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US20110067445A1 - Method And Apparatus For Separating Air By Cryogenic Distillation - Google Patents

Method And Apparatus For Separating Air By Cryogenic Distillation Download PDF

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US20110067445A1
US20110067445A1 US12/937,608 US93760809A US2011067445A1 US 20110067445 A1 US20110067445 A1 US 20110067445A1 US 93760809 A US93760809 A US 93760809A US 2011067445 A1 US2011067445 A1 US 2011067445A1
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nitrogen
column
pressure
pressure column
vaporizer
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US12/937,608
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Benoit Davidian
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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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Priority claimed from FR0852710A external-priority patent/FR2930331B1/en
Priority claimed from FR0852708A external-priority patent/FR2930329A1/en
Priority claimed from FR0852705A external-priority patent/FR2930326B1/en
Priority claimed from FR0852706A external-priority patent/FR2930327A1/en
Priority claimed from FR0852707A external-priority patent/FR2930328A1/en
Application filed by LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Assigned to L'AIR LIQUIDE SOCIETE ANONYME POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE reassignment L'AIR LIQUIDE SOCIETE ANONYME POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: DAVIDIAN, BENOIT
Publication of US20110067445A1 publication Critical patent/US20110067445A1/en
Abandoned legal-status Critical Current

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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
    • F25J3/04—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 for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04181—Regenerating the adsorbents
    • 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
    • F25J3/04—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 for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams 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
    • F25J3/04—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 for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • F25J3/04—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 for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04103—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression using solely hydrostatic liquid head
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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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    • F25J3/04—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 for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
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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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    • 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
    • F25J3/04—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 for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • F25J3/04—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 for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure 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
    • 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
    • F25J3/04—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 for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams 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
    • F25J3/04—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 for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams 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
    • F25J3/04—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 for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
    • 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
    • F25J3/04—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 for air
    • F25J3/04406—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 for air using a dual pressure main column system
    • F25J3/04418—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 for air using a dual pressure main column system with thermally overlapping high and low pressure columns
    • 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
    • F25J2200/34—Processes or apparatus using separation by rectification using a side column fed by a stream from the low pressure 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
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
    • 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
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    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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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    • F25J2250/42—One fluid being 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
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    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen

