claim 12, wherein the gas compressed in the compressor is a residual gas from a pressure swing adsorption hydrogen separation unit.

15. A device for membrane separation of a mixture containing hydrogen and carbon dioxide and also at least one other component chosen from the following group: carbon monoxide, methane and nitrogen, said process comprising: a) a heat exchanger and a means for sending the mixture to heat in the heat exchanger to a first temperature; a) a first membrane separation unit and a means for sending the mixture reheated to the first temperature to the first membrane separation unit in order to obtain a first permeate which is hydrogen and carbon dioxide enriched and a first residue which is hydrogen and carbon dioxide lean; c) at least one pipe for sending at least one portion of the first permeate to cool in the heat exchanger; d) a second membrane separation unit, a pipe for sending the first residue to the second membrane separation unit configured to obtain a second permeate and a second residue which is hydrogen and carbon dioxide lean relative to the second permeate, and e) a booster compressor, a means connected to the heat exchanger for sending at least one portion of the first permeate, cooled in the heat exchanger, to the booster compressor in order to be compressed, a turbine, a means for sending the second residue to expand in the turbine, and the booster compressor being coupled with the turbine in order to be driven by said turbine.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0058] For a further understanding of the nature and objects for the present invention, reference should be made to the following detailed description, taken in conjunction with the accompanying drawings, in which like elements are given the same or analogous reference numbers and wherein:

[0059] FIG. 1 shows a scheme of a comparative process.

[0060] FIG. 2 shows a variant of FIG. 1 according to the invention.

DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0061] In FIG. 1, a gas mixture 1 containing as main, or even major, components hydrogen and carbon dioxide and also at least one other component, for example chosen from the following group: carbon monoxide, methane and nitrogen, is reheated in a heat exchanger E by indirect heat exchange with three flows separated by the separation process, preferably only with these three flows.

[0062] The mixture 1 preferably originates from a PSA-type adsorption unit producing a hydrogen-enriched flow and a flow which is separated in order to form the mixture.

[0063] The reheated flow 3 is reheated even more in a reheater heated for example by steam S. The flow 5 reheated by the reheater is sent to separate in a first membrane separation unit M1. This separation produces a first permeate 7 which is hydrogen and carbon dioxide enriched relative to the mixture and lean with respect to the at least one other component relative to the mixture, and a first residue 9 which is hydrogen and carbon dioxide lean relative to the mixture and enriched with respect to the at least one other component relative to the mixture. The first permeate 7 cools in the heat exchanger E in order to be sent to the PSA. The first residue 9 is sent to a second membrane separation unit M2 in order to produce a second permeate 11 which is hydrogen and carbon dioxide enriched and lean with respect to the at least one other component, and a second residue 13 which is hydrogen and carbon dioxide lean and enriched with respect to the at least one other component. The second permeate 11 is in this case more hydrogen and/or carbon dioxide rich than the first permeate 7, and the second residue 13 is less hydrogen and/or carbon dioxide rich than the first residue 9. Or else, the second permeate 11 may be more hydrogen and/or carbon dioxide lean than the first permeate 7, and the second residue 13 is more hydrogen and/or carbon dioxide rich than the first residue 9,

[0064] The second permeate 11 is more hydrogen and carbon dioxide rich than the second residue 13.

[0065] The second permeate 11 cools in the heat exchanger E and is sent to a compressor. This compressor can for example compress a flow intended to be separated by low-temperature separation (distillation and/or partial condensation) in order to produce the gas 1.

[0066] The second residue 13 is expanded, and can be used to regenerate a dryer, then it is optionally sent as fuel to a hydrogen production unit, for example upstream of the adsorption unit.

[0067] In FIG. 2, a gas mixture 1 containing as main, or even major, components hydrogen and carbon dioxide and also at least one other component, for example chosen from the following group: carbon monoxide, methane and nitrogen, is reheated in a heat exchanger E by indirect heat exchanger with two flows separated by the separation process, preferably only with these two flows.

