US20120174625A1 - Method and device for producing a gaseous pressurized oxygen product by cryogenic separation of air - Google Patents

Method and device for producing a gaseous pressurized oxygen product by cryogenic separation of air Download PDF

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Publication number
US20120174625A1
US20120174625A1 US13/389,862 US201013389862A US2012174625A1 US 20120174625 A1 US20120174625 A1 US 20120174625A1 US 201013389862 A US201013389862 A US 201013389862A US 2012174625 A1 US2012174625 A1 US 2012174625A1
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Prior art keywords
pseudo
stream
partial stream
increased pressure
feed air
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Abandoned
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US13/389,862
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English (en)
Inventor
Thomas Rathbone
Frances Masterson
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Linde GmbH
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Linde GmbH
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Priority claimed from DE200920010874 external-priority patent/DE202009010874U1/de
Application filed by Linde GmbH filed Critical Linde GmbH
Assigned to LINDE AKTIENGESELLSCHAFT reassignment LINDE AKTIENGESELLSCHAFT ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: MASTERSON, FRANCES, RATHBONE, THOMAS
Publication of US20120174625A1 publication Critical patent/US20120174625A1/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
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest 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
    • F25J3/04006—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
    • F25J3/04054—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 air
    • 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
    • F25J3/04066—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 oxygen
    • 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
    • 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
    • F25J3/0429—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
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high 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
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
    • 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
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/04—Multiple expansion turbines in parallel