Definitions

  • the present invention relates to a method and to an apparatus for producing oxygen by separating air using cryogenic distillation.
  • One object of the invention is to reduce the specific energy of separation of low-pressure low-purity oxygen, particularly in schemes where the pressurized nitrogen is not realized as an asset in its own right by the end-customer.
  • the object of the invention is achieved via the use of a scheme employing three vaporizers in the low-pressure column, in which:
  • the specific energy saving represents between 0.5% and 7%.
  • U.S. Pat. No. 5,006,139 describes a method for producing nitrogen using a low-pressure column the bottom vaporizer of which is heated by a flow of medium-pressure nitrogen compressed in a cold compressor. According to the invention, there is also a proposal to use several turbines in order better to optimize the exchange line.
  • the method of the present invention produces gaseous oxygen and preferably does not produce nitrogen from the medium-pressure column.
  • One subject of the invention provides a method for producing oxygen by separating air using cryogenic distillation in an installation comprising a double column comprising a medium-pressure and a low-pressure column, the low-pressure column containing a bottom vaporizer, an intermediate vaporizer and an upper vaporizer, in which method:
  • Another aspect of the invention provides an apparatus for producing oxygen by separation of air using cryogenic distillation comprising a double column comprising a medium-pressure column and a low-pressure column, the low-pressure column containing a bottom vaporizer, an intermediate vaporizer and an upper vaporizer, a purification unit, an exchange line, at least one first turbine, at least one cold compressor, means for sending compressed air, purified in the purification unit and cooled in the exchange line, to the medium-pressure column of the double column, means for withdrawing an oxygen-rich fluid from the low-pressure column, means for possibly heating it up, said means consisting at least in part of the exchange line and means for sending the heated-up oxygen-rich fluid sent to the customer, means for splitting the nitrogen tapped off from the medium-pressure column into at least three parts, means for sending a first part of the nitrogen to a first turbine, means for sending a second part of the nitrogen to a cold compressor where its pressure can be raised, means for sending the raised-pressure second part to the bottom vaporizer, means for sending the nitrogen thus
  • the apparatus may possibly comprise:
  • FIGS. 1 , 2 and 3 are schematic diagrams of air separation apparatuses according to the invention.
  • FIG. 1 shows an air separation apparatus in which a pressurized and purified air flow 1 is split into three flows 3 , 5 , 7 .
  • the flow 3 is cooled as it passes from one end of the exchange line 11 to the other and is sent to the medium-pressure column 15 of a double column.
  • the flow 5 is cooled as it passes from one end of the exchange line 11 to the other and is sent to an intermediate vaporizer 21 of the low-pressure column 17 of the double column 15 , 17 .
  • the other air flow 7 has its pressure raised in a hot pressurizer 9 , is cooled by passing from one end of the exchange line 11 to the other and is sent to a vaporizer 13 where it condenses at least partially by exchanging heat with pressurized liquid oxygen.
  • the condensed air is either sent in its entirety to the medium-pressure column or split between the medium-pressure column and the low-pressure column 17 .
  • Rich liquid 25 , lean liquid 61 and possibly a liquid 27 somewhat like liquid air are sent from the medium-pressure column 15 to the low-pressure column 17 as reflux flows after supercooling in the exchanger 29 .
  • a flow of liquid oxygen 33 is tapped off from the low-pressure column, pressurized by the pump 35 and vaporized in the vaporizer 13 upstream of the exchange line 11 .
  • the fluid 33 may also be compressed by the effect of a hydrostatic head, without the pump 35 .
  • Low-pressure nitrogen 31 is tapped off from the top of the low-pressure column 17 and is heated up in the exchangers 29 , 11 .
  • a medium-pressure gaseous flow of nitrogen 39 is tapped off from the top of the medium-pressure column 15 and split into two.
  • One part 53 is sent to an upper vaporizer 23 of the low-pressure column 17 where it condenses before being returned to the medium-pressure column by way of reflux.
  • the remainder of the nitrogen 41 is split into two, one portion 43 being sent to a cold compressor 51 to form a flow 55 , and this flow 55 is sent to the bottom vaporizer 19 of the low-pressure column 17 .
  • this vaporizer 19 it condenses and then acts as reflux for at least one of the columns.
  • the remainder 45 of the nitrogen is sent to the exchange line, is heated up to an intermediate level, and is sent to a turbine 47 .
  • the nitrogen expanded in the turbine 47 is sent to the cold end of the exchange line and heats up, becoming the flow 49 .
  • FIG. 2 shows an air separation apparatus in which a pressurized and purified air flow 1 is split into two flows 3 , 7 .
  • the flow 3 is cooled as it passes from one end of the exchange line 11 to the other and is sent to the medium-pressure column 15 of a double column.
  • the other air flow 7 has its pressure raised in a hot pressurizer 9 , is cooled as it passes from one end of the exchange line 11 to the other and is sent to a vaporizer 13 where it condenses at least in part by exchange of heat with pressurized liquid oxygen.
