EP2504646B1 - Verfahren und anlage zur kryogenen trennung einer mischung aus wasserstoff und kohlenmonoxid - Google Patents

Verfahren und anlage zur kryogenen trennung einer mischung aus wasserstoff und kohlenmonoxid Download PDF

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EP2504646B1
EP2504646B1 EP10792965.5A EP10792965A EP2504646B1 EP 2504646 B1 EP2504646 B1 EP 2504646B1 EP 10792965 A EP10792965 A EP 10792965A EP 2504646 B1 EP2504646 B1 EP 2504646B1
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Prior art keywords
liquid
column
carbon monoxide
gas
phase separator
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French (fr)
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EP2504646A2 (de
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Antoine Hernandez
Arthur Darde
Bernard Saulnier
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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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    • 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
    • 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
    • F25J3/0228—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
    • F25J3/0252—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 hydrogen
    • 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
    • F25J3/0228—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
    • F25J3/0257—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 nitrogen
    • 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
    • F25J3/0228—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
    • F25J3/0261—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 carbon monoxide
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • 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
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—Nitrogen
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/24—Quasi-closed internal or closed external carbon monoxide refrigeration cycle
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/34—Details about subcooling of liquids
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/80—Retrofitting, revamping or debottlenecking of existing plant

Definitions

  • the present invention relates to a method and apparatus for cryogenic separation of a mixture of nitrogen and carbon monoxide, according to the preambles of claims 1 and 4 respectively and known from the document DE-A-2,147,465 .
  • the most common cryogenic process is methane scrubbing
  • the residual methane content in the synthesis gas is compatible with the methane washing process.
  • a methane scrubbing scheme with a CO / N 2 column is described in FR-A-2910603 .
  • the synthesis gas produced is treated in a cold box by partial condensation without a cycle, the inert content (CH 4 , Ar and N 2 ) being very low and compatible with the purity of the product. CO.
  • a partial condensation scheme with a CO / N 2 column is described in US-A-4478621 .
  • the reboiling of the column CO / N 2 is provided by a direct supply of CO at medium pressure in the bottom of the column coming from the compressor CO.
  • the apparatus according to the invention is a partial condensation apparatus including a CO / N 2 column with a common integrated cycle for the cooling of the synthesis gas and for the separation energy CO / N 2 .
  • At least a portion of the reboiling energy of the CO / N 2 column is provided by an external reboiler where the feed gas of the CO / N 2 column is condensed totally or partially. This makes it possible to reduce the MPCO flow rate of the cycle compressor and thus reduce the energy of the compressor by about 15%.
  • the process scheme may include a CO / N 2 distillation column alone or a CO / N 2 column with a CO / CH 4 column.
  • This invention can also be applied when it is desired to invest a CO / N 2 separation column treating impure CO coming from a cold box which does not comprise a CO / N 2 column. As the nitrogen content in CO increases over time, it then becomes necessary to add a CO / N 2 separation step. The new column is then installed in a dedicated cold box that must be supplied with frigories and reboiling energy.
  • DE-A-4228784 and DE-A-2147465 describe processes comprising the features of the preamble of claim 1 and similar to that of Figure 1 .
  • a flow of nitrogen and carbon monoxide 1 is cooled in an exchanger 3. It is condensed at least partially in a reboiler 5 fed by the liquid column of the column 15. The vaporized liquid is returned to the column.
  • the at least partially condensed flow rate is expanded in a valve 7 and sent to a phase separator 9. the liquid 11 of the phase separator and the gas 13 of the phase separator 9 are sent to the column at different heights or not.
