US20060021380A1 - Method and installation for production of noble gases and oxygen by means of cryrogenic air distillation - Google Patents

Method and installation for production of noble gases and oxygen by means of cryrogenic air distillation Download PDF

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Publication number
US20060021380A1
US20060021380A1 US10/527,002 US52700205A US2006021380A1 US 20060021380 A1 US20060021380 A1 US 20060021380A1 US 52700205 A US52700205 A US 52700205A US 2006021380 A1 US2006021380 A1 US 2006021380A1
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stream
column
oxygen
pressure column
withdrawing
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Lasad Jaouani
Frederic Judas
Bernard Saulnier
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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LAir Liquide SA a Directoire et Conseil de Surveillance pour lEtude et lExploitation des Procedes Georges Claude
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Assigned to L'AIR LIQUIDE, SOCIETE ANONYME A DIRECTOIRE ET CONSEIL DE SURVEILLANCE POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE reassignment L'AIR LIQUIDE, SOCIETE ANONYME A DIRECTOIRE ET CONSEIL DE SURVEILLANCE POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: JAOUANI, LASAD, JUDAS, FREDERIC, SAULNIER, BERNARD
Publication of US20060021380A1 publication Critical patent/US20060021380A1/en
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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
    • F25J3/04006—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
    • 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
    • F25J3/04303—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
    • F25J3/04406—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
    • F25J3/04412—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 in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04745—Krypton and/or Xenon
    • 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
    • F25J2200/32—Processes or apparatus using separation by rectification using a side column fed by a stream from the 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
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F25J2200/94—Details relating to the withdrawal point
    • 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
    • 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
    • F25J2290/12—Particular process parameters like pressure, temperature, ratios

