EP2140216B1 - Verfahren und vorrichtung zur trennung einer mischung mit mindestens einem wasserstoff, stickstoff und kohlenmonoxid durch kryogene destillation - Google Patents

Verfahren und vorrichtung zur trennung einer mischung mit mindestens einem wasserstoff, stickstoff und kohlenmonoxid durch kryogene destillation Download PDF

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EP2140216B1
EP2140216B1 EP07871916.8A EP07871916A EP2140216B1 EP 2140216 B1 EP2140216 B1 EP 2140216B1 EP 07871916 A EP07871916 A EP 07871916A EP 2140216 B1 EP2140216 B1 EP 2140216B1
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flow
carbon monoxide
column
high pressure
denitrogenation
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EP2140216A2 (de
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Arthur Darde
Antoine Hernandez
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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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
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • 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
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • 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
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/02—Control in general, load changes, different modes ("runs"), measurements

Definitions

  • the present invention relates to a process for separating a mixture of carbon monoxide, nitrogen, hydrogen and optionally methane by cryogenic distillation.
  • Figure 6 of Berninger's article shows a method and an installation according to the preamble of claim 1 and 6 respectively.
  • Other documents describing methane scrubbing processes include: EP-A-0928937 , US Patent 4478621 , US Patent 5609040 , and Tieftemperaturtechnik, page 418.
  • Carbon monoxide from cold boxes H 2 / CO carries with it a large fraction of the nitrogen present in the feed gas. This phenomenon is related to the difficulty of separating the two components CO and N 2 , their bubble points being very close. Nevertheless, depending on the use made of the CO downstream of the cold box, it is sometimes necessary to reduce its nitrogen content before exporting it.
  • denitrogenation column whose function is to produce carbon monoxide tank at the required purity.
  • a nitrogen purge containing a fraction of CO is recovered.
  • the denitrogenation column is located either upstream or downstream of the CO / CH 4 separation column.
  • the reboiling of the denitrogenation column is provided by an injection of carbon monoxide in the form of steam in the bottom of the column.
  • the average carbon dioxide vapor pressure flow rate will be dimensioned by the exchange line or by the maximum permissible fraction in the reboiling of the column CO / N 2 .
  • the average carbon dioxide vapor pressure flow rate will be dimensioned by the exchange line or by the maximum permissible fraction in the reboiling of the column CO / N 2 .
  • the present invention aims to eliminate this constraint which leads to a significant energy loss on the current estimates, as well as to eliminate the output of medium pressure gas on the compressor which compresses the carbon monoxide up to the high pressure (line, filter, valves, passages in exchangers, regulations, etc ).
  • the installation comprises means for measuring a flow rate of carbon monoxide rich gas sent to the tank.
  • the idea is to dimension the apparatus without the stress on the reboiling fraction independent of the vapor pressure medium carbon monoxide (and thus it is accepted that all the reboiling can come from the vaporization of the medium pressure carbon monoxide). Then a line is installed between the exit of high pressure carbon monoxide to the reboilers of the depletion column and the CO / CH 4 column (approximately -110 ° C) and the reboiling feed of the CO / N column 2 .
  • This line will therefore lead to the investment of the line itself and of a single valve (there are already the valves on the upstream lines going to the reboilers fed by the high pressure carbon monoxide) and downstream (monoxide of medium vaporized pressure carbon)).