  • the bottom liquid of the column is expanded in a valve 19 and sent to the head condenser 23 forming part of the column.
  • a nitrogen flow is removed as a purge and heats up in the exchanger 3.
  • the vaporized carbon monoxide 27 also heats up in the exchanger 3 and is compressed in the first stage 29 of a compressor. It is cooled in a cooler 31 by water and then divided in two. The flow 33 cools to an intermediate temperature in the exchanger 3 to form the flow 45 which is sent to the bottom of the column 15. The flow 41 is cooled very partially in the exchanger 3, expanded in a turbine 43 and The remainder of the carbon monoxide is compressed at the product pressure by the compressor stage 37 and cooled by the cooler 31A to form the product flow 39.
  • the stage 29 is all the more small part of the reboil is provided by flow 1.
  • a flow of nitrogen, hydrogen and carbon monoxide 1 is cooled in an exchanger 3 and then in a heat exchanger 3A.
  • the flow 1 is sent to a first phase separator 51 where it separates into a flow rate 53 rich in hydrogen and a liquid flow 57.
  • the flow 53 is heated in the exchangers 3,3A and the flow 57 is expanded in a valve 55 and then sent to a second phase separator 61.
  • the gas of the second separator of phases is heated in the heat exchangers 3,3A to form the flow 77.
  • the liquid 63 is separated in two.
  • a portion 67 is expanded in a valve 69, sent to a phase separator 71 and then the flow rates 73,75 are sent to the distillation column 15.
  • the remainder 65 of the liquid of the separator 61 is heated in the exchanger 3A to forming the flow 65 which serves to heat the reboiler 5 fed by the tank liquid 17 of the column 15. Having served to reboil the column, the flow 65 is expanded in the valve 7, sent to the separator 9 and then to the column of the same way as for the Figure 1 .
  • a nitrogen flow is removed as a purge and heats up in the exchanger 3.
  • the vaporized carbon monoxide 27 also heats up in the exchanger 3 and is compressed in the first stage 29 of a compressor. It is cooled in a cooler 31 by water and then divided in two.
  • the flow 33 cools to an intermediate temperature in the exchanger 3 and is divided in two to form the flow 133.
  • This flow 133 is cooled in the exchanger 135 against liquid nitrogen 137.
  • the liquid nitrogen 137 vaporizes and heats in the exchanger 3.
  • the flow 133 is expanded and mixed with the flow 21 downstream of the valve 19.
  • the flow 45 is sent to the bottom of the column 5 after cooling in the exchanger 3A.
  • the liquid carbon monoxide 79 is withdrawn from the condenser 23, expanded in the valve 81, sent to the phase separator 83 to produce a liquid portion and a gas portion.
  • the liquid portion 85 vaporizes in the exchange line 3A and the gas 87 is mixed with the flow rate of carbon monoxide 27 for the compressor 29.
  • a flow of nitrogen, hydrogen and carbon monoxide 1 is cooled in an exchanger 3 and then in a heat exchanger 3A.
  • the flow 1 is sent to a first phase separator 51 where it separates into a gaseous flow 53 rich in hydrogen and a liquid flow 57.
  • the flow 53 is heated in the exchangers 3,3A and the flow 57 is expanded in a valve 55 and then sent to a second phase separator 61.
  • the gas of the second phase separator heats up in the exchangers 3,3A to form the flow 77.
  • the liquid 63 is separated in two.
  • a portion 67 is expanded in a valve 69, sent to a phase separator 71 and then the flow rates 73,75 are sent to the distillation column 5.
  • the remainder 65 of the liquid of the separator 61 is heated in the exchanger 3A to forming the flow 65 which serves to heat the reboiler 5 fed by the tank liquid 17 of the column 5. Having served to reboil the column the flow 65 is expanded in the valve 7, sent to the separator 9 and then to the column of the same way as for the Figure 1 .
  • a nitrogen flow is removed as a purge and is heated in the exchanger 3.
  • the vaporized carbon monoxide enriched flow 27 also warms up in the exchanger 3 and is compressed in the first stage 29 of a compressor. It is cooled in a cooler 31 by water and then divided in two.
  • the flow 33 cools to an intermediate temperature in the exchanger 3 and is divided in two to form the flow 93.
  • This flow 93 is expanded in the turbine 91 to form the expanded flow 93 which is mixed with the flow 27 for to heat up in the exchanger 3.
  • the flow 45 from the stage 29 is sent to the bottom of the column 5 after cooling in the exchanger 3A.
  • the liquid carbon monoxide 79 is withdrawn from the condenser 23, expanded in the valve 81, sent to the phase separator 83 to produce a liquid portion and a gas portion.
  • the liquid portion 85 vaporizes in the exchange line 3A and the gas 87 is mixed with the flow rate of carbon monoxide 27 for the compressor 29.

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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)

Claims (9)

  1. Verfahren zur Trennung eines Versorgungsgases, das Stickstoff und Kohlenmonoxid und gegebenenfalls Wasserstoff als Hauptkomponenten enthält, in einer Destillationskolonne (15), wobei:
    i) das Versorgungsgas in einem Wärmeaustauscher (3) gekühlt wird
    ii) mindestens ein Teil eines aus dem Versorgungsgas abgeleiteten Gases einem Sumpfverdampfer (5) in der Destillationskolonne zugeführt wird, um durch die Erzeugung einer Flüssigkeit und gegebenenfalls eines Gases zumindest teilweise kondensiert zu werden
    iii) mindestens ein Teil der Flüssigkeit und gegebenenfalls mindestens ein Teil des Gases der Kolonne zugeführt wird
    iv) aus der Kolonne ein mit gasförmigem Stickstoff angereicherter Durchsatz entnommen wird
    v) ein mit Kohlenmonoxid angereicherter Durchsatz aus der Kolonne entnommen und in dem Wärmeaustauscher erhitzt wird, dadurch gekennzeichnet, dass der mit Kohlenmonoxid angereicherte Durchsatz komprimiert wird, um ein mit Kohlenmonoxid angereichertes Produkt bei einem Produktionsdruck bereitzustellen, das Versorgungsgas nach dem Abkühlen in einen ersten Phasenabscheider (51) geführt wird, die Flüssigkeit des ersten Phasenabscheiders (61) expandiert wird, die expandierte Flüssigkeit in einen zweiten Phasenabscheider geführt wird und mindestens ein Teil der Flüssigkeit des zweiten Phasenabscheiders verdampft wird, um das dem Sumpfverdampfer zuzuführende Gas abzuleiten.
  2. Verfahren nach Anspruch 1, wobei ein Teil des Kohlenmonoxids auf einen Druck komprimiert wird, der kleiner oder gleich dem Produktionsdruck ist, im Wärmeaustauscher (3) gekühlt und in den Sumpf der Destillationskolonne (15) geführt wird.
  3. Verfahren nach Anspruch 1, wobei mindestens ein Teil der Flüssigkeit des zweiten Phasenabscheiders (61) im Wärmeaustauscher (33) verdampft wird.
  4. Vorrichtung zur Trennung eines Versorgungsgases, das Stickstoff und Kohlenmonoxid und gegebenenfalls Wasserstoff als Hauptkomponenten enthält, umfassend:
    a. eine Destillationskolonne (15), die einen Sumpfverdampfer (5) und gegebenenfalls einem Kopfkondensator (23)
    b. einen Wärmeaustauscher (3)
    c. einen Kompressor (29, 37)
    d. Mittel zum Zuführen des Versorgungsgases in den Wärmeaustauscher
    e. Mittel zum Zuführen mindestens eines Teils eines aus dem Versorgungsgas abgeleiteten Gases zum Verdampfer, um ihn durch die Erzeugung einer Flüssigkeit und gegebenenfalls eines Gases zumindest teilweise zu kondensieren
    f. mindestens Mittel zum Zuführen mindestens eines Teils der Flüssigkeit und gegebenenfalls mindestens eines Teils des Gases zu der Kolonne
    g. Mittel zum Entnehmen einer mit gasförmigem Stickstoff angereicherten Durchflussmenge aus der Kolonne
    h. Mittel zum Entnehmen eines mit Kohlenmonoxid angereicherten Durchsatzes aus der Kolonne und zum Zuführen derselben zum Wärmeaustauscher, dadurch gekennzeichnet, dass sie Mittel zum Zuführen des mit Kohlenmonoxid angereicherten Durchsatzes zum Kompressor umfasst, um ein mit Kohlenmonoxid angereichertes Produkt bei einem Produktionsdruck bereitzustellen, einen ersten Phasenabscheider (51), einen zweiten Phasenabscheider (61), Mittel zum Zuführen des gekühlten Versorgungsgases in den ersten Phasenabscheider, ein Expansionsventil (55) zum Expandieren der Flüssigkeit des ersten Phasenabscheiders, Mittel zum Zuführen der expandierten Flüssigkeit in den zweiten Phasenabscheider und Mittel (3) zum Verdampfen mindestens eines Teils der Flüssigkeit des zweiten Phasenabscheiders, um das dem Sumpfverdampfer (5) zuzuführende Gas abzuleiten.
  5. Vorrichtung nach Anspruch 4, umfassend Mittel zum Zuführen eines Teils des mit Kohlenmonoxid angereicherten Durchsatzes bei einem Druck, der kleiner oder gleich dem Produktionsdruck ist, zu dem Wärmeaustauscher (3) und dann in den Sumpf der Destillationskolonne (15).
  6. Vorrichtung nach Anspruch 4, wobei der Wärmeaustauscher (3) mit der Kolonne (15) und dem zweiten Phasenabscheider (61) verbunden ist, um mindestens einen Teil der Flüssigkeit des zweiten Abscheiders zu verdampfen, um das Heizgas aus dem Sumpfverdampfer (5) abzuleiten.
  7. Vorrichtung nach Anspruch 4, wobei die Destillationskolonne einen Kopfkondensator umfasst.
  8. Vorrichtung nach Anspruch 7, umfassend Mittel zum Zuführen der Sumpfflüssigkeit aus der Kolonne zum Kopfkondensator.
  9. Vorrichtung nach Anspruch 8, umfassend Mittel zum Zuführen der verdampften Sumpfflüssigkeit zum Kompressor.
EP10792965.5A 2009-11-24 2010-11-04 Verfahren und anlage zur kryogenen trennung einer mischung aus wasserstoff und kohlenmonoxid Active EP2504646B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR0958305A FR2953004B1 (fr) 2009-11-24 2009-11-24 Procede de separation cryogenique d'un melange d'azote et de monoxyde de carbone
PCT/FR2010/052368 WO2011067492A2 (fr) 2009-11-24 2010-11-04 Procede de separation cryogenique d'un melange d'azote et de monoxyde de carbone

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EP2504646A2 EP2504646A2 (de) 2012-10-03
EP2504646B1 true EP2504646B1 (de) 2019-01-02

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US (1) US9625209B2 (de)
EP (1) EP2504646B1 (de)
JP (1) JP2013511697A (de)
CN (1) CN102893110B (de)
FR (1) FR2953004B1 (de)
WO (1) WO2011067492A2 (de)

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JP2013511697A (ja) 2013-04-04
CN102893110A (zh) 2013-01-23
CN102893110B (zh) 2014-11-26
US9625209B2 (en) 2017-04-18
FR2953004B1 (fr) 2013-12-20
WO2011067492A3 (fr) 2014-03-20
WO2011067492A2 (fr) 2011-06-09
FR2953004A1 (fr) 2011-05-27
US20120279254A1 (en) 2012-11-08
EP2504646A2 (de) 2012-10-03

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