US3751934A - Concentrating krypton and xenon in air separation by liquid oxygen wash - Google Patents

Concentrating krypton and xenon in air separation by liquid oxygen wash Download PDF

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US3751934A
US3751934A US00196447A US3751934DA US3751934A US 3751934 A US3751934 A US 3751934A US 00196447 A US00196447 A US 00196447A US 3751934D A US3751934D A US 3751934DA US 3751934 A US3751934 A US 3751934A
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liquid
rectifying column
column
xenon
oxygen
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K Frischbier
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    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02Processes 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
    • F25J3/04Processes 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
    • F25J3/04406Processes 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
    • F25J3/04412Processes 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
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02Processes 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
    • F25J3/04Processes 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
    • F25J3/04642Recovering noble gases from air
    • F25J3/04745Krypton and/or Xenon
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02Processes 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
    • F25J3/04Processes 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
    • F25J3/04763Start-up or control of the process; Details of the apparatus used
    • F25J3/04866Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04872Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04884Arrangement of reboiler-condensers
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00Processes or apparatus using separation by rectification
    • F25J2200/34Processes or apparatus using separation by rectification using a side column fed by a stream from the low pressure column
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00Processes or apparatus using other separation and/or other processing means
    • F25J2205/30Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00Details related to the use of reboiler-condensers
    • F25J2250/02Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10STECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00Refrigeration
    • Y10S62/923Inert gas
    • Y10S62/925Xenon or krypton