Definitions

  • the present invention relates to a method and a plant for producing oxygen and rare gases by air distillation.
  • a weak krypton/xenon mixture is conventionally produced from a purge at the main vaporizer of a double air separation column (see “Tieftemperaturtechnik” by Hausen and Linde, 1985 edition, pp. 337-340 and “Separation of Gases” by Isalski, 1989 edition, pp. 96-98).
  • the oxygen produced is then withdrawn from the low-pressure column a few stages above the vaporizer. If the oxygen is withdrawn in gaseous form, this arrangement allows a substantial fraction of the krypton present in the air and all of the xenon to be recovered.
  • DE-A-2603505 discloses an air separation unit in which a fluid containing krypton and xenon is produced in a purification column fed with two streams of rich liquid coming from the medium-pressure column, the reboiling in the purification column being provided by a vaporizer fed with the overhead gas from an argon column.
  • One object of the present invention is to propose systems for increasing the krypton and xenon yield of units producing gaseous oxygen by pumping and vaporization of liquid oxygen (or more generally those with substantial withdrawal of liquid oxygen from the bottom of the low-pressure column) and, preferably, also producing argon.
  • Another object of the present invention is again to have a principal vaporizer with a high oxygen content and massively purged, and thus to greatly limit the concentration of hydrocarbons/impurities (the advantage of a pumped “oxytonne”), which is not the case with the conventional scheme producing a weak mixture of krypton and xenon.
  • One subject of the invention is a method for producing oxygen and rare gases by distillation in a column system comprising at least one medium-pressure column, one low-pressure column and one auxiliary column, in which method:
  • the liquid stream sent as reflux to the auxiliary column is liquefied air and/or liquid enriched with nitrogen relative to a liquefied air stream sent to the medium-pressure column.
  • the liquid stream sent as reflux to the auxiliary column is liquefied air and/or liquid enriched with nitrogen relative to a liquefied air stream sent to the medium-pressure column.
  • Another subject of the invention is a plant for producing oxygen and rare gases by distillation in a column system comprising at least one medium-pressure column, one low-pressure column and one auxiliary column, which plant comprises:
  • the plant includes:
  • FIGS. 1 to 9 are diagrams showing the principle of plants according to the invention.
  • a double air separation column comprises a medium-pressure column K 01 and a low-pressure column K 02 that are thermally coupled by means of a principal vaporizer E 02 that is used to condense at least part of the gaseous overhead nitrogen of the column K 01 by heat exchange with oxygen from the bottom of the column K 02 .
  • An argon column K 10 is fed with an argon-enriched fluid 7 coming from the low-pressure column K 02 and an argon-enriched liquid 9 is returned from the argon column K 10 to the low-pressure column K 02 .
  • An argon-rich stream ARGON is withdrawn from the top of the column K 10 .
  • a portion of the dry and decarbonized air is compressed in an air booster (not illustrated) up to the pressure sufficient to allow vaporization of the optionally pumped oxygen. It is then condensed in the main exchange line (not illustrated). At the cold end of the main exchange line, this flow is expanded in a valve or in a hydraulic turbine.
  • the liquid phase LIQ AIR of this fluid can then be distributed as streams 1 , 3 and 5 between the medium-pressure column K 01 , the low-pressure column K 02 and the auxiliary column K 05 , respectively.
  • the liquid contains 78 mol % nitrogen.
  • the other portion of the medium-pressure air MP AIR is cooled in the main exchange line and sent to the bottom of the medium-pressure column K 01 .
  • the principle of the present invention is to concentrate the krypton and the xenon in a rich liquid RL 2 , which will then be treated in an auxiliary column K 05 .
  • Two rich liquids RL 1 and RL 2 are therefore withdrawn from the medium-pressure column K 01 , namely a “conventional” rich liquid withdrawn from an intermediate level a few stages above the bottom of the column and containing a small quantity of krypton and of xenon, RL 1 , and a rich bottoms liquid concentrated with krypton and xenon, RL 2 .
  • This “conventional” rich liquid RL 1 can then be sent to the column K 02 after having been subcooled.
  • the rich bottoms liquid RL 2 is sent to the K 10 argon mixture condenser E 10 after subcooling (not illustrated). Stages are installed above this equipment in order to concentrate the krypton and the xenon at the argon mixture condenser.
  • This assembly constitutes the column K 05 .
  • a portion of the reflux from this column is provided by a portion 5 of the liquid air LIQ AIR not feeding the column K 01 , after this has been subcooled.
  • the other portion of the reflux is provided by a portion 15 of the mean liquid 11 conventionally sent to the column K 02 via the line 13 and containing at least 80 mol % nitrogen.
  • a gas 16 is withdrawn from the intermediate level of the column K 05 below the points of reflux injection, and constitutes the vaporized rich liquid. It is then recycled in the column K 02 .
  • the overhead gas WN 2 ′ from the column K 05 constitutes a portion of the waste gas WN 2 leaving the cold box.
  • the purge PURGE from the mixture condenser E 10 contains most of the krypton and xenon that are present in the air and have been treated by the columns K 01 and K 05 .
  • This flow feeds a device for concentrating the rare gases. For example, it may be sent into the weak krypton/xenon mixture column (K 90 ). The bottom of this column contains the product to be beneficiated. The vapor 17 coming from the column K 90 is sent back into the bottom of the column K 05 .
  • the column K 90 is heated by a stream of air forming a fraction of the MP AIR.
  • the liquefied air thus formed may be sent back to the medium-pressure column K 01 and/or to the low-pressure column K 02 .
  • liquid oxygen LO is withdrawn as bottoms from the column K 02 , level with the principal vaporizer E 02 .
  • the principal vaporizer is therefore massively purged.
  • the liquid oxygen LO is preferably pressurized by a pump and then vaporized in the exchange line or in a dedicated vaporizer, by heat exchange with the pressurized air.
  • a nitrogen cycle may serve to vaporize the liquid oxygen LO.
  • FIG. 1 various alternative embodiments deriving from FIG. 1 will be presented.
  • the elements common with FIG. 1 will not be described a second time.
  • all of the liquid air LIQ AIR present at the outlet of the exchange line can be withdrawn from the column K 01 (preferably at the point of introduction of the liquid air) and then distributed between the column K 02 and the column K 05 after having been subcooled, as shown in FIG. 4 .
  • the stream 16 is omitted and replaced with a stream of waste nitrogen WN 2 ′ sent from the top of the auxiliary column K 05 to an intermediate point on the low-pressure column.
  • FIG. 8 An example is given in FIG. 8 .
  • FIG. 9 An example is given in FIG. 9 .
  • the blown air is sent into the bottom of the column K 05 so as to recover the krypton and xenon that it contains.
  • the schemes illustrated in FIGS. 1 to 9 may also include distillation assemblies, such as for example an Etienne column (a column that operates at an intermediate pressure between the medium and low pressures and fed with rich liquid).
  • Etienne column a column that operates at an intermediate pressure between the medium and low pressures and fed with rich liquid.

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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)
US10/527,002 2002-09-04 2003-07-30 Method and installation for production of noble gases and oxygen by means of cryrogenic air distillation Abandoned US20060021380A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR02/10922 2002-09-04
FR0210922A FR2844039B1 (fr) 2002-09-04 2002-09-04 Procede et installation de production d'oxygene et de gaz rares par distillation cryogenique d'air
PCT/FR2003/002420 WO2004023054A1 (fr) 2002-09-04 2003-07-30 Procede et installation de production d'oxygene et de gaz rares par distillation cryogenique d'air

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US20060021380A1 true US20060021380A1 (en) 2006-02-02

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US10/527,002 Abandoned US20060021380A1 (en) 2002-09-04 2003-07-30 Method and installation for production of noble gases and oxygen by means of cryrogenic air distillation

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Country Link
US (1) US20060021380A1 (fr)
EP (1) EP1552230A1 (fr)
JP (1) JP2005538335A (fr)
CN (1) CN100420908C (fr)
FR (1) FR2844039B1 (fr)
RU (1) RU2319084C2 (fr)
UA (1) UA85167C2 (fr)
WO (1) WO2004023054A1 (fr)

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20080289362A1 (en) * 2007-05-24 2008-11-27 Stefan Lochner Process and apparatus for low-temperature air fractionation
US20100037656A1 (en) * 2008-08-14 2010-02-18 Neil Mark Prosser Krypton and xenon recovery method
US20100071412A1 (en) * 2008-09-22 2010-03-25 David Ross Parsnick Method and apparatus for producing high purity oxygen
US20110041552A1 (en) * 2008-04-23 2011-02-24 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Apparatus And Method For Separating Air By Cryogenic Distillation
US20110126585A1 (en) * 2009-12-02 2011-06-02 David Ross Parsnick Krypton xenon recovery from pipeline oxygen
US20110302956A1 (en) * 2010-06-09 2011-12-15 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Rare Gases Recovery Process For Triple Column Oxygen Plant
EP2481815A1 (fr) 2006-05-11 2012-08-01 Raindance Technologies, Inc. Dispositifs microfluidiques
US20120285197A1 (en) * 2009-12-11 2012-11-15 L'air Liquide Societe Anonyme Pour L'etude Et L' Exploitation Des Procedes Georges Claude Process and unit for the separation of air by cryogenic distillation
EP3067649A1 (fr) * 2015-03-13 2016-09-14 Linde Aktiengesellschaft Système de colonnes de distillation et procédé de production d'oxygène par séparation cryogénique de l'air
US20210356205A1 (en) * 2020-05-15 2021-11-18 Brian R. Kromer Enhancements to a moderate pressure nitrogen and argon producing cryogenic air separation unit
US20220357104A1 (en) * 2021-05-06 2022-11-10 Air Products And Chemicals, Inc. Fluid recovery process and apparatus for xenon and or krypton recovery

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009029749A1 (fr) * 2007-08-30 2009-03-05 Linde, Inc. Procédés pour produire des fluides cryogéniques stériles
RU2481658C2 (ru) * 2011-06-30 2013-05-10 Александр Прокопьевич Елохин Способ и система концентрирования и утилизации инертных радиоактивных газов из газоаэрозольных выбросов энергоблоков атомных электростанций
RU2528792C1 (ru) * 2013-03-20 2014-09-20 Открытое акционерное общество "Газпром" Способ выделения одноступенчатой ректификацией инертных газов из хвостовых газов и устройство для его осуществления
RU2528786C1 (ru) * 2013-03-20 2014-09-20 Открытое акционерное общество "Газпром" Способы выделения двухступенчатой ректификацией инертных газов из хвостовых газов и устройство для его осуществления
FR3013431B1 (fr) * 2013-11-21 2018-11-09 L'air Liquide,Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de separation d’air par distillation cryogenique
WO2015109522A1 (fr) * 2014-01-24 2015-07-30 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Enceinte cryogénique
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JP2005538335A (ja) 2005-12-15
UA85167C2 (ru) 2009-01-12
CN1678875A (zh) 2005-10-05
RU2319084C2 (ru) 2008-03-10
EP1552230A1 (fr) 2005-07-13
FR2844039B1 (fr) 2005-04-29
CN100420908C (zh) 2008-09-24
WO2004023054A1 (fr) 2004-03-18
RU2005109412A (ru) 2005-10-10

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