METHOD AND INSTALLATION FOR CRYOGENIC SEPARATION OF A GASEOUS MIXTURE BY METHANE SCRUBBING

Abstract

In a process for the combined production of a) a hydrogen-enriched gas and a carbon monoxide-enriched gas and/or b) a mixture of hydrogen and carbon monoxide by cryogenic distillation and scrubbing, a still liquor is extracted from a scrubbing column and sent to a stripping column, a still liquor is extracted from the stripping column and sent to a separating column for carbon monoxide and methane and a cooling fluid is used at a pressure greater than that of the head of the separating column for cooling at least one fluid extracted at an intermediate level from the scrubbing column.

Claims

1-15. (canceled)

16. A process for the combined production a) of a hydrogen-enriched gas and a carbon monoxide-enriched gas and/or b) a mixture of hydrogen and carbon monoxide and optionally methane by cryogenic distillation and scrubbing, in which: a. a gaseous mixture containing at least hydrogen, carbon monoxide and methane and optionally nitrogen is cooled in a heat exchanger b. the cooled mixture is sent to a scrubbing column c. a methane-rich liquid is introduced into the scrubbing column as scrubbing liquid d. a hydrogen-enriched gas is drawn off as top gas from the scrubbing column e. a vessel liquid is drawn off from the scrubbing column and sent to a stripping column f. a vessel liquid is drawn off from the stripping column and sent to a column for separating carbon monoxide and methane g. at least a portion of the vessel liquid from the separation column constitutes the liquid of step iii), and h. a carbon monoxide-rich fluid is used as coolant fluid for cooling at least one fluid drawn off at an intermediate level of the scrubbing column wherein the fluid serving to cool the at least one fluid drawn off at an intermediate level of the scrubbing column is at a greater pressure than that of the top of the separation column, and in that the fluid having served to cool the at least one fluid drawn off at an intermediate level of the scrubbing column is sent to an intermediate level of a centrifugal compressor in order to be compressed therein.

17. The process as claimed in claim 16, wherein the fluid serving to cool at least one fluid drawn off at an intermediate level of the scrubbing column is drawn off from the top of the separation column or from a volume located at the top of the separation column, and/or a carbon monoxide-enriched gas originating from the separation column is compressed to form carbon monoxide at a higher pressure, and at least a portion of the carbon monoxide at higher pressure is reduced in pressure to form the coolant fluid.

18. The process as claimed in claim 16, wherein liquid from a volume located at the top of the separation column is reduced in pressure and sent to the separation column.

19. The process as claimed in claim 16, wherein the pressure difference between the fluid serving to cool at least one fluid drawn off from an intermediate level of the scrubbing column and that of the top of the separation column is at least 0.5 bar.

20. The process as claimed in claim 16, wherein the pressure difference between the fluid serving to cool at least one fluid drawn off from an intermediate level of the scrubbing column and that of the top of the separation column is at least 0.9 bar.

21. The process as claimed in claim 16, wherein a portion of the vessel liquid from the separation column is recovered as methane-rich product in liquid form or in gaseous form, after having vaporized it in the heat exchanger.

22. The process as claimed in claim 16, wherein a carbon monoxide-enriched fluid is produced from the separation column, and is mixed with the hydrogen-enriched fluid to form a product.

23. The process as claimed in claim 16, wherein a carbon monoxide-enriched gas heats the vessel of the stripping column and/or the vessel of the separation column and is sent to a volume at the top of the separation column after reduction in pressure in a valve.

24. The process as claimed in claim 16, wherein at least a portion of the carbon monoxide-rich liquid from a volume located at the top of the separation column is reduced in pressure and sent to the top of the separation column to be vaporized on contact with the vapor rising inside the column and is subsequently mixed with a portion of the top gas of the separation column.

25. The process as claimed in claim 16, wherein the separation column is operated at 1.6 bar.

26. The process as claimed in claim 16, wherein a gas from the top of the separation column or from a volume at the top of the separation column is sent to the inlet of the compressor.