  • the condensed air is either sent in its entirety to the medium-pressure column or split between the medium-pressure column and the low-pressure column 17 .
  • Rich liquid 25 , lean liquid 61 and possibly a liquid 27 somewhat like liquid air are sent from the medium-pressure column 15 to the low-pressure column 17 as reflux flows after supercooling in the exchanger 29 .
  • a flow of liquid oxygen 33 is tapped off from the low-pressure column, pressurized by the pump 35 and vaporized in the vaporizer 13 upstream of the exchange line 11 .
  • the fluid 33 may also be compressed using a hydrostatic head, without the pump 35 .
  • Low-pressure nitrogen 31 is tapped off from the top of the low-pressure column 17 and heats up in the exchangers 29 , 11 .
  • a medium-pressure gaseous flow of nitrogen 39 is tapped off from the top of the medium-pressure column 15 and split into two.
  • One part 53 is sent to an upper vaporizer 23 of the low-pressure column 17 where it condenses before being returned to the medium-pressure column by way of reflux.
  • the remainder of the air is once again split into two.
  • One fraction is sent to the cold compressor 151 to become the flow 155 which heats the intermediate vaporizer 21 before being sent to the columns by way of reflux.
  • the remainder of the nitrogen 41 is split into two, one portion 43 being sent to a cold compressor 51 to form a flow 55 , and this flow 55 is sent to the bottom vaporizer 19 of the low-pressure column 17 . In this vaporizer 19 it condenses and then serves as reflux for at least one of the columns.
  • the remainder 45 of the nitrogen is sent to the exchange line, is heated up to an intermediate level and is sent to a turbine 47 .
  • the nitrogen expanded in the turbine 47 is sent to the cold end of the exchange line and heats up, becoming the flow 49 . Having the two cold compressors 51 , 151 on the medium-pressure nitrogen line allows the distribution of power across the compressors to be adjusted to best suit the low-pressure column reboiling requirement.
  • FIG. 3 shows an air separation apparatus in which an air flow 1 , pressurized by a compressor M and purified in a purification unit 2 is split into two flows 3 , 7 .
  • the flow 3 is cooled as it passes from one end of the exchange line 11 to the other and is sent to the medium-pressure column 15 of a double column.
  • the other 7 has its pressure raised in a hot pressurizer 9 , is cooled by passing from one end of the exchange line 11 to the other and is sent to a vaporizer 13 where it condenses at least in part by exchange of heat with pressurized liquid oxygen.
  • the condensed air is either sent in its entirety to the medium-pressure column or split between the medium-pressure column and the low-pressure column 17 .
  • Rich liquid 25 , lean liquid 61 , and possibly a liquid 27 somewhat like liquid air are sent from the medium-pressure column 15 to the low-pressure column 17 by way of reflux flows following supercooling in the exchanger 29 .
  • a flow of liquid oxygen 33 is tapped off from the low-pressure column, pressurized by the pump 35 and vaporized in the vaporizer 13 upstream of the exchange line 11 .
  • the fluid 33 may also be compressed using a hydrostatic head, without the pump 35 .
  • Low-pressure nitrogen 31 is tapped off from the top of the low-pressure column 17 and is heated up in the exchangers 29 , 11 .
  • a medium-pressure gaseous flow of nitrogen 39 is tapped off from the top of the medium-pressure column 15 and split into two.
  • One part 53 is sent to an upper vaporizer 23 of the low-pressure column 17 where it condenses before being returned to the medium-pressure column by way of reflux.
  • the remainder of the air is once again split into two.
  • One fraction is sent to the cold compressor 151 where it becomes the flow 155 , the flow 155 being cooled in the exchange line 11 before being used to heat the intermediate vaporizer 21 before being sent to the columns by way of reflux.
  • the remainder of the nitrogen 41 is split into two, one portion 43 being sent to a cold compressor 51 to form a flow 55 , and this flow 55 is sent to the bottom vaporizer 19 of the low-pressure column 17 after having been cooled in the exchange line 11 .
  • this vaporizer 19 it condenses and then serves as reflux for at least one of the columns.
  • the remainder 45 of the nitrogen is sent to the exchange line, heats up to an intermediate level and is split into two.
  • One part 49 of the nitrogen 45 is sent to a turbine 47 .
  • the nitrogen expanded in the turbine 47 is sent to the cold end of the exchange line and is heated up before being used periodically to regenerate the purification unit 2 .
  • the remainder of the nitrogen 46 continues to be heated up in the exchange line 11 and is split into two, one part 149 being sent to a turbine 147 at a higher inlet temperature than the turbine 47 .
  • This part of the nitrogen is expanded, heated up and discharged into the atmosphere.
  • the remainder 249 of the nitrogen is sent to a turbine 247 at a higher inlet temperature than the turbines 47 , 147 . This part 249 of the nitrogen is expanded, heated up and discharged into the atmosphere.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
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  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

