EP2504646A2 - Verfahren zur kryogenen trennung einer mischung aus wasserstoff und kohlenmonoxid - Google Patents

Verfahren zur kryogenen trennung einer mischung aus wasserstoff und kohlenmonoxid

Info

Publication number
EP2504646A2
EP2504646A2 EP10792965A EP10792965A EP2504646A2 EP 2504646 A2 EP2504646 A2 EP 2504646A2 EP 10792965 A EP10792965 A EP 10792965A EP 10792965 A EP10792965 A EP 10792965A EP 2504646 A2 EP2504646 A2 EP 2504646A2
Authority
EP
European Patent Office
Prior art keywords
liquid
gas
column
carbon monoxide
phase separator
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP10792965A
Other languages
English (en)
French (fr)
Other versions
EP2504646B1 (de
Inventor
Antoine Hernandez
Arthur Darde
Bernard Saulnier
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP2504646A2 publication Critical patent/EP2504646A2/de
Application granted granted Critical
Publication of EP2504646B1 publication Critical patent/EP2504646B1/de
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • 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.
  • the production units for carbon monoxide and hydrogen can be separated into two parts:
  • cryogenic separation unit called cold box for the production of CO.
  • 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 washing 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, Ar and N 2 ) being very low and compatible with the purity of the 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 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 disclose methods comprising the features of the preamble of claim 1 and similar to that of FIG. According to one object of the invention, there is provided a method for separating a feed gas containing, as main components, nitrogen and carbon monoxide and optionally hydrogen in a distillation column in which:
  • the feed gas is cooled in a heat exchanger (3) ii) at least a portion of the feed gas or at least a portion of a gas derived from the feed gas is supplied to a bottom reboiler of the distillation column in order to condense it at least partially by producing a liquid and optionally a gas
  • a carbon monoxide enriched flow is withdrawn from the column, it is heated in the heat exchanger characterized in that the carbon monoxide enriched flow is compressed to provide a product enriched in carbon monoxide at a rate of production pressure, the feed gas is sent after cooling in a first phase separator, the liquid is depressurized from the first phase separator, the expanded liquid is sent to a second phase separator and at least a portion of the liquid is vaporized the second phase separator for diverting the gas to be sent to the reboiler.
  • the at least part of the liquid of the second phase separator is vaporized in the heat exchanger.
  • an apparatus for separating a feed gas containing as main components nitrogen and carbon monoxide and optionally hydrogen comprising: i) a distillation column having a bottom reboiler and optionally a top condenser
  • v) means for sending at least a portion of the feed gas or at least a portion of a gas derived from the feed gas to the reboiler to at least partially condense it by producing a liquid and optionally a gas
  • viii) means for withdrawing a carbon monoxide enriched flow from the column and for sending it to the heat exchanger, characterized in that it comprises means for sending the flow enriched in carbon monoxide to the compressor to provide a product enriched in carbon monoxide at a production pressure, a first phase separator (51), a second phase separator, means for sending the cooled feed gas into the first phase separator, an expansion valve to relax the liquid of the first phase separator, means for sending the expanded liquid to the second phase separator and means for vaporizing at least a portion of the liquid of the second phase separator to divert the gas to be sent to the reboiler.
  • the apparatus comprises:
  • the heat exchanger is connected to the column and to the second phase separator in order to vaporize at least a portion of the liquid of the second separator in order to divert the heating gas from the reboiler the distillation column comprises a top condenser.
  • a flow rate of nitrogen and carbon monoxide 1 is cooled in a heat exchanger 3. It condenses at least partially in a loop, which is then fed to the tank 15 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 1 1 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 with water and then divided in half. 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, expands in a turbine 43 and remixed with the flow 27. The rest of the carbon monoxide is compressed to the product pressure by the stage 37 of the compressor and cooled by the cooler 31 A to form the product flow 39.
  • the stage 29 is located as much smaller than some of the reboiling is provided by the 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 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 fed to the distillation column 5.
  • the remainder 65 of the liquid of the separator 61 is heated in the exchanger 3A to form the flow 65 which serves to heat the reboiler 5 fed by the liquid tank 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 in the same way as in Figure 1.
  • a nitrogen flow rate is removed as a temperature and is heated in the exchanger 3.
  • the vaporized carbon monoxide 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 with 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 1 against liquid nitrogen 137.
  • the liquid nitrogen 137 is vaporized and heated in the exchanger 3.
  • the flow 133 is expanded and mixed with the flow 21 downstream of the valve 19.
  • the flow 45 which is sent to the bottom of the column 5 after cooling in the exchanger 3A.
  • the carbon monoxide liquefied 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 part 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 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 fed to the distillation column 5.
  • the remainder 65 of the liquid of the separator 61 is heated in the exchanger 3A to form the flow 65 which serves to heat the reboiler 5 fed by the liquid tank 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 in the same way as for Figure 1.
  • a nitrogen flow is removed as a purge and is heated in the exchanger 3.
  • the enriched flow rate of vaporized carbon monoxide 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 with water and then diverted in half.
  • the flow 33 is cooled 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 to heat up in the exchanger 3.
  • the flow 45 from the shelf 29 is sent to the tank 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 part vaporizes in the exchange line 3A and the gas 87 is mixed with the flow rate of carbon monoxide 27 for the compressor 29.

Landscapes

  • 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)
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

Publications (2)

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

Family

ID=42364047

Family Applications (1)

Application Number Title Priority Date Filing Date
EP10792965.5A Active EP2504646B1 (de) 2009-11-24 2010-11-04 Verfahren und anlage zur kryogenen trennung einer mischung aus wasserstoff und kohlenmonoxid

Country Status (6)

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

Families Citing this family (6)

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Publication number Priority date Publication date Assignee Title
FR2982168B1 (fr) * 2011-11-04 2015-05-01 Air Liquide Procede et appareil de separation d'un gaz riche en dioxyde de carbone par distillation
FR3011069B1 (fr) * 2013-09-24 2015-09-11 Air Liquide Procede et appareil de separation cryogenique d'un melange contenant au moins du monoxyde de carbone, de l'hydrogene et de l'azote
FR3013107A1 (fr) * 2013-11-14 2015-05-15 Air Liquide Procede et appareil de deazotation d’un fluide riche en monoxyde de carbone
FR3084453B1 (fr) * 2018-07-25 2020-11-27 Air Liquide Procede et appareil de separation cryogenique d'un melange de monoxyde de carbone, d'hydrogene et de methane pour la production de ch4
DE102020130946B4 (de) * 2020-11-23 2023-02-02 Xenon Holding Gmbh Kryogenes Verfahren zur Wertstoffgewinnung aus einem wasserstoffreichen Einsatzgas
FR3118144A3 (fr) * 2020-12-22 2022-06-24 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de separation cryogenique d’un melange d’hydrogene, de methane, d’azote et de monoxyde de carbone

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FR2953004A1 (fr) 2011-05-27
WO2011067492A2 (fr) 2011-06-09
US20120279254A1 (en) 2012-11-08
CN102893110A (zh) 2013-01-23
WO2011067492A3 (fr) 2014-03-20
EP2504646B1 (de) 2019-01-02
US9625209B2 (en) 2017-04-18
CN102893110B (zh) 2014-11-26
FR2953004B1 (fr) 2013-12-20
JP2013511697A (ja) 2013-04-04

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