27. The process as claimed in claim 16, wherein a carbon monoxide cycle is used to heat the vessels of the stripping column and of the separation column and to cool the top of the separation column, the centrifugal compressor serving to compress the cycle gas.

28. A plant for the combined production a) of a hydrogen-enriched gas and a carbon monoxide-enriched gas and/or b) a mixture of hydrogen and carbon monoxide and optionally methane by cryogenic distillation and scrubbing, comprising a centrifugal compressor, a first heat exchanger, a scrubbing column, a stripping column, a column for separating carbon monoxide and methane, a pipe for sending a gaseous mixture containing at least hydrogen, carbon monoxide and methane to cool in the first heat exchanger, a pipe for sending the cooled liquid from the first heat exchanger to the scrubbing column, a pipe for introducing a methane-rich liquid at the top of the scrubbing column as first scrubbing liquid, a pipe for drawing off a hydrogen-enriched gas as top gas of the scrubbing column, a pipe for drawing off a vessel liquid from the scrubbing column and for sending the vessel liquid of the scrubbing column to the stripping column, a pipe for drawing off a vessel liquid from the stripping column and sending it to the column for separating carbon monoxide and methane, at least a portion of the vessel liquid of the separation column constituting the methane-enriched liquid, and a pipe for drawing off a carbon monoxide-enriched fluid from the top of the separation column, a pipe for sending a carbon monoxide-enriched fluid as coolant fluid for cooling at least one fluid drawn off at an intermediate level of the scrubbing column in a second heat exchanger, wherein the plant comprises means for sending the fluid having served to cool the at least one fluid drawn off at an intermediate level of the scrubbing column, at a pressure greater than that of the top of the separation column, to an intermediate level of the centrifugal compressor.

29. The plant as claimed in claim 28, wherein the compressor is connected to the separation column and comprising means for sending the carbon monoxide-enriched gas originating from the separation column to the centrifugal compressor in order to pressurize this gas such that it can serve as product and cycle gas.

30. The plant as claimed in claim 28, further comprising means for reducing in pressure the gas originating from the centrifugal compressor in order to serve as coolant fluid for the at least one fluid drawn off at an intermediate level of the scrubbing column.

31. The plant as claimed in claim 28, further comprising means for sending a fluid from the top of the separation column to the second heat exchanger as coolant fluid.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0049] Further features, advantages and possible applications of the invention are apparent from the following description of working and numerical examples and from the drawings. All described and/or depicted features on their own or in any desired combination form the subject matter of the invention, irrespective of the way in which they are combined in the claims the way in which said claims refer back to one another.

[0050] FIG. 1 provides a first embodiment of the present invention.

[0051] FIG. 2 provides a second embodiment of the present invention.

[0052] FIG. 3 provides a showing of an embodiment of the cryogenic separation in accordance with an embodiment of the present invention.

[0053] FIG. 4 provides a showing of another embodiment of the cryogenic separation in accordance with an embodiment of the present invention.

DETAILED DESCRIPTION OF THE INVENTION

[0054] The invention will be described in more detail with reference to FIGS. 1 to 4, FIGS. 1 and 2 depicting the overall process and FIGS. 3 and 4 showing the cryogenic separation in particular.

[0055] According to the process of FIG. 1, a flow of synthesis gas at 24 bar containing at least hydrogen, carbon monoxide and methane and optionally nitrogen 1 is purified of water, carbon dioxide, methanol and other impurities in the purification unit 3 and subsequently the flow 5 of dry synthesis gas is sent to a cold box CB which is an insulated chamber containing distillation columns. A product of this system of distillation columns is a purge gas 103. Another 27 is hydrogen HRG, a portion of which serves to regenerate the purification unit. A flow of carbon monoxide 59 at 1.2 bar and another flow of carbon monoxide 43 at 2.2 bar are sent to different levels of the compressor 67 where they are compressed. The flow 43 serves to cool a flow drawn off at an intermediate level of the scrubbing column. A flow of product 69 leaves at an intermediate level of the compressor 67 at less than 22 bar. The rest of the gas is compressed up to the final stage at a pressure of 22 bar and is returned to the cold box CB as flow 61.

[0056] According to the process of FIG. 2, the process does not produce carbon monoxide but a mixture of carbon monoxide and hydrogen formed by mixing a gas 101 drawn off from the methane scrubbing column at an intermediate level containing hydrogen and carbon monoxide and a portion of the compressed gas in the final stage of the compressor 67 at 22 bar. A portion 61 of the gas at 22 bar is returned to the cold box CB and the rest 62 is compressed in a compressor 167 with the flow 101 to form a product 105 containing carbon monoxide and hydrogen at 29 bar.

[0057] According to the process of FIG. 3, a flow of synthesis gas containing at least hydrogen, carbon monoxide and methane and optionally nitrogen 1 is purified of water, carbon dioxide, methanol and other impurities in the purification unit 3 and subsequently the flow 5 of dry synthesis gas is sent to the cold box where it is cooled in the heat exchanger 7, which is preferably a brazed aluminum plate exchanger. The cooled gas is sent to the bottom of a scrubbing column 15. The scrubbing column is suppled at the top with a methane-rich liquid 45 as scrubbing liquid. A hydrogen-enriched gas 27 is drawn off as top gas from the scrubbing column 15 and a vessel liquid 17 is drawn off from the scrubbing column.

[0058] The vessel liquid 17 from the scrubbing column is sent to the middle of a stripping column 31. At least one, preferably several, intermediate liquids 28 are drawn off at intermediate levels of the scrubbing column 51 and sent to be vaporized in the heat exchanger 29. A vessel liquid 35 is drawn off from the stripping column 31 and sent at 1.6 bar to a column for separating carbon monoxide and methane 37 at an intermediate level after cooling. At least a portion 45 of the vessel liquid 41 from the separation column 37 constitutes the scrubbing liquid after pressurization in the pump 46. A carbon monoxide-rich gas 53 is drawn off at the top of the separation column 37. The separation column 37 operates at 1.6 bar and optionally comprises a volume 55 which serves as storage for liquid carbon monoxide at the column top. The gas 53 at 1.6 bar abs is mixed with the gas 57 from the volume, after having reduced in pressure the gas 57 of the volume, from the volume pressure of 2.6 bar abs to 1.6 bar abs. The mixture of the two gases 59 is heated in the exchanger 7 and sent to the inlet of a carbon monoxide compressor 67 to provide the carbon monoxide-rich product 69. A portion 61 of the carbon monoxide at 22 bar abs is cooled in the heat exchanger 7 and divided into two; one portion 63 is reduced in pressure in a turbine 68 to be heated in the exchanger 7 and returned to the compressor 57. The rest 65 at 22 bar abs serves to reboil the columns 31 and 37 and, where appropriate, to supply the volume 55. The carbon monoxide-rich gas 71 which has served to heat the vessels of the columns 31 and 37 is reduced in pressure by 22 bar abs down to the pressure of the volume which is 2.6 bar, to form a biphase flow. Carbon monoxide-enriched liquid accumulates in the volume 55 and is sent through an expansion valve at the top of the separation column through a pipe 73 to reduce in pressure the liquid from 2.6 bar to 1.6 bar, the pressure of the top of the separation column 37.

[0059] There are therefore two CO cycle circuits, 2.6 bar abs and 1.6 bar abs.

[0060] Liquid carbon monoxide 43 from the storage 55 after reduction in pressure serves to cool the intermediate fluids 28 from the scrubbing column 15 at a point below the inlet of the scrubbing liquid. Otherwise, the liquid carbon monoxide 43 may be taken at the top of the CO/CH.sub.4 column 37 and sent to the heat exchanger 29 to cool the intermediate fluids 28.

[0061] A gas 33 leaves the top of the stripping column 31 and a methane-rich product 47 is optionally drawn off from the CO/CH.sub.4 column 37 in liquid form and vaporized in the exchanger 7.

[0062] The gas 33 is mixed with a portion of the methane 45 after reduction in pressure of the latter in a valve. The mixture thus formed is heated and may serve as fuel.

[0063] The gas 43 which has served to cool the intermediate drawing-offs 28 from the scrubbing column is sent at 2.6 bar to an intermediate level of the compressor 67.

[0064] The carbon monoxide-enriched gas 69 serves as product, optionally mixed with another product to form oxogas.

[0065] The pressure difference between the fluid 43 serving to cool at least one intermediate fluid from the scrubbing column 15 and that of the top of the separation column 37 is at least 0.5 bar, or even at least 0.9 bar.

[0066] As an alternative, as illustrated in FIG. 4, a portion 66 of the gas 61 or 69 compressed in the compressor 67 (not illustrated) may be reduced in pressure in a valve V to serve as coolant fluid for at least one fluid 28 drawn off at an intermediate level of the scrubbing column 15 in the exchanger 29. Even after reduction in pressure, this fluid 66 will be at a pressure greater than that of the top of the separation column 37 by at least 0.5 bar, or even at least 0.9 bar.

[0067] The fluid 66 cooled in the heat exchanger 29 is subsequently sent as gas 43 to the compressor 67 at an intermediate level of the latter. It is mixed with the gas 37 originating from the volume 55 and with the vaporized liquid originating from the volume 55.

[0068] Another portion 64 of the fluid reduced in pressure in the valve V is sent to the volume 55 or simply to the top of the column 37 if there is no volume 55.

[0069] The gas 53, 59 originating from the top of the CO/CH.sub.4 column and at lower pressure than the flow 43 is sent to the inlet of the compressor 67.

[0070] The gas 39 produced in the volume 55 mixes with the gas having served to heat the exchanger 29 and is returned to the compressor like the gas 43.

[0071] In this variant, the methane produced 47 has not been pressurized in the pump 46 before being vaporized in the exchanger 7.

[0072] While the invention has been described in conjunction with specific embodiments thereof, it is evident that many alternatives, modifications, and variations will be apparent to those skilled in the art in light of the foregoing description. Accordingly, it is intended to embrace all such alternatives, modifications, and variations as fall within the spirit and broad scope of the appended claims. The present invention may suitably comprise, consist or consist essentially of the elements disclosed and may be practiced in the absence of an element not disclosed. Furthermore, if there is language referring to order, such as first and second, it should be understood in an exemplary sense and not in a limiting sense. For example, it can be recognized by those skilled in the art that certain steps can be combined into a single step.

[0073] The singular forms a, an and the include plural referents, unless the context clearly dictates otherwise.

[0074] Comprising in a claim is an open transitional term which means the subsequently identified claim elements are a nonexclusive listing (i.e., anything else may be additionally included and remain within the scope of comprising). Comprising as used herein may be replaced by the more limited transitional terms consisting essentially of and consisting of unless otherwise indicated herein.

[0075] Providing in a claim is defined to mean furnishing, supplying, making available, or preparing something. The step may be performed by any actor in the absence of express language in the claim to the contrary.

[0076] Optional or optionally means that the subsequently described event or circumstances may or may not occur. The description includes instances where the event or circumstance occurs and instances where it does not occur.

[0077] Ranges may be expressed herein as from about one particular value, and/or to about another particular value. When such a range is expressed, it is to be understood that another embodiment is from the one particular value and/or to the other particular value, along with all combinations within said range.

[0078] All references identified herein are each hereby incorporated by reference into this application in their entireties, as well as for the specific information for which each is cited.