  • the medium pressure carbon monoxide thus produced does not pass in a line of exchange and the flow can be set to zero for a running of the device. In operation, if it is desired to reduce the average vaporized pressure carbon monoxide while maintaining a higher reboil flow rate, it is sufficient to supplement this medium pressure carbon monoxide.
  • This invention is generalizable to all methane washing apparatus with denitration in the current scheme.
  • the flow rate of carbon monoxide medium pressure that can be vaporized in the exchange line is significantly lower than the reboiling rate, it will nonetheless be interesting to install a medium pressure outlet on the compressor, to avoid to relax a large flow of high pressure at the pressure of the column.
  • a flow containing carbon monoxide, hydrogen, methane and nitrogen 45 cools in exchanger 9 by heat exchange with a flow of carbon monoxide 1 and is sent to a methane scrubber column.
  • the bottom liquid of the column C1 is sent to the top of the depletion column C2.
  • the overhead gas of the C1 column enriched in hydrogen leaves the installation.
  • the bottoms liquid from the exhaust column C2 is sent to a CO / C3 methane separation column.
  • the bottom liquid of column C3 is returned to the top of column C1.
  • the overhead gas from the column C3 is sent to an intermediate point of the denitrogenation column C4 where it separates into a carbon monoxide rich liquid in the tank and a nitrogen-rich gas at the top.
  • the operation of the columns therefore corresponds essentially to that of the process of Figure 6 of Linde Reports on Science and Technology, Berninger's "Progress in H 2 / CO Low-Temperature Separation", 44/1988.
  • a flow rate of impure carbon monoxide at a pressure of 2.6 bar is sent to the compressor V1, V2 to be compressed to a pressure between 25 and 45 bar, preferably between 35 and 40 bar to form the flow 5.
  • This flow is divided into a part 7 which constitutes a production and another flow which is sent to the exchanger 9.
  • a fraction 13 passes entirely through the exchanger before being divided in two.
  • a first flow 55 is then divided into three flow rates 19, 21, 23.
  • a first flow 19 serves to reboil the exhaust column C2, a second flow 23 serves to reboil the CO / methane C3 column, the two flows 19, 23 being thereby liquefied and the cooled flow rates 19, 23 are sent with the third flow 21 to an exchanger 17.
  • the flow 23 is divided in two, a portion 25 being expanded in a valve 27 and then vaporized in the exchanger 17 and sent under gaseous form in the tank of the denitrogenation column C4.
  • the remainder 26 of the flow 23 is expanded to a pressure of 2.6 bar and sent to a separator pot 35 after expansion in a valve.
  • the flow rates 21, 19 are also expanded in valves and sent to the same separator pot 35.
  • the flow 57 of high pressure carbon monoxide is expanded in a valve 59 and then sent to the bottom of the denitrogenation column C4.
  • the sending of high pressure carbon monoxide 57 expanded in the valve 59 is triggered if the flow rate of gaseous carbon monoxide 15,25 sent to the denitrogenation column is reduced by at least 5%, or even by at least 10% compared to the nominal flow.
  • the gas 43 formed in the separator pot 35 is returned to the compressor V1 after reheating in the exchanger 9.
  • the liquid of the separator pot 35 is divided into four.
  • a part 1 is sent to a separator pot 33 where it forms a gaseous fraction 41 and a liquid fraction 31.
  • the liquid fraction 31 vaporizes in the exchanger 17.
  • the gaseous fraction 41 is heated in the exchanger 17 against the flow rates 19 , 21, 23 before being returned to the compressor V1.
  • Part 2 serves to sub-cool the methane wash column C1 before being mixed at the flow rate 41.
  • Part 3 serves to condense the head of the column CO / methane C3 where it vaporizes and is then returned to the compressor V1.
  • the fourth portion 37 is mixed with the bottom liquid 29 of the denitrogenation column and serves to cool the head thereof.
  • the formed flow 39 is returned to the compressor V1.
  • a flow 11 cools partially in the exchanger 9, is expanded in a turbine T, cools in the exchanger 17 as flow 15 and is sent to the bottom of the denitrogenation column C4.

Claims (9)