Definitions

  • the invention relates to a process according to the preamble of patent claim 1 .
  • an oxygen product stream compressed in liquid form is vaporized against a heat transfer medium and finally obtained as a pressurized gaseous product.
  • This method is also referred to as internal compression. It serves for obtaining pressurized oxygen.
  • the product stream is then “pseudo-vaporized”.
  • a heat transfer medium under high pressure is liquefied (or pseudo-liquefied if under supercritical pressure) against the (pseudo) vaporizing product stream.
  • the heat transfer medium is often formed by part of the air, in the present case by the “second partial stream” of the compressed feed air.
  • the invention is based on the object of providing a process of the type mentioned at the beginning and a corresponding apparatus that operate particularly favorably in terms of energy.
  • the pressure increase to the product pressure (the “second increased pressure”) is not entirely carried out in the liquid state but only partly, that is to the lower “first increased pressure”.
  • the rest of the pressure increase is performed after the (pseudo) vaporization in the cold, but gaseous state.
  • the cold compression has the effect of introducing heat into the process that cannot be removed by means of economical coolants such as cooling water, as would be the case with warm compression.
  • the (pseudo) vaporization pressure lying below the final pressure, also allows the pressure of the second partial stream, which supplies the heat, to be chosen correspondingly lower.
  • mechanical energy produced in the process itself is used for driving the cold compressor; for this purpose, particularly the expander for the first partial stream of the feed air is mechanically coupled directly to the cold compressor, for example via a common shaft or a transmission.
  • the apparent disadvantage of an increased temperature when the cold-compressed product stream re-enters the heat exchange has proven to be an advantage.
  • the inlet temperature of the cold compressor lies, for example, 2 to 50 K, preferably 5 to 10 K, above the (pseudo) vaporization temperature of the product stream under the first increased pressure.
  • the process is particularly favorable when the oxygen product pressure (“second increased pressure”) lies between 20 and 40 bar.
  • the pressure ratio at the cold compressor is preferably 1.4 to 2.1, the “first increased pressure” between 10 and 30 bar.
  • the process can be carried out with a single expander.
  • a dissipative brake, a generator or a warm compressor must be coupled to the expander in addition to the cold compressor in order to produce the cold necessary for the process.
  • a second expander with a suitable process stream may be operated, assuming the task of producing the cold.
  • the work-performing expansion of the first partial stream is preferably carried out in two expanders connected in parallel or in series.
  • one of the two expanders may be coupled to the cold compressor and the other to a warm compressor, a generator or a dissipative brake.
  • the two expanders have the same inlet temperature and/or the same inlet pressure and the same outlet pressure and/or the same outlet temperature.
  • both expanders are therefore mechanically coupled to the cold compressor (and optionally in addition to a warm compressor, a generator or a dissipative brake).
  • the cold compressor and optionally in addition to a warm compressor, a generator or a dissipative brake.
  • two turbines connected in series are used, mechanically coupled to each other, for example via a common shaft, or a transmission machine.
  • the construction with both turbine wheels in a common housing, driving a common shaft and thus representing a unit, is particularly advantageous.
  • the common shaft drives the cold compressor and optionally a further braking device, for example a dissipative brake, a generator or a warm compressor.
  • main heat exchanger may be formed by one or more heat exchanger portions connected in parallel and/or in series, for example one or more plate heat exchanger blocks.
  • the invention also relates to an apparatus for producing a pressurized gaseous product by cryogenic air separation according to patent claims 8 to 13 .
  • FIG. 1 shows a first exemplary embodiment of the invention with a combined machine
  • FIGS. 2 to 5 show further embodiments, in which only one expander respectively drives the cold compressor.
  • air 1 flows from the main air compressor and the downstream air purification (neither represented) under very high pressure and is divided into a first partial stream 2 (turbine stream) and a second partial stream 3 (throttle stream).
  • the first partial stream 2 is introduced into a main heat exchanger 10 at the warm end thereof. At an intermediate temperature, the first partial stream is removed again via line 4 and subsequently expanded to an intermediate pressure in a first turbine 5 while performing work.
  • the intermediately compressed air 6 is warmed again in the main heat exchanger 10 (intermediate warming) and fed via line 7 to a second turbine 8 and expanded there from the intermediate pressure to approximately the operating pressure of the high-pressure column of the distillation column system (not represented) while performing work.
  • the exhaust air 9 of the second turbine 8 is fed to the high-pressure column as substantially gaseous feed air.
  • the second partial stream 3 is passed through the main heat exchanger 10 under very high pressure up to the cold end and thereby supplies the heat for an oxygen product stream vaporizing or pseudo-vaporizing under pressure, which has been removed from the distillation column system in liquid form ( 51 -LOX) and brought to a “first increased pressure” of 19.5 bar in a pump 52 .
  • the cold second partial stream is expanded to approximately high-pressure column pressure in a throttle valve 11 and introduced in liquid form or as a two-phase mixture into one or more columns of the distillation column system.
  • the two turbines 5 , 8 are mechanically coupled, to be precise by a common shaft 12 , which drives them both. Also seated on this shaft is a cold compressor 13 , which is driven by means of the mechanical energy produced in the turbines and transferred to the shaft 12 .
  • the shaft also drives a dissipative brake, a generator or a warm compressor (not represented).
  • the vaporized product stream 53 is drawn off from the main heat exchanger 10 at an intermediate temperature of approximately 5 to 10 K above the (pseudo) vaporization temperature and fed to the cold compressor 13 . There, it is compressed from the “first increased pressure” further to a “second increased pressure” of 33 bar. It leaves the cold compressor (line 54 ) at a temperature which is 15 to 30 K higher than the inlet temperature and is then fed at a suitable point to the main heat exchanger 10 again and warmed there to approximately ambient temperature. Finally, the pressurized gaseous product (PGOX) is removed from the warm end via line 55 .
  • PGOX pressurized gaseous product
  • the two expanders are connected in parallel.
  • the first partial stream 4 at the intermediate temperature is in this case divided into two branch streams 204 , 207 , which are respectively expanded in only one of the turbines 205 , 208 while performing work.
  • the two expanded air streams are reunited and passed on via line 9 , as in FIG. 1 .
  • the two turbines are designed as two separate machines.
  • the first turbine 205 drives a warm compressor 223 via a first common shaft.
  • This compressor is formed as a re-compressor for the feed air 1 compressed in the air compressor (not represented). There then follows a re-cooler and the re-compressed air is passed via line 201 to the warm end of the main heat exchanger 10 .
  • the second turbine 208 drives the cold compressor 13 for the (pseudo) vaporized product stream 53 via a second common shaft.
  • FIG. 3 differs from FIG. 2 in that not the entire air 1 is re-compressed, but only the second partial stream 303 .
  • the feed air 1 compressed in the air compressor is already divided into the first partial stream 2 and the second partial stream 303 upstream of the re-compressor 323 , and only the second partial stream 303 is fed to the re-compressor 323 .
  • the re-compressed second partial stream 3 is finally passed as before to the warm end of the main heat exchanger 10 and forms the throttle stream.
  • FIG. 4 a further modification of FIG. 2 is represented.
  • the compressed feed air is pre-cooled upstream of the re-compressor 223 in an additional group of passages 410 of the main heat exchanger 10 , as is explained in more detail in DE 102007042462.
  • the exemplary embodiment of Figure differs from FIG. 3 by the additional group of passages 510 of the main heat exchanger.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
US13/389,862 2009-08-11 2010-08-10 Method and device for producing a gaseous pressurized oxygen product by cryogenic separation of air Abandoned US20120174625A1 (en)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
DE202009010874.0 2009-08-11
DE200920010874 DE202009010874U1 (de) 2009-08-11 2009-08-11 Vorrichtung zur Erzeugung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
EP09013224 2009-10-20
EP09013224.2 2009-10-20
PCT/EP2010/004883 WO2011018207A2 (fr) 2009-08-11 2010-08-10 Procédé et dispositif pour générer un produit gazeux sous pression contenant de l'oxygène par fractionnement cryogénique de l'air

Publications (1)

Publication Number Publication Date
US20120174625A1 true US20120174625A1 (en) 2012-07-12

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Application Number Title Priority Date Filing Date
US13/389,862 Abandoned US20120174625A1 (en) 2009-08-11 2010-08-10 Method and device for producing a gaseous pressurized oxygen product by cryogenic separation of air

Country Status (5)

Country Link
US (1) US20120174625A1 (fr)
EP (1) EP2464937A2 (fr)
CN (1) CN102741636A (fr)
RU (1) RU2012108588A (fr)
WO (1) WO2011018207A2 (fr)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2600090B1 (fr) * 2011-12-01 2014-07-16 Linde Aktiengesellschaft Procédé et dispositif destinés à la production d'oxygène sous pression par décomposition à basse température de l'air
CN112361716A (zh) * 2020-10-26 2021-02-12 乔治洛德方法研究和开发液化空气有限公司 用于从空气分离装置中制备高压气体的方法和装置

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4796431A (en) * 1986-07-15 1989-01-10 Erickson Donald C Nitrogen partial expansion refrigeration for cryogenic air separation
FR2709537B1 (fr) * 1993-09-01 1995-10-13 Air Liquide Procédé et installation de production d'oxygène et/ou d'azote gazeux sous pression.
US6009723A (en) * 1998-01-22 2000-01-04 Air Products And Chemicals, Inc. Elevated pressure air separation process with use of waste expansion for compression of a process stream
FR2854682B1 (fr) * 2003-05-05 2005-06-17 Air Liquide Procede et installation de separation d'air par distillation cryogenique
US7228715B2 (en) * 2003-12-23 2007-06-12 L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic air separation process and apparatus
EP1767884A1 (fr) * 2005-09-23 2007-03-28 L'Air Liquide Société Anon. à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé et dispositif pour la séparation cryogénique d'air
DE102006012241A1 (de) * 2006-03-15 2007-09-20 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
EP1972875A1 (fr) * 2007-03-23 2008-09-24 L'AIR LIQUIDE, S.A. pour l'étude et l'exploitation des procédés Georges Claude Procédé et dispositif pour la séparation cryogénique d'air
FR2915271A1 (fr) * 2007-04-23 2008-10-24 Air Liquide Procede et appareil de separation des gaz de l'air par distillation cryogenique

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Publication number Publication date
RU2012108588A (ru) 2013-09-20
CN102741636A (zh) 2012-10-17
EP2464937A2 (fr) 2012-06-20
WO2011018207A3 (fr) 2014-03-13
WO2011018207A2 (fr) 2011-02-17

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