A method and to an apparatus for producing oxygen by separating air using cryogenic distillation is presented.

Description

  • The present invention relates to a method and to an apparatus for producing oxygen by separating air using cryogenic distillation.
  • One object of the invention is to reduce the specific energy of separation of low-pressure low-purity oxygen, particularly in schemes where the pressurized nitrogen is not realized as an asset in its own right by the end-customer.
  • The object of the invention is achieved via the use of a scheme employing three vaporizers in the low-pressure column, in which:
      • the bottom vaporizer operates on cold compressed medium-pressure nitrogen
      • the upper intermediate vaporizer operates on medium-pressure nitrogen
      • the lower intermediate vaporizer operates either on medium-pressure air or on medium-pressure nitrogen which is cold compressed.
  • Depending on variables, the specific energy saving represents between 0.5% and 7%.
  • U.S. Pat. No. 5,006,139 describes a method for producing nitrogen using a low-pressure column the bottom vaporizer of which is heated by a flow of medium-pressure nitrogen compressed in a cold compressor. According to the invention, there is also a proposal to use several turbines in order better to optimize the exchange line.
  • The method of the present invention produces gaseous oxygen and preferably does not produce nitrogen from the medium-pressure column.
  • One subject of the invention provides a method for producing oxygen by separating air using cryogenic distillation in an installation comprising a double column comprising a medium-pressure and a low-pressure column, the low-pressure column containing a bottom vaporizer, an intermediate vaporizer and an upper vaporizer, in which method:
      • a) compressed air is purified in a purification unit, cooled in an exchange line and fed to the medium-pressure column of the double column
      • b) an oxygen-rich fluid is withdrawn from the low-pressure column, heated up and sent to the customer
      • c) nitrogen tapped off from the medium-pressure column is split into at least three parts
      • d) a first part of the nitrogen is expanded in a first turbine
      • e) a second part of the nitrogen has its pressure raised in a cold compressor and is sent to the bottom vaporizer, the nitrogen thus condensed being sent to at least one column of the double column
      • f) a third part of the nitrogen is sent to the upper vaporizer, with no pressure-modifying step downstream of the column from which it is tapped off and upstream of the upper vaporizer, the nitrogen thus condensed being sent to at least one column of the double column
      • g) a gaseous flow is sent to the intermediate vaporizer, this flow consisting of purified and cooled compressed air or of the nitrogen tapped off from the medium-pressure column and compressed in a cold compressor.
  • According to other optional aspects:
      • the gaseous flow sent to the intermediate vaporizer, is nitrogen from the medium-pressure column
      • the gaseous flow sent to the intermediate vaporizer is purified and cooled compressed air
      • the first part of the nitrogen expanded in the first turbine is used for regenerating the purification unit
      • the first turbine drives the cold compressor in which the pressure of the second part of the fluid is raised and provides substantially all the cold energy for the method
      • the low-pressure column has no top condenser
      • all the gaseous nitrogen from the top of the medium-pressure column is split into just the three parts
      • all the gaseous nitrogen from the top of the medium-pressure column is split into just four parts, the fourth part being sent to the intermediate vaporizer
      • substantially all the cold energy is produced by expanding nitrogen from the medium-pressure column in at least one turbine
      • a liquid oxygen flow from the low-pressure column is vaporized, possibly after pressurizing it, to produce the fluid sent to the customer.
  • Another aspect of the invention provides an apparatus for producing oxygen by separation of air using cryogenic distillation comprising a double column comprising a medium-pressure column and a low-pressure column, the low-pressure column containing a bottom vaporizer, an intermediate vaporizer and an upper vaporizer, a purification unit, an exchange line, at least one first turbine, at least one cold compressor, means for sending compressed air, purified in the purification unit and cooled in the exchange line, to the medium-pressure column of the double column, means for withdrawing an oxygen-rich fluid from the low-pressure column, means for possibly heating it up, said means consisting at least in part of the exchange line and means for sending the heated-up oxygen-rich fluid sent to the customer, means for splitting the nitrogen tapped off from the