[0068] The mixture 1 preferably originates from a PSA-type adsorption unit producing a hydrogen-enriched flow and a flow which is separated by distillation and/or partial condensation in order to form the mixture 1.

[0069] The reheated flow 1 is sent to separate in a first membrane separation unit M1. This separation produces a first permeate 7 which is hydrogen and carbon dioxide enriched and lean with respect to at least one other component, and a first residue 9 which is hydrogen and carbon dioxide lean and enriched with respect to the at least one other component. At least one portion of the first permeate 7 (in this case the entire first permeate) is sent to a booster compressor C. Optionally, at least one portion of the first permeate cools in the heat exchanger E upstream of the booster compressor C. The boosted flow 17 is cooled in the exchanger E.

[0070] The first residue 9 is sent to a second membrane separation unit M2 in order to produce a second permeate 11 which is hydrogen and carbon dioxide enriched and lean with respect to the at least one other component, and a second residue 13 which is hydrogen and carbon dioxide lean and enriched with respect to the at least one other component.

[0071] The second permeate 11 may be more hydrogen and/or carbon dioxide rich than the first permeate 7, and the second residue 13 may be less hydrogen and/or carbon dioxide rich than the first residue 9. Or else, the second permeate 11 may be more hydrogen and/or carbon dioxide lean than the first permeate 7, and the second residue 13 may be less hydrogen and/or carbon dioxide lean than the first residue 9.

[0072] The second permeate 11 is more hydrogen and carbon dioxide rich than the second residue 13.

[0073] The second permeate 11 is sent to a compressor of a flow from which the gas 1 is derived by low-temperature separation (distillation and/or partial condensation).

[0074] The second residue 13 is sent to a turbine T coupled to the booster compressor C. The flow expanded in the turbine is not cooled here in the exchanger E.

[0075] The second residue 13 expanded in the turbine can be used to regenerate a dryer and/or sent as fuel to a hydrogen production unit, for example a reformer, for example upstream of the adsorption unit.

[0076] The absence of any reheater between the hot end of the exchanger E and the inlet of the separation unit M1 is noted.

[0077] Such a reheater can however be present.

[0078] There is a bypassing pipe 1A which makes it possible to send a portion of the flow 1 from the cold end to the hot end of the exchanger E without passing through the heat exchanger E and thus to arrive at the unit 1 without having been reheated.

[0079] This pipe 1A is fitted with a valve V3 regulated by the inlet temperature of the gas 1 in the unit M1.

[0080] There is also a bypassing pipe 7A between the permeate 7 outlet of the unit M1 and the inlet of the booster compressor C, this pipe being fitted with a valve V2 regulated by the outlet temperature of the booster compressor C and by the inlet temperature of the gas 1 in the unit.

[0081] It is possible to send only one portion of the first permeate compressed in the booster compressor C to the heat exchanger E.

[0082] At least one portion 17 of the first permeate compressed in the booster compressor C can be sent to a pressure swing adsorption unit in order to be separated and to extract the hydrogen therefrom, preferably at substantially the outlet pressure of the booster compressor C.

[0083] The device can comprise, upstream of the membrane separation portion, a separation unit operating at a temperature below 0° C. by distillation and/or by partial condensation in order to produce the mixture to be separated in the membrane separation portion. In this case, the cold produced by the expansion in the turbine T can be used in the separation unit operating at a temperature below 0° C. or in a refrigeration cycle.

[0084] A portion of the second permeate 11 can be sent to the compressor of the low-temperature separation unit.

[0085] In the two examples, the heat exchanger E can be divided into a plurality of heat exchangers.

[0086] It will be understood that many additional changes in the details, materials, steps and arrangement of parts, which have been herein described in order to explain the nature of the invention, may be made by those skilled in the art within the principle and scope of the invention as expressed in the appended claims. Thus, the present invention is not intended to be limited to the specific embodiments in the examples given above.