  1. Verfahren zum Trennen eines Gemisches aus Kohlenmonoxid, Stickstoff, Wasserstoff und eventuell aus Methan durch kryogene Destillation in einem System aus Trennmitteln umfassend eine Turbine (T), eine Methanwaschsäule (C1), eine Abtriebssäule (C2), eine CO/CH4 Säule (C3) und eine Säule zur Stickstoffentfernung (C4), wobei sich die Säule zur Stickstoffentfernung stromabwärts der CO/CH4 Säule befindet, wobei man das Gemisch trennt, um ein mit Kohlenmonoxid angereichertes, und Stickstoff enthaltendes Fluid zu erhalten, man dieses Fluid in der Säule zur Stickstoffentfernung trennt, man eine Fördermenge an Kohlenmonoxid, die aus dem Säulensystem stammt, in einem Verdichter (V1, V2) bis auf einen Hochdruck, eventuell zwischen 25 und 45 bar, verdichtet, man Kohlenmonoxid mit hohem Druck (11, 15) von dem Verdichter in die Turbine, und von der Turbine in die Säule zur Stickstoffentfernung schickt, wobei eine Fraktion (7) einer Fördermenge an Kohlenmonoxid als Produkt dient, und man einen anderen Teil (57) des Kohlenmonoxids mit hohem Druck, eventuell zwischen 25 und 45 bar, abkühlt, bevor dieser andere Teil entspannt wird, man zumindest zeitweise eine erste Fördermenge entspannt, die eine variable Menge des anderen Teils (57) von Kohlenmonoxid mit hohem Druck bildet, der in einem Ventil (59) abgekühlt wird, bevor er in den Sumpf der Säule zur Stickstoffentfernung geschickt wird, und eine zweite Fördermenge, die eine Fraktion des anderen Teils des Kohlenmonoxids mit hohem Druck, eventuell zwischen 25 und 45 bar, bildet, zum Sumpfverdampfer der Abtriebssäule und/ oder der CO/CH4 Säule geschickt wird, dadurch gekennzeichnet, dass die Fraktion (7) einer Fördermenge an Kohlenmonoxid, das als Produkt dient, hohen Druck aufweist, dadurch, dass die erste Fördermenge stromaufwärts des Sumpfverdampfers der Abtriebssäule und/ oder der CO/CH4 Säule von der zweiten Fördermenge getrennt wird, und dadurch, dass man die erste Fördermenge, die im Ventil entspannt wird, in Abhängigkeit von den Aufsiedbedürfnissen der Säule zur Stickstoffentfernung variiert.
  2. Verfahren nach Anspruch 1, wobei der hohe Druck zwischen 25 und 45 bar liegt.
  3. Verfahren nach einem der vorstehenden Ansprüche, wobei man eine Fördermenge (15, 25) an kohlenmonoxidreichem Gas, die in den Sumpf der Säule zur Stickstoffentfernung (C4) geschickt wird, misst und die Beschickung der ersten in dem Ventil (59) entspannten Fördermenge (57) in Abhängigkeit von der Fördermenge an kohlenmonoxidreichem Gas auslöst, die in den Sumpf der Säule zur Stickstoffentfernung geschickt wird.
  4. Verfahren nach Anspruch 3, wobei man die Beschickung der ersten in dem Ventil (59) entspannten Fördermenge (57) auslöst, wenn die Fördermenge an kohlenmonoxidreichem Gas (15, 25), die zur Säule zur Stickstoffentfernung geschickt wird, um mindestens 5%, oder gar um mindestens 10% im Verhältnis zur nominalen Fördermenge reduziert wird.
  5. Verfahren nach einem der vorstehenden Ansprüche, wobei der hohe Druck dem Ausgangsdruck der letzten Stufe des Verdichters (V1, V2) entspricht.
  6. Installation zum Trennen eines Gemisches aus Kohlenmonoxid, Stickstoff, Wasserstoff und eventuell aus Methan durch kryogene Destillation in einem System aus Trennmitteln umfassend eine Turbine (T), eine Methanwaschsäule (C1), eine Abtriebssäule (C2), eine CO/CH4 Säule (C3) und eine Säule zur Stickstoffentfernung (C4), wobei sich die Säule zur Stickstoffentfernung stromabwärts der CO/CH4 Säule befindet, Mittel zum Schicken des Gemisches zum System aus Trennmitteln, um ein mit Kohlenmonoxid angereichertes, und Stickstoff enthaltendes Fluid zu erhalten, Mittel zum Schicken dieses Fluids in die Säule zur Stickstoffentfernung, einen Verdichter (V1, V2), Mittel zum Schicken einer Fördermenge an Kohlenmonoxid, die aus dem Säulensystem stammt, zum