EP1552230A1 - Procede et installation de production d oxygene et de gaz ra res par distillation cryogenique d air - Google Patents

Procede et installation de production d oxygene et de gaz ra res par distillation cryogenique d air

Info

Publication number
EP1552230A1
EP1552230A1 EP03758191A EP03758191A EP1552230A1 EP 1552230 A1 EP1552230 A1 EP 1552230A1 EP 03758191 A EP03758191 A EP 03758191A EP 03758191 A EP03758191 A EP 03758191A EP 1552230 A1 EP1552230 A1 EP 1552230A1
Authority
EP
European Patent Office
Prior art keywords
column
flow
oxygen
enriched
pressure column
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP03758191A
Other languages
German (de)
English (en)
French (fr)
Inventor
Lasad Jaouani
Frédéric Judas
Bernard Saulnier
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Publication of EP1552230A1 publication Critical patent/EP1552230A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—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 process and installation for the production of oxygen and rare gases by air distillation.
  • the production of a weak mixture of krypton and xenon is conventionally carried out from a purge at the level of the main vaporizer of a double column of air separation (see 'Tieftemperaturtechriik' by Hausen and Linde, edition of 1985, pp. 337-340 and 'Separation of Gases' by Isalski, 1989 edition, pp. 96-98).
  • the oxygen production is then withdrawn from the low pressure column a few trays above the vaporizer. In the case where the oxygen is drawn off in the gaseous form, this arrangement makes it possible to recover a large fraction of the krypton present in the air and all of the xenon.
  • DE-A-2605305 describes an air separation device in which a fluid containing krypton and xenon is produced in a purification column supplied by. two flow rates of rich liquid coming from the medium pressure column, the reboiling of the purification column being ensured by a vaporizer supplied with the overhead gas from an argon column.
  • An object of the present invention is to propose systems making it possible to increase the krypton and xenon yield of devices producing gaseous oxygen by pumping and vaporizing liquid oxygen (or more generally with high draw-off of liquid oxygen in the bottom of the column low pressure) and preferably also producing argon.
  • Another object of the present invention is to find a main vaporizer with a high oxygen content that is massively purged and thus to greatly limit the concentration of hydrocarbons / impurities (advantage of pump oxygen), which is not the case with the diagram. classic producing a weak mixture of krypton and xenon. According to an object of the invention,.
  • a process for producing oxygen and rare gases by distillation in a column system comprising at least one medium pressure column, a low pressure column and an auxiliary column in which: i) at least one flow of cooled and purified air at the medium pressure column where it separates, ii) at least a first nitrogen-enriched flow is withdrawn from the medium pressure column and at least part of this flow is sent directly or indirectly to the low pressure column, iii) an intermediate flow is withdrawn from an intermediate level of the medium pressure column, iv) a flow, enriched in oxygen with respect to the intermediate flow, is withdrawn from the medium pressure column and it is sent to the bottom of the auxiliary column , v) a flow rich in nitrogen is drawn off from the head of the low pressure column, vi) a liquid flow rich in oxygen is drawn off from the low pressure column as a product, possibly after s a vaporization step to form a gaseous product, vii) an oxygen-enriched flow rate, also enriched in krypton and xenon, is drawn
  • the liquid flow rate sent as reflux to the auxiliary column is liquefied air and / or liquid enriched in nitrogen compared to a flow rate of liquefied air sent to the medium pressure column.
  • the tank of the auxiliary column is heated by an overhead gas from an argon column.
  • the liquefied air and / or the liquid enriched in nitrogen with respect to the air is produced by heat exchange with the liquid flow rich in oxygen coming from the tank of the low pressure column, possibly after a pressurization step.
  • the liquid enriched in nitrogen contains at least 80% mol. nitrogen.
  • an installation for producing oxygen and rare gases by distillation in a column system comprising at least one medium pressure column, a low pressure column and an auxiliary column comprising: i) means for sending at least one flow of cooled and purified air to the medium pressure column where it separates, ii " ) means for withdrawing at least a first flow enriched in nitrogen from the medium pressure column and means for sending to the at least part of this flow directly or indirectly to the low pressure column, iii) means for withdrawing a nitrogen-rich flow from the head of the low pressure column, iv) means for withdrawing an intermediate flow of an intermediate level of the medium pressure column, v) means for sending a flow, richer in oxygen than the intermediate flow, from the tank of the medium pressure column to the tank of the
  • the installation comprises: a purification column, means for sending the third oxygen-enriched flow at the head of the purification column and means for withdrawing at least some theoretical plates lower in the column, a fourth flow enriched in oxygen constituting a mixture enriched in krypton and xenon.
  • a double air separation column comprises a medium pressure column K01 and a low pressure column K02, thermally connected to each other by means of a main vaporizer E02 which is used to condense at least part nitrogen gas at the top of the column
  • An argon column K10 is supplied with a fluid enriched in argon 7 coming from the low pressure column K02 and a liquid enriched in argon 9 is returned from the argon column K10 to the low pressure column K02.
  • a flow rich in ARGON argon is withdrawn at the head of column K10.
  • the other part of the medium pressure air AIR P is cooled in the main exchange line and sent to the medium pressure column tank K01.
  • the principle of the present invention is to concentrate the krypton and the xenon in a rich liquid LR2 which will then be treated at the level of an auxiliary column K05.
  • Two rich liquids LR1 and LR2 are therefore drawn off from the medium pressure column K01: a “classic” rich liquid drawn off at an intermediate level a few trays above the column tank and containing a small amount of krypton and xenon LR1 and a liquid rich in vats, concentrated in krypton and xenon LR2.
  • This "classic" LR1 rich liquid can then be sent to column K02 after being sub-cooled.
  • the rich tank liquid LR2 is sent to the condenser E10 of the argon mixture K10 after sub-cooling (not shown). Trays are installed above this equipment to concentrate krypton and xenon at the argon mixture condenser.
  • This set constitutes column K05.
  • Part of the reflux of this column is provided by part 5 of the AIR LIQ liquid air which does not supply the column K01, and this after having sub-cooled it.
  • the other part of the reflux is provided by a part 15 of the lean liquid 11 conventionally sent in column K02 via line 13 and containing at least 80% mol. nitrogen.
  • a gas 16 is drawn off at the intermediate level of the column K05, below the reflux injection points and constitutes the rich vaporized liquid. It is then recycled in column K02.
  • the overhead gas WN2 'from column K05 constitutes part of the waste gas WN2 leaving the cold box.
  • the PURGE purge of the mixture condenser E10 contains most of the krypton and xenon present in the air and having been treated by columns K01 and K05. This flow feeds a device allowing the concentration of rare gases. For example, it can be sent to the weak mixture column krypton-xenon (K90). The tank in this column contains the product to be recovered. Steam 17 from column K90 is returned to the column tank K05.
  • Liquid oxygen OL 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. Alternatively a nitrogen cycle can be used to vaporize the liquid oxygen OL.
  • all of the AIR LIQ liquid air present at the outlet of the exchange line can be withdrawn from column K01 (preferably at the level of introduction of liquid air) and then distributed between column K02 and K05 after being sub-cooled as seen in Figure 4.
  • the waste gas WN2 'from column K05 is returned to column K02 below the point of injection of the lean liquid 13.
  • the flow rate 16 is eliminated and replaced by a sending of residual nitrogen WN2 'from the head of the auxiliary column K05 at an intermediate point of the low pressure column.
  • the blown air is sent to the column tank K05 in order to recover the krypton and the xenon it contains.
  • diagrams described in Figures 1 to 9 can also include distillation units such as an Etienne column for example (column operating at an intermediate pressure between medium and low pressures and supplied with rich liquid).
  • distillation units such as an Etienne column for example (column operating at an intermediate pressure between medium and low pressures and supplied with rich liquid).

Landscapes

  • 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)
EP03758191A 2002-09-04 2003-07-30 Procede et installation de production d oxygene et de gaz ra res par distillation cryogenique d air Withdrawn EP1552230A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
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
FR0210922 2002-09-04
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

Publications (1)

Publication Number Publication Date
EP1552230A1 true EP1552230A1 (fr) 2005-07-13

Family

ID=31503096

Family Applications (1)

Application Number Title Priority Date Filing Date
EP03758191A Withdrawn EP1552230A1 (fr) 2002-09-04 2003-07-30 Procede et installation de production d oxygene et de gaz ra res par distillation cryogenique d air

Country Status (8)

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

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AU2008293476A1 (en) * 2007-08-30 2009-03-05 Linde Llc Methods for producing sterile cryogenic fluids
FR2930629B1 (fr) * 2008-04-23 2010-05-07 Air Liquide Appareil et procede de separation d'air par distillation cryogenique
US8443625B2 (en) * 2008-08-14 2013-05-21 Praxair Technology, Inc. Krypton and xenon recovery method
US8479535B2 (en) * 2008-09-22 2013-07-09 Praxair Technology, Inc. Method and apparatus for producing high purity oxygen
US8484992B2 (en) 2009-12-02 2013-07-16 Praxair Technology, Inc. Krypton xenon recovery from pipeline oxygen
FR2953915B1 (fr) * 2009-12-11 2011-12-02 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
US8978413B2 (en) * 2010-06-09 2015-03-17 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Rare gases recovery process for triple column oxygen plant
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 (en) * 2014-01-24 2015-07-30 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic enclosure
EP3067649A1 (de) * 2015-03-13 2016-09-14 Linde Aktiengesellschaft Destillationssäulen-system und verfahren zur erzeugung von sauerstoff durch tieftemperaturzerlegung von luft
EP4150274A1 (en) * 2020-05-15 2023-03-22 Praxair Technology, Inc. Enhancements to a moderate pressure nitrogen and argon producing cryogenic air separation unit
CN112781321B (zh) * 2020-12-31 2022-07-12 乔治洛德方法研究和开发液化空气有限公司 一种具有氮液化器的空气分离装置和方法

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CN100420908C (zh) 2008-09-24
US20060021380A1 (en) 2006-02-02
CN1678875A (zh) 2005-10-05
WO2004023054A1 (fr) 2004-03-18
FR2844039B1 (fr) 2005-04-29
RU2319084C2 (ru) 2008-03-10
JP2005538335A (ja) 2005-12-15
UA85167C2 (ru) 2009-01-12
FR2844039A1 (fr) 2004-03-05
RU2005109412A (ru) 2005-10-10

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