medium-pressure column into at least three parts, means for sending a first part of the nitrogen to a first turbine, means for sending a second part of the nitrogen to a cold compressor where its pressure can be raised, means for sending the raised-pressure second part to the bottom vaporizer, means for sending the nitrogen thus condensed to at least one column of the double column, means for sending a third part of the nitrogen to the upper vaporizer, without a pressure modifying means downstream of the column from which it was tapped off and upstream of the upper vaporizer, means for sending the nitrogen thus condensed being sent to at least one column of the double column, means for sending a gaseous flow to the intermediate vaporizer, this flow consisting of purified and cooled compressed air or of nitrogen tapped off from the medium-pressure column and compressed in the second cold compressor.
  • The apparatus may possibly comprise:
      • means for connecting the intermediate vaporizer to the top of the medium-pressure column
      • means for connecting the outlet of the first turbine to the purification unit
      • the first turbine is coupled to the cold compressor in which the pressure of the second part of the fluid is raised and constitutes the only turbine in the apparatus
      • the low-pressure column has no top condenser
      • means for vaporizing liquid oxygen, possibly in the exchange line, and possibly means for pressurizing liquid oxygen upstream of the means for vaporizing the liquid oxygen.
  • The invention will be described in greater detail with reference to FIGS. 1, 2 and 3 which are schematic diagrams of air separation apparatuses according to the invention.
  • FIG. 1 shows an air separation apparatus in which a pressurized and purified air flow 1 is split into three flows 3, 5, 7. The flow 3 is cooled as it passes from one end of the exchange line 11 to the other and is sent to the medium-pressure column 15 of a double column. The flow 5 is cooled as it passes from one end of the exchange line 11 to the other and is sent to an intermediate vaporizer 21 of the low-pressure column 17 of the double column 15, 17. The other air flow 7 has its pressure raised in a hot pressurizer 9, is cooled by passing from one end of the exchange line 11 to the other and is sent to a vaporizer 13 where it condenses at least partially by exchanging heat with pressurized liquid oxygen. The condensed air is either sent in its entirety to the medium-pressure column or split between the medium-pressure column and the low-pressure column 17.
  • Rich liquid 25, lean liquid 61 and possibly a liquid 27 somewhat like liquid air are sent from the medium-pressure column 15 to the low-pressure column 17 as reflux flows after supercooling in the exchanger 29.
  • A flow of liquid oxygen 33 is tapped off from the low-pressure column, pressurized by the pump 35 and vaporized in the vaporizer 13 upstream of the exchange line 11. The fluid 33 may also be compressed by the effect of a hydrostatic head, without the pump 35.
  • Low-pressure nitrogen 31 is tapped off from the top of the low-pressure column 17 and is heated up in the exchangers 29, 11.
  • A medium-pressure gaseous flow of nitrogen 39 is tapped off from the top of the medium-pressure column 15 and split into two. One part 53 is sent to an upper vaporizer 23 of the low-pressure column 17 where it condenses before being returned to the medium-pressure column by way of reflux. The remainder of the nitrogen 41 is split into two, one portion 43 being sent to a cold compressor 51 to form a flow 55, and this flow 55 is sent to the bottom vaporizer 19 of the low-pressure column 17. In this vaporizer 19 it condenses and then acts as reflux for at least one of the columns.
  • The remainder 45 of the nitrogen is sent to the exchange line, is heated up to an intermediate level, and is sent to a turbine 47. The nitrogen expanded in the turbine 47 is sent to the cold end of the exchange line and heats up, becoming the flow 49.
  • This yields a potential energy saving of 0.5% over the scheme disclosed in WO-A-2007/129152.
  • FIG. 2 shows an air separation apparatus in which a pressurized and purified air flow 1 is split into two flows 3,7. The flow 3 is cooled as it passes from one end of the exchange line 11 to the other and is sent to the medium-pressure column 15 of a double column. The other air flow 7 has its pressure raised in a hot pressurizer 9, is cooled as it passes from one end of the exchange line 11 to the other and is sent to a vaporizer 13 where it condenses at least in part by exchange of heat with pressurized liquid oxygen. The condensed air is either sent in its entirety to the medium-pressure column or split between the medium-pressure column and the low-pressure column 17.
  • Rich liquid 25, lean liquid 61 and possibly a liquid 27 somewhat like liquid air are sent from the medium-pressure column 15 to the low-pressure column 17 as reflux flows after supercooling in the exchanger 29.
  • A flow of liquid oxygen 33 is tapped off from the low-pressure column, pressurized by the pump 35 and vaporized in the vaporizer 13 upstream of the exchange line 11. The fluid 33 may also be compressed using a hydrostatic head, without the pump 35.
  • Low-pressure nitrogen 31 is tapped off from the top of the low-pressure column 17 and heats up in the exchangers 29, 11.
  • A medium-pressure gaseous flow of nitrogen 39 is tapped off from the top of the medium-pressure column 15 and split into two. One part 53 is sent to an upper vaporizer 23 of the low-pressure column 17 where it condenses before being returned to the medium-pressure column by way of reflux. The remainder of the air is once again split into two. One fraction is sent to the cold compressor 151 to become the flow 155 which heats the intermediate vaporizer 21 before being sent to the columns by way of reflux. The remainder of the nitrogen 41 is split into two, one portion 43 being sent to a cold compressor 51 to form a flow 55, and this flow 55 is sent to the bottom vaporizer 19 of the low-pressure column 17. In this vaporizer 19 it condenses and then serves as reflux for at least one of the columns.
  • The remainder 45 of the nitrogen is sent to the exchange line, is heated up to an intermediate level and is sent to a turbine 47. The nitrogen expanded in the turbine 47 is sent to the cold end of the exchange line and heats up, becoming the flow 49. Having the two cold compressors 51, 151 on the medium-pressure nitrogen line allows the distribution of power across the compressors to be adjusted to best suit the low-pressure column reboiling requirement.
  • An energy saving of 1.7% over the scheme of WO-A-2007/129152 can be achieved.
  • FIG. 3 shows an air separation apparatus in which an air flow 1, pressurized by a compressor M and purified in a purification unit 2 is split into two flows 3, 7. The flow 3 is cooled as it passes from one end of the exchange line 11 to the other and is sent to the medium-pressure column 15 of a double column. The other 7 has its pressure raised in a hot pressurizer 9, is cooled by passing from one end of the exchange line 11 to the other and is sent to a vaporizer 13 where it condenses at least in part by exchange of heat with pressurized liquid oxygen. The condensed air is either sent in its entirety to the medium-pressure column or split between the medium-pressure column and the low-pressure column 17.
  • Rich liquid 25, lean liquid 61, and possibly a liquid 27 somewhat like liquid air are sent from the medium-pressure column 15 to the low-pressure column 17 by way of reflux flows following supercooling in the exchanger 29.
  • A flow of liquid oxygen 33 is tapped off from the low-pressure column, pressurized by the pump 35 and vaporized in the vaporizer 13 upstream of the exchange line 11. The fluid 33 may also be compressed using a hydrostatic head, without the pump 35.
  • Low-pressure nitrogen 31 is tapped off from the top of the low-pressure column 17 and is heated up in the exchangers 29, 11.
  • A medium-pressure gaseous flow of nitrogen 39 is tapped off from the top of the medium-pressure column 15 and split into two. One part 53 is sent to an upper vaporizer 23 of the low-pressure column 17 where it condenses before being returned to the medium-pressure column by way of reflux. The remainder of the air is once again split into two. One fraction is sent to the cold compressor 151 where it becomes the flow 155, the flow 155 being cooled in the exchange line 11 before being used to heat the intermediate vaporizer 21 before being sent to the columns by way of reflux. The remainder of the nitrogen 41 is split into two, one portion 43 being sent to a cold compressor 51 to form a flow 55, and this flow 55 is sent to the bottom vaporizer 19 of the low-pressure column 17 after having been cooled in the exchange line 11. In this vaporizer 19 it condenses and then serves as reflux for at least one of the columns.
  • The remainder 45 of the nitrogen is sent to the exchange line, heats up to an intermediate level and is split into two. One part 49 of the nitrogen 45 is sent to a turbine 47. The nitrogen expanded in the turbine 47 is sent to the cold end of the exchange line and is heated up before being used periodically to regenerate the purification unit 2. The remainder of the nitrogen 46 continues to be heated up in the exchange line 11 and is split into two, one part 149 being sent to a turbine 147 at a higher inlet temperature than the turbine 47. This part of the nitrogen is expanded, heated up and discharged into the atmosphere. The remainder 249 of the nitrogen is sent to a turbine 247 at a higher inlet temperature than the turbines 47, 147. This part 249 of the nitrogen is expanded, heated up and discharged into the atmosphere.
  • An energy saving of 7% over the scheme of WO-A-2007/129152 can be achieved.

Claims (15)

1-15. (canceled)
16. A method for producing oxygen by separating air using cryogenic distillation in an installation comprising a double column comprising a medium-pressure column and a low-pressure column, the low-pressure column containing the bottom vaporizer, an intermediate vaporizer and an upper vaporizer, said method comprising:
a) purifying compressed air in a purification unit, cooling said purified compressed air in an exchange line, and feeding the cooled compressed air to the medium-pressure column of the double column;
b) withdrawing an oxygen-rich fluid from the low-pressure column, heating the oxygen-rich fluid and sending the heated oxygen-rich fluid to a customer
c) withdrawing a nitrogen stream from the medium-pressure column, and splitting said nitrogen stream into at least three parts
d) expanding a first part of the nitrogen in a first turbine,
e) increasing the pressure of a second part of the nitrogen in a cold compressor and sending said pressurized nitrogen to the bottom vaporizer, sending the nitrogen thus condensed to at least one column of the double column;
f) condensing a third part of the nitrogen in the upper vaporizer, with no pressure-modifying step downstream of the column from which it is tapped off and upstream of the upper vaporizer, sending the nitrogen thus condensed to at least one column of the double column;
g) sending a gaseous flow to the intermediate vaporizer, this flow consisting of the nitrogen withdrawn from the medium-pressure column and compressed in a cold compressor.
17. The method of claim 16, in which the first part of the nitrogen expanded in the first turbine is used for regenerating the purification unit.
18. The method of claim 16, wherein the first turbine drives the cold compressor in which the pressure of the second part of the nitrogen is raised and provides substantially all cold energy required for the method.
19. The method of claim 16, wherein the low-pressure column has no top condenser.
20. The method of claim 16, wherein all the gaseous nitrogen from the top of the medium-pressure column is split into just the three parts.
21. The method of claim 16, wherein all the gaseous nitrogen from the top of the medium-pressure column is split into just four parts, the fourth part being sent to the intermediate vaporizer.
22. The method of claim 16, wherein substantially all cold energy required for the method is produced by expanding nitrogen from the medium-pressure column in at least one turbine.
23. The method of claim 16, wherein a liquid oxygen flow from the low-pressure column is vaporized to produce the fluid sent to the customer.
24. The method of claim 23, wherein said liquid oxygen is pressurized after removal from the low-pressure column and prior to vaporization.
25. An apparatus for producing oxygen by separation of air using cryogenic distillation comprising a double column comprising;
a) a medium-pressure column and a low-pressure column, the low-pressure column containing a bottom vaporizer, an intermediate vaporizer and an upper vaporizer,
b) a purification unit, a
c) n exchange line,
d) at least one first turbine,
e) at least one cold compressor,
f) means for sending compressed air, purified in the purification unit and cooled in the exchange line, to the medium-pressure column of the double column,
g) means for withdrawing an oxygen-rich fluid from the low-pressure column,
h) said means consisting at least in part of the exchange line means for sending the oxygen-rich fluid sent to the customer,
i) means for splitting the nitrogen withdrawn from the medium-pressure column into at least three parts,
j) means for sending a first part of the nitrogen to the first turbine,
k) means for sending a second part of the nitrogen to the cold compressor where its pressure is raised,
l) means for sending the raised-pressure second part to the bottom vaporizer,
m) means for sending the nitrogen thus condensed to at least one column of the double column,
n) means for sending a third part of the nitrogen to the upper vaporizer, without a pressure modifying means downstream of the column from which it was withdrawn from and upstream of the upper vaporizer,
o) means for sending the nitrogen thus condensed being sent to at least one column of the double column,
p) means for sending a gaseous flow to the intermediate vaporizer, this flow consisting of purified and cooled compressed air or of nitrogen
tapped off from the medium-pressure column and compressed in the second cold compressor,
also comprising means for connecting the intermediate vaporizer to the top of the medium-pressure column so that the nitrogen tapped off from the top of this column is sent to the intermediate vaporizer.
26. The apparatus of claim 25, further comprising g′) means for heating said oxygen-rich fluid from step g).
27. The apparatus of claim 25, further comprising means for connecting the outlet of the first turbine to the purification unit.
28. The apparatus of claim 25, wherein the first turbine is coupled to the cold compressor in which the pressure of the second part of the fluid is raised and constitutes the only turbine in the apparatus.
29. The apparatus of claim 25, wherein the low-pressure column has no top condenser.
US12/937,608 2008-04-22 2009-04-08 Method And Apparatus For Separating Air By Cryogenic Distillation Abandoned US20110067445A1 (en)

Applications Claiming Priority (13)

Application Number Priority Date Filing Date Title
FR0852709A FR2930330B1 (en) 2008-04-22 2008-04-22 METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION
FR0852709 2008-04-22
FR0852710A FR2930331B1 (en) 2008-04-22 2008-04-22 METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION
FR0852708A FR2930329A1 (en) 2008-04-22 2008-04-22 Air separating method, involves sending residual oxygen directly to atmosphere through tower in direct contact with water at hot end of exchange line and cold compressor that uses part of refrigerated power of turbine
FR0852705 2008-04-22
FR0852708 2008-04-22
FR0852705A FR2930326B1 (en) 2008-04-22 2008-04-22 METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION
FR0852706 2008-04-22
FR0852706A FR2930327A1 (en) 2008-04-22 2008-04-22 Air separating method for carbon oxycombustion frame, involves sending oxygen and nitrogen enrich liquids, and reheating nitrogen rich flow from low pressure columns and oxygen rich flow in exchange line
FR0852707 2008-04-22
FR0852710 2008-04-22
FR0852707A FR2930328A1 (en) 2008-04-22 2008-04-22 Air separating method for oxycombustion application in boiler, involves sending oxygen and nitrogen enriched liquids to low pressure column, removing oxygen enriched gas in condenser, and drawing nitrogen enriched gas from column
PCT/FR2009/050617 WO2009136075A2 (en) 2008-04-22 2009-04-08 Method and apparatus for separating air by cryogenic distillation

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US20140223959A1 (en) * 2011-09-20 2014-08-14 Linde Aktiengesellschaft Method and device for the cryogenic decomposition of air
US10443931B2 (en) * 2011-09-20 2019-10-15 Linde Aktiengesellschaft Method and device for the cryogenic decomposition of air
US20150121955A1 (en) * 2012-05-11 2015-05-07 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and apparatus for air separation by cryogenic distillation
US20160245586A1 (en) * 2013-10-15 2016-08-25 L'Air Liquide, Societe Anonyme pour I'Etude et I'Exploitation des Procedes Claude Method and device for separating air by cryogenic distillation
US10295253B2 (en) * 2013-10-15 2019-05-21 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and device for separating air by cryogenic distillation
US20170030637A1 (en) * 2015-07-31 2017-02-02 Air Liquide Global E&C Solutions Us Inc Method for the production of low pressure gaseous oxygen
US20170030636A1 (en) * 2015-07-31 2017-02-02 AIR LIQUIDE GLOBAL E&C SOLUTIONS US Inc. Apparatus for the production of low pressure gaseous oxygen
US10018414B2 (en) * 2015-07-31 2018-07-10 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for the production of low pressure gaseous oxygen
US10101084B2 (en) * 2015-07-31 2018-10-16 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Apparatus for the production of low pressure gaseous oxygen

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WO2009136075A2 (en) 2009-11-12
CA2722261A1 (en) 2009-11-12
WO2009136075A3 (en) 2010-10-07
AU2009245592A1 (en) 2009-11-12
AU2009245592B2 (en) 2013-09-19
JP2011518307A (en) 2011-06-23
CN102016469A (en) 2011-04-13
WO2009136075A4 (en) 2010-11-25

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