Definitions

  • the air separation plants they end up in the liquid oxygen.
  • the air contains such small proportions of these two rare gases that, first of all, a large volume of feed air is required in order to recover a measurable amount and, secondly, a process is required for concentrating these slight traces in the liquid oxygen.
  • This concentration represents the first intermediate step toward complete separation of the krypton and xenon from the oxygen. This invention is particularly directed to this first intermediate step.
  • the oxygen product is withdrawn in gaseous. form above the condenser-reboiler which connects the two rectifying columns. Since the liquid oxygen is vaporized completely,the krypton and xenon contained in the liquid oxygen escape with the gaseous oxygen product stream. Concentration of krypton and xenon in the liquid oxygen cannot be obtained in this manner.
  • the concentration of krypton in the liquid oxygen is about times larger at equilibrium than in the vapor.
  • the reflux ratio of liquid to vapor on the lowest trays of the oxygen section of an air separation plant is relatively high: 1.30 to 1.45.
  • the liquid portion amounts to about 70 percent of the air volume. Consequently, the rare gas portion (Kr X) therein. is about 1.5 ppm.
  • This liquid flows toward the lowermost barrier" trays.
  • the methane is prevented from leaving the barrier zone; and of all things it is the methane which gets into the air separator at relatively the highest concentration together with the process air. This is shown, almost without exception, by all air analyses. The amount is often 10 to 20 times larger than that of all other hydrocarbons combined.
  • the liquid oxygen containing krypton, xenon and hydrocarbons and drawn from the sump section of the rectifying column is conducted into a vessel provided with several rectifying trays, entering below the rectifying trays,
  • the krypton and xenon-enriched wash liquid is withdrawn from the bottom of the aforesaid vessel and returned to the sump of the rectifying column while liquid oxygen enriched in krypton, xenon and some hydrocarbons is withdrawn from the sump of the rectifying column for further concentration.
  • the barrier zone for the gaseous product oxygen is removed from the rectifying column and installed separately.
  • Another essential feature of the invention is that it is possible, by means of the liquid oxygen drawn from the sump section of the rectifying column, to adjust the reflux ratio in the separate barrier zone," i.e., on the rectifying trays of the separate vessel, to any desired value. Since the equilibrium constant K for methane is about twice as high as K for krypton, the reflux in the separate barrier zone" can be adjusted so that methane can escape with the gaseous phase, while krypton and xenon are still being washed out of the gas stream.
  • the basic idea of the invention is to provide a barrier" which, due to the reflux being variable within wide limits independently of the air separation plant, is a barrier" in the true sense of the word for the rare gases, krypton and xenon, but represents a continuously open hatch" for methane.
  • wash liquid for the separate barrier part of the liquid running off the lowest tray of the rectifying column is collected and withdrawn. This liquid has a lower rare gas content than that of the sump liquid in the rectifying column and is therefore most suitable as barrier liquid.
  • the low-pressure column of a double rectifying column serves as a suitable rectifying column.
  • the vaporization of the sump liquid may take place in the known manner by condensing nitrogen from the mediumpressure column in a tube condenser located within the double column between the low-pressure and mediumpressure columns.
  • a plate condenser of the type frequently used in modern plants. This plate condenser may be located outside the rectifying columns between the low-pressure and medium-pressure columns; therein, sump liquid from the low-pressure column is heated by condensing nitrogen vapor from the medium-pressure column. In such case, the sump liquid to be vaporized is pumped through the condenser in excess in order to prevent dry evaporation.
  • FIG. 1 is a flowsheet for the two-stage rectification of air, wherein the condenser-reboiler is located within a double rectifying column between the mediumpressure and low-pressure columns;
  • FIG. 2 is a partial flowsheet similar to that of FIG. 1, with a plate condenser-reboiler located outside the rectifying columns.
  • FIG. 1 shows the known double column consisting of medium-pressure column 1, low-pressure column 2 and condenser-reboiler 3 located between the two columns.
  • the air to be separated enters the plant through line 4, heats the sump liquid of medium-pressure column 1 by means of heating coil 5 and discharges into mediumpressure column 1 through line 6.
  • the resultant crude liquid oxygen enters low-pressure column 2 through line 7 and the liquid nitrogen through line 8.
  • pure nitrogen is withdrawn through line 9, while liquid oxygen enriched with krypton and xenon accumulates in the sump.
  • This sump liquid is vaporized by gaseous nitrogen in medium-pressure column l which condenses in condenser-reboiler 3.
  • the reflux ratio may be adjusted so that the amount of methane leaving the air separation plant with the gaseous product oxygen ls equal to the amount that enters the plant with the process feed air. In this way, a certain methane level will establish itself in the liquid oxygen.
  • the reflux ratio is reduced so that a lower level establishes itself in the liquid oxygen.
  • a loss of rare gases will occur only if the reflux ratio is reduced to a value which is lower than that required for retaining the rare gases; i.e., the liquid-to-vapor minimum is equal to K y/k l/l5 0.066.
  • the gaseeus product oxygen thus freed of krypton and xenon, then leaves separator 12 through line 17.
  • FIG. 2 shows a variation of the invention wherein heating of the sump liquid of the low-pressure column takes place in an aluminum plate condenser-reboiler located outside both rectifying columns, as is often the case in modern air separation plants. Similar plant components are makred in FIG. 2 with the same reference numerals used in FIG. 1.
  • Low-pressure column 2 has lines 7 and 8 which, respectively, feed liquid crude oxygen and liquid nitrogen from the medium-pressure column which is not shown. Part of the liquid oxygen containing krypton and xenon, which accumulates in the bottom of column 2, is withdrawn by pump and conducted into plate condenser-reboiler 22 through line 2i. There, the liquid oxygen is vaporized by condensing gaseous nitrogen from the medium-pressure column which enters through line 23 and leaves as liquid through line 24 and then is dumped in part into the top of low-pressure column 2 through line 8; the remainder of the liquid nitrogen leaving through line 24 returns to the top of the medium-pressure column as reflux.
  • the liquid oxygen is pumped through plate condenser-reboiler H2 in excess to prevent dry evaporation. Consequently, a liquid and vapor mixture enters separator 12 through line 25.
  • the gas rises through rectifying trays I3 countercurrent to the wash liquid which pump 24 withdraws through line 15 from channel 110 located at the level of the lowest rectifying tray in the bottom section of rectifying column 2.
  • Krypton and xenon are washed into the liquid accumulating in the bottom of separator 12 and are returned therewith to the sump of rectifying column 2 through line 18 and valve 16 which is used to control the liquid level.
  • a partial stream of the gaseous phase separated in separator 12 is not conducted up through rectifying trays 113 but is withdrawn through line 26 and returned into the bottom of low-pressure column 2. This partial stream provides the necessary reboil vapor for lowpressure coumn 2.
  • the krypton, xenon and hydrocarbons in this partial stream are washed out completely on the rectifying trays of low-pressure column 2 and end up in its sump. Again, as in the process of FIG.
  • a relatively high concentration of krypton and xenon in the liquid oxygen in the sump of low-pressure column 2 is obtained before the rising hydrocarbon content puts an end to any further concentration of krypton and xenon.
  • the concentrate is withdrawn through line 19 and subjected to further concentration processes which are known and do not form a part of this inventron.
  • the relatively high krypton and xenon concentration obtained in the first concentration by this invention reduces the cost of further concentration. Since a large percentage of the hydrocarbons leave the plant through line 117 together with the gaseous product oxygen, the known process for removing hydrocarbons from the krypton and xenon concentrate becomes simpler and cheaper as well.
  • the improvement of recovering a concentrate of krypton and xenon which comprises discharging into the top of a krypton and xenon concentrating rectifying column liquid oxygen containing small quantities of krypton, xenon and hydrocarbons drawn from a level near the bottom tