EP2856050B1 - Vorrichtung und verfahren zur kryogenen trennung einer mischung aus kohlenmonoxid und methan plus wasserstoff und gegebenenfalls stickstoff - Google Patents

Vorrichtung und verfahren zur kryogenen trennung einer mischung aus kohlenmonoxid und methan plus wasserstoff und gegebenenfalls stickstoff Download PDF

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Publication number
EP2856050B1
EP2856050B1 EP13727260.5A EP13727260A EP2856050B1 EP 2856050 B1 EP2856050 B1 EP 2856050B1 EP 13727260 A EP13727260 A EP 13727260A EP 2856050 B1 EP2856050 B1 EP 2856050B1
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Prior art keywords
column
methane
liquid
carbon monoxide
mixture
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EP13727260.5A
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English (en)
French (fr)
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EP2856050A2 (de
Inventor
Pascal Marty
Jean-Jacques Talbot
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Priority to PL13727260T priority Critical patent/PL2856050T3/pl
Publication of EP2856050A2 publication Critical patent/EP2856050A2/de
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0223—H2/CO mixtures, i.e. synthesis gas; Water gas or shifted synthesis gas
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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    • F25J3/0276—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of H2/N2 mixtures, i.e. of ammonia synthesis gas
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    • F25J2200/30—Processes or apparatus using separation by rectification using a side column in a single pressure column system
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    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
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    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—Nitrogen
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J2215/04—Recovery of liquid products
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    • F25J2290/42—Modularity, pre-fabrication of modules, assembling and erection, horizontal layout, i.e. plot plan, and vertical arrangement of parts of the cryogenic unit, e.g. of the cold box

Definitions

  • the present invention relates to an apparatus and method for cryogenic separation of a mixture of carbon monoxide, methane and hydrogen and optionally nitrogen.
  • An object of the invention is to make more compact an apparatus for cryogenic separation of a mixture of carbon monoxide, hydrogen and methane when the methane is to be produced under pressure.
  • Another aim of the invention is, in certain cases, to reduce the maximum height of an apparatus for cryogenic separation of a mixture of carbon monoxide, hydrogen and methane. This makes it possible to reduce the cost of the apparatus as well as the transport costs.
  • the liquid methane withdrawn from the bottom of the CO / CH 4 column can be pressurized in a pump to then be stored and / or sent to a customer or to be sent to the head of the methane washing column, if necessary.
  • the Figure 1 represents a methane washing process according to the prior art
  • the Figures 2 and 3 represent methane washing processes according to the invention
  • the Figure 4 represents a partial condensation process according to the prior art
  • the Figure 5 represents a partial condensation process according to the invention
  • the Figure 6 represents a carbon monoxide washing process according to the prior art
  • the Figure 7 represents a carbon monoxide washing process according to the invention
  • the Figure 8 shows a nitrogen washing process according to the prior art
  • the Figure 9 represents a nitrogen washing process according to the invention.
  • a mixture of hydrogen, carbon monoxide and methane 1 is purified in unit 3 to remove water and carbon dioxide.
  • the purified mixture 5 cools in the main cryogenic exchanger 9 to be sent to a phase separator 7, where it is separated to form a gas 11 enriched in hydrogen and a liquid 13 enriched in methane.
  • the gas 11 separates in a methane washing column 17 fed at the top with a washing liquid 41 rich in methane.
  • the bottom liquid of column 17 is mixed with liquid 13 to form liquid 18 rich in CO and CH 4 and also containing nitrogen sent to the top of a stripping column 19 (in English "flash column") having a bottom reboiler 22.
  • the gas 21 withdrawn from the top of the column 19 is enriched in hydrogen and is heated in the exchanger 9 for upgrading as purge gas to a fuel network in general.
  • the bottom liquid 23 of column 19 mainly contains carbon monoxide (and nitrogen) and methane and is expanded in valve 25 and then sent for separation in CO / CH 4 column 27.
  • a gas 44 enriched in carbon monoxide is formed at the top of the column and a liquid enriched in methane 33 is formed at the bottom of the column.
  • the liquid 33 is divided into two, a part 37 being heated (or not) in the main cryogenic exchanger 9 for upgrading as purge gas (or in liquid form by bypassing the exchanger 9) at the pressure of the CO / column.
  • CH 4 (a few bars) and the other part 35 being pressurized by a pump 36 to supply the head of the washing column with methane 17 and for possible upgrading under pressure (fluid 38) in gaseous form via the main cryogenic exchanger 9 (or directly in liquid form by short-circuiting exchanger 9).
  • a carbon monoxide cycle keeps the device cold.
  • the carbon monoxide coming from the top of the column 27 is heated in the exchanger 9, sent as flow 45 to a compressor 51.
  • Part of the carbon monoxide is produced as gas 53 under pressure at the outlet of the compressor.
  • Another part 57 cools in the exchanger 9 and is divided into two.
  • a part 59 at an intermediate temperature of the exchanger 9 is expanded in a turbine 61 and sent by a valve 63 via line 65 to the compressor 51.
  • Another part 67 continues to cool in the exchanger 9.
  • a fraction 69 of the cooled carbon monoxide is used to heat the tank reboiler 22 of the tank. exhaustion column 19 and is condensed.
  • Another fraction 71 is used to heat the bottom reboiler 31 of the CO / CH 4 column 27 and is mixed with the condensed fraction 69.
  • the entire flow 73 is expanded in a valve 73 and sent to the top condenser 29 of the CO column. / CH 4 where it vaporizes to form the flow of carbon monoxide 43 which mixes with the overhead gas from the CO / CH 4 column.
  • phase separator 79 Part of the liquid 77 from the overhead condenser 29 is sent to a phase separator 79. From the phase separator 79 a liquid 81 is withdrawn which is sent to the exchanger 21 which cools the intermediate withdrawals from the methane washing column, the liquid 81 vaporizes therein and the gas is returned to the phase separator 79. The gas 83 from the phase separator 79 is sent to the inlet of the compressor 51 with the gas 43.
  • the three columns 17, 27, 19 are all placed on the ground, which increases the grip (the size) on the ground.
  • the column 27 is raised to a sufficient height.
  • the CO / CH 4 column 27 is placed above the exhaustion column 19, the two columns having the same main axis.
  • the liquid enriched in methane 33 from the bottom of the column 27 passes through a height H to reach the pump 36 and is at a higher pressure because of the hydrostatic pressure. Part of the liquid at the elevated pressure can be taken to serve as a product downstream or upstream of the pump 36.
  • the footprint of the columns of the cold box is thus reduced.
  • the sum of the heights of the two columns 27 and 19 is less than the height of the column 17, the length of the package of the columns of the cold box is not modified.
  • the stripping column comprises a few additional trays at the top of the column, constituting an auxiliary column 20 of reduced diameter compared to column 19.
  • the gas phase is washed with countercurrent with liquid methane 39 to extract the still dissolved carbon monoxide.
  • the liquid / vapor traffic in this section 20 is quite low: all the other gas flows entering the stripping column 19 are located below the section 20.
  • it is therefore justified to reduce the diameter in the upper section 20 of the exhaustion column: it then takes the name of “auxiliary column” (minaret).
  • the auxiliary column 20 is integrated for approximately one meter in the exhaustion column 19.
  • a mixture of hydrogen, carbon monoxide and methane 1 is purified in unit 3 to remove water and carbon dioxide.
  • the purified mixture 5 cools in a main cryogenic exchanger 9 to be sent to a phase separator 7, where it is separated to form a gas 11 enriched in hydrogen and a liquid 13 enriched in methane.
  • the liquid 13 is sent to the top of a stripping column 19 having a bottom reboiler 22.
  • the gas 21 withdrawn from the top of the column 19 is enriched in hydrogen and is heated in the exchanger 9 for upgrading as gas. purge to a fuel network in general.
  • the bottom liquid 23 of column 19 mainly contains carbon monoxide and methane and is sent to separate in the CO / CH 4 column 27.
  • a gas enriched in carbon monoxide is formed at the top of the column and an enriched liquid.
  • methane 33 is formed at the bottom of the column.
  • the liquid 35 is heated in the exchanger to serve as fuel.
  • the liquid 33 is divided into two, a part 37 being heated (or not) in the exchanger main cryogenic 9 for recovery as purge gas (or in liquid form by short-circuiting the exchanger 9) at the pressure of the CO / CH 4 column (a few bars) and the other part 35 being pressurized by a pump 36 for possible recovery under pressure (fluid 38) in gaseous form via the main cryogenic exchanger 9 (or directly in liquid form by bypassing the exchanger 9).
  • a carbon monoxide cycle keeps the device cold.
  • the carbon monoxide coming from the top of the column 27 is heated in the exchanger 9, sent as flow 45 to a compressor 51.
  • Part of the carbon monoxide is produced as gas 53 under pressure at the outlet of the compressor.
  • Another part 57 cools in the exchanger 9 and is divided into two.
  • a part 59 at an intermediate temperature of the exchanger 9 is expanded in a turbine 61 and sent by a valve 63 via the line 65 to the compressor 51.
  • Another part continues its cooling in the exchanger 9.
  • a fraction 69 of the monoxide of cooled carbon serves to heat the bottom reboiler 22 of column 19 and is condensed.
  • Another fraction 71 is used to heat the bottom reboiler 31 of the CO / CH 4 column 27 and is mixed with the condensed fraction 69.
  • the entire flow 73 is expanded in a valve and sent to the top condenser 29 of the CO / column. CH 4 where it vaporizes to form the flow of carbon monoxide 43 which will feed the compressor 51 after passing through the exchanger 9.
  • column 27 is positioned above column 19, which is itself positioned above phase separator 7. It is also possible to place phase separator 7 next to two columns 19, 27.
  • a mixture of hydrogen, carbon monoxide, nitrogen and methane 1 is purified in unit 3 to remove water and carbon dioxide.
  • the purified mixture 5 cools in an exchanger 9 to be sent to a phase separator 7, where it is separated to form a gas 11 enriched in hydrogen and a liquid 13 enriched in methane.
  • Gas 11 separates in a carbon monoxide washing column 601 fed at the top with a washing liquid 623 rich in carbon monoxide.
  • the bottom liquid of the column 601 is mixed with the liquid 13 to form the liquid 18 and the liquid formed is sent to the top of a stripping column 19 (in English “flash column”) having a bottom reboiler 22.
  • the gas 21 withdrawn from the top of column 19 is enriched in hydrogen and is heated in exchanger 9 for upgrading as purge gas to a fuel network in general ....
  • the bottom liquid 23 of column 19 mainly contains carbon monoxide and methane and is sent to separate in the CO / CH 4 column 27.
  • a gas enriched in carbon monoxide 43 is formed at the top of the column and a liquid.
  • enriched in methane 33 is formed at the bottom of the column.
  • the liquid 33 is divided into two, a part 37 being heated (or not) in the main cryogenic exchanger 9 for upgrading as purge gas (or in liquid form by short-circuiting the exchanger 9) at the pressure of the column CO / CH 4 27 (a few bars) and the other part 35 being pressurized by a pump 36 for possible recovery under pressure (fluid 38), in gaseous form via the main cryogenic exchanger 9 (or directly in liquid form in short- circuiting the exchanger 9).
  • a carbon monoxide cycle keeps the device cold.
  • the carbon monoxide coming from the top of the column 27 is heated in the exchanger 9, sent as flow 45 to a compressor 51.
  • Part of the carbon monoxide is produced as gas 53 under pressure at the outlet of the compressor.
  • Another part 57 cools in the exchanger 9 and is divided into two.
  • a part 59 is expanded in a valve 63 then sent through line 65 to the compressor 51.
  • Another part is divided into two fractions.
  • a fraction 69 of the cooled carbon monoxide serves to heat the bottom reboiler 22 of the stripping column 19 and is condensed.
  • Another fraction 71 is used to heat the bottom reboiler 631 of the CO / CH 4 column 27 and is mixed with the condensed fraction 71.
  • the entire flow 73 is expanded in a valve and sent to the overhead condenser 619 of the CO / column. CH 4 where it vaporizes to form the carbon monoxide fluid 43.
  • a carbon monoxide bath 29 at the top of column 27 supplies condenser 619 with gas to be condensed.
  • the overhead gas 635 from the column 27 is sent to the denitrogenation column 603 having an overhead condenser 615.
  • the bottom liquid 613 from the denitrogenation column 603 is sent to the denitrogenation column 603.
  • the overhead gas enriched in nitrogen 617 is heated in the exchanger 9 and directed to a network fuel.
  • the carbon monoxide necessary for washing in column 603 is provided by the fluids 609 and 611 withdrawn from the discharge of the compressor 51. A portion of these fluids is sent as flow 623 to the head of the washing column 601.
  • the installation of A denitrogenation column can be applicable in all the cases mentioned above when the nitrogen must be partially or totally removed from the gas produced.
  • the CO / CH 4 column 27 is positioned above the stripping column 19 so that the flow rate rich in liquid methane 35 is hydrostatically pressurized upstream of the pump 36.
  • the Figure 8 shows a nitrogen washing process in which a mixture of hydrogen, carbon monoxide, nitrogen and methane 1 leaves a unit of the Rectisol ® 804 type and is purified in a purification unit 3 for remove the water, the methanol and the CO 2 (adsorbing the methanol or any other solvent used in an upstream wash may also be required in all the cases mentioned above).
  • the purified mixture 5 is cooled in the exchanger 9 and then sent to a phase separator 7.
  • the gas from the phase separator 7 is mixed with an uncooled part 6 of the gas 5 to form the flow 11. Part of the flow 11 is used to reheat the bottom reboiler 851 of an N 2 / CH 4 850 column, being partially condensed.
  • the partially condensed flow is sent to a phase separator 809.
  • the liquid 819 from the separator 809 is rich in methane and is sent to the pump 36.
  • the gas 827 from the separator 809 joins gas 821 from separator 7, is cooled in exchanger 9, then separated in a phase separator 807 and the product gas 814 feeds the washing column with nitrogen 811 to be separated.
  • Column 811 is fed at the top with a flow of liquid 833 produced by the liquefaction of a flow 831 of gaseous nitrogen in exchanger 9. Another part 835 of the condensed nitrogen is mixed with the heated top gas 829.
  • the bottom liquid 847 of the nitrogen washing column 811 is expanded, then sent to a phase separator 845.
  • the product gas 853 is heated in the exchanger 9 as purge gas.
  • the fluid 849 feeds the column N 2 / CH 4 850 852 to form a gas flow depleted in methane and enriched in nitrogen and a liquid stream enriched in methane.
  • the liquid flow enriched in methane 35 is sent to the pump 36, then feeds a phase separator 821.
  • the gas 825 is sent to the exchanger 9 to produce a gas phase rich in methane.
  • the liquid 823 can either also be sent to the exchanger 9 to produce a phase rich in gaseous methane under pressure, or bypass the exchanger 9 to produce liquid methane under pressure as a final product. It is also possible to produce a phase rich in gaseous or liquid methane at low pressure by vaporizing liquid taken upstream of the pump 36.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Gas Separation By Absorption (AREA)

Claims (15)

  1. Vorrichtung zur kryogenen Trennung eines Gemischs (5) aus Methan, Kohlenmonoxid und Wasserstoff und eventuell Stickstoff, umfassend eine erste Trennungseinheit umfassend mindestens eine erste Kolonne (19, 811) und eventuell einen Phasentrenner (7, 807, 809, 821, 845), wobei die erste Trennungseinheit durch das Gemisch (5, 814) versorgt wird, eine erste Leitung zur Ausleitung eines mit Wasserstoff und eventuell Stickstoff angereicherten Gases (21, 829) aus der ersten Einheit, eine zweite Leitung zur Ausleitung einer Flüssigkeit (23, 847, 849), die Methan und Kohlenmonoxid enthält, aus der ersten Kolonne oder dem Phasentrenner, eine zweite Kolonne (27, 850), die mit der zweiten Leitung verbunden ist, eine dritte Leitung, die mit dem Tank der zweiten Kolonne verbunden ist, um eine mit Methan angereicherte Flüssigkeit (33) abzuziehen, und eine vierte Leitung, die mit dem Kopf der zweiten Kolonne verbunden ist, um ein mit Kohlenmonoxid und eventuell Stickstoff angereichertes Gas (43, 852) abzuziehen, wobei die zweite Kolonne einen Tankverdampfer (31) umfasst, wobei die Vorrichtung kein Mittel zum Leiten von Kopfgas der ersten Kolonne aufweist, um den Tankverdampfer der zweiten Kolonne zu erhitzen, und die zweite Leitung eine Leitung ist, die mit dem Tank der ersten Kolonne verbunden ist, dadurch gekennzeichnet, dass die erste Kolonne unter der zweiten Kolonne angeordnet ist, die beiden Kolonnen dieselbe Hauptachse aufweisen, so dass die mit Methan angereicherte Flüssigkeit (33) bei einem höheren Druck als der Druck des Tanks der zweiten Kolonne erzeugt wird, und die mit Methan angereicherte Flüssigkeit wenigstens teilweise durch hydrostatischen Druck bei dem höheren Druck erzeugt wird.
  2. Vorrichtung nach Anspruch 1, umfassend eine Pumpe (36), die mit der dritten Leitung verbunden ist, die näher am Boden angeordnet ist als der Tank der zweiten Kolonne (27, 850).
  3. Vorrichtung nach Anspruch 2, umfassend eine Hilfskolonne (20), deren Kopf eventuell mit der Pumpe (36) verbunden ist und deren Tank durch Mittel zum Leiten des Gases aus dem Kopf der ersten Kolonne zum Tank der Hilfskolonne und durch Mittel zum Leiten der Flüssigkeit aus dem Tank der Hilfskolonne zum Kopf der ersten Kolonne mit dem Kopf der ersten Kolonne (19, 811) verbunden ist, wobei die Hilfskolonne eventuell neben der ersten Kolonne angeordnet ist.
  4. Vorrichtung nach Anspruch 3, wobei die Hilfskolonne (20) so angeordnet ist, dass ihr Tank weiter vom Boden entfernt ist als der Kopf der ersten Kolonne (19) .
  5. Vorrichtung nach Anspruch 3 oder 4, wobei die Hilfskolonne (20) an der zweiten Kolonne (27) befestigt ist, oder die erste Einheit eine Vorbehandlungskolonne (17), eine Leitung zum Zuführen des Gemischs aus der Vorbehandlungskolonne zur ersten Kolonne, umfasst, wobei die Hilfskolonne an der Vorbehandlungskolonne befestigt ist, oder die Vorrichtung eine Nachbehandlungskolonne stromab der zweiten Kolonne umfasst, wobei die Hilfskolonne an der Nachbehandlungskolonne befestigt ist.
  6. Vorrichtung nach einem der Ansprüche 2 bis 5, wobei die erste Einheit eine Methanwaschkolonne (17) umfasst, wobei diese Kolonne mit der ersten Kolonne (19) verbunden ist, um sie mit dem Gemisch zu versorgen, das eine Tankflüssigkeit der Methanwaschkolonne ist, wobei der Kopf der Methanwaschkolonne mit der Pumpe (36) verbunden ist.
  7. Vorrichtung nach einem der Ansprüche 1 bis 5, wobei die erste Einheit einen Phasentrenner (7) und Mittel zum Zuführen von Flüssigkeit aus dem Phasentrenner, wie das Gemisch, das die erste Kolonne versorgt, umfasst.
  8. Vorrichtung nach einem der Ansprüche 1 bis 5, wobei die erste Einheit eine Waschkolonne (601), wobei die Waschflüssigkeit reich an Kohlenmonoxid ist, sowie Mittel zum Leiten der Tankflüssigkeit aus der Waschkolonne zur ersten Kolonne (19) umfasst.
  9. Vorrichtung nach einem der vorhergehenden Ansprüche, umfassend Mittel zum Erzeugung des Flüssigmethans als Endprodukt.
  10. Verfahren zur kryogenen Trennung eines Gemischs aus Methan und Kohlenmonoxid sowie Wasserstoff und eventuell Stickstoff, wobei eine erste Trennung des Gemischs mithilfe mindestens einer ersten Kolonne (19, 811) durchgeführt wird, die durch das Gemisch versorgt wird, um ein Fluid (23, 847, 849), das mit Methan angereichert ist und Kohlenmonoxid und eventuell Stickstoff enthält, und ebenfalls ein Gas, das mit Wasserstoff (21, 829) angereichert ist, zu erzeugen, das Fluid in einer zweiten Kolonne (27, 850) getrennt wird, um ein mit Kohlenmonoxid (45) und eventuell mit Stickstoff angereichertes Gas, und eine mit Methan angereicherte Flüssigkeit (35, 37) zu erzeugen, wobei die zweite Kolonne einen Tankverdampfer (31) umfasst, der von einem anderen Gas (71) als ein Kopfgas der ersten Kolonne erhitzt wird, und das mit Methan angereicherte Fluid aus dem Tank der ersten Kolonne stammt, dadurch gekennzeichnet, dass die erste Kolonne unter der zweiten Kolonne angeordnet ist, wobei die beiden Kolonnen dieselbe Hauptachse aufweisen, so dass die mit Methan angereicherte Flüssigkeit wenigstens teilweise durch hydrostatischen Druck auf einen höheren Druck als der Druck des Tanks der zweiten Kolonne gebracht wird.
  11. Verfahren nach Anspruch 10, wobei der Tankverdampfer (31) durch ein Zyklusgas (71) erhitzt wird, das das Kohlenmonoxid ist.
  12. Verfahren nach einem der Ansprüche 10 und 11, wobei sich ein Kopfgas (21) der ersten Kolonne (19) in einem Austauscher (9) erhitzt, wo sich das Gemisch abkühlt.
  13. Verfahren nach Anspruch 12, wobei sich jedes Kopfgas (21) der ersten Kolonne im Austauscher (9) erhitzt.
  14. Verfahren nach einem der Ansprüche 10 bis 13, wobei die mit Methan angereicherte Flüssigkeit (35) zum Teil durch eine Pumpe (36) mit Druck beaufschlagt wird, die näher am Boden angeordnet ist als der Tank der zweiten Kolonne (27).
  15. Verfahren nach Anspruch 14, wobei sich die Pumpe (36) am Boden befindet.
EP13727260.5A 2012-05-31 2013-05-06 Vorrichtung und verfahren zur kryogenen trennung einer mischung aus kohlenmonoxid und methan plus wasserstoff und gegebenenfalls stickstoff Active EP2856050B1 (de)

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PCT/FR2013/051003 WO2013178901A2 (fr) 2012-05-31 2013-05-06 Appareil et procédé de séparation cryogénique d'un mélange de monoxyde de carbone et de méthane ainsi que d'hydrogène et/ou d'azote

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US11137204B2 (en) * 2016-08-25 2021-10-05 Praxair Technology, Inc. Process and apparatus for producing carbon monoxide
FR3057942B1 (fr) * 2016-10-21 2019-12-27 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de separation cryogenique d’un gaz de synthese par condensation partielle
FR3079288B1 (fr) * 2018-03-21 2020-05-22 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de separation d'un gaz de synthese par distillation cryogenique
SG11202008918SA (en) * 2018-03-21 2020-10-29 Air Liquide Method and appliance for separating a synthesis gas by cryogenic distillation
CN108332510A (zh) * 2018-03-22 2018-07-27 上海华林工业气体有限公司 一种提高HyCO冷箱CO回收率的系统及方法
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FR2991442B1 (fr) 2018-12-07
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FR2991442A1 (fr) 2013-12-06
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