Verdichter, und Mittel zum Aufnehmen einer Fördermenge an Kohlenmonoxid mit hohem Druck am Ausgang des Verdichters, Mittel zum Schicken eines Teils der Fördermenge mit hohem Druck in die Turbine, und von der Turbine in die Säule zur Stickstoffentfernung, Mittel zum Herausbekommen einer Fraktion einer Fördermenge an Kohlenmonoxid als Produkt, einen Wärmetauscher (9), in dem sich ein anderer Teil des Kohlenmonoxids mit hohem Druck abkühlt, und ein Ventil zum Entspannen (59) des Kohlenmonoxids mit hohem Druck, um eine erste Fördermenge zu entspannen, die eine variable Menge des anderen Teils des Kohlenmonoxids (57) bildet, wobei das Ventil mit dem Wärmetauscher und mit der Säule zur Stickstoffentfernung verbunden ist, Mittel zum Schicken einer zweiten Fördermenge, die eine Fraktion des anderen Teils des Kohlenmonoxids mit hohem Druck bildet, zum Sumpfverdampfer der Abtriebssäule und/ oder der CO/CH4 Säule, dadurch gekennzeichnet, dass die Mittel zum Herausbekommen des Kohlenmonoxids als Produkt aus Mitteln zum Herausbekommen einer Fraktion einer Fördermenge an Kohlenmonoxid mit hohem Druck bestehen, und dass sie Mittel zum Trennen der ersten Fördermenge von der zweiten Fördermenge stromaufwärts des Sumpfverdampfers der Abtriebssäule und/ oder der CO/CH4 Säule, und Mittel (59) zum Variieren der ersten Fördermenge an Kohlenmonoxid mit hohem Druck, die im Ventil entspannt wird, in Abhängigkeit von den Aufsiedbedürfnissen der Säule zur Stickstoffentfernung, umfasst.
  7. Installation nach Anspruch 6 umfassend Mittel zum Messen einer Fördermenge (15, 25) an kohlenmonoxidreichem Gas, die in den Sumpf der Säule zur Stickstoffentfernung (C4) geschickt wird, und Mittel zum Auslösen der Beschickung der ersten in dem Ventil (59) entspannten Fördermenge (57) in Abhängigkeit von der Fördermenge an kohlenmonoxidreichem Gas, die in den Sumpf der Säule zur Stickstoffentfernung geschickt wird.
  8. Installation nach Anspruch 6 oder 7 umfassend Mittel zum Schicken der zweiten Fördermenge zu einem Sumpfverdampfer der Abtriebssäule.
  9. Installation nach Anspruch 6 oder 7 oder 8 umfassend Mittel zum Schicken der zweiten Fördermenge zu einem Sumpfverdampfer der CO/CH4 Säule.
EP07871916.8A 2006-12-21 2007-12-12 Verfahren und vorrichtung zur trennung einer mischung mit mindestens einem wasserstoff, stickstoff und kohlenmonoxid durch kryogene destillation Active EP2140216B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR0655770A FR2910602B1 (fr) 2006-12-21 2006-12-21 Procede et appareil de separation d'un melange comprenant au moins de l'hydrogene, de l'azote et du monoxyde de carbone par distillation cryogenique
PCT/FR2007/052486 WO2008078040A2 (fr) 2006-12-21 2007-12-12 Procédé et appareil de séparation d'un mélange comprenant au moins de l'hydrogène, de l'azote et du monoxyde de carbone par distillation cryogénique

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EP2140216A2 EP2140216A2 (de) 2010-01-06
EP2140216B1 true EP2140216B1 (de) 2017-11-08

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US (1) US8555673B2 (de)
EP (1) EP2140216B1 (de)
CN (1) CN101568788B (de)
FR (1) FR2910602B1 (de)
WO (1) WO2008078040A2 (de)

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US20100251765A1 (en) * 2009-04-01 2010-10-07 Air Products And Chemicals, Inc. Cryogenic Separation of Synthesis Gas
FR2959297B1 (fr) * 2010-04-22 2012-04-27 Air Liquide Procede et appareil de production d'azote par distillation cryogenique d'air
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US20100071411A1 (en) 2010-03-25
US8555673B2 (en) 2013-10-15
CN101568788B (zh) 2011-11-02
WO2008078040A3 (fr) 2009-05-22
FR2910602B1 (fr) 2012-12-14
FR2910602A1 (fr) 2008-06-27
EP2140216A2 (de) 2010-01-06
WO2008078040A2 (fr) 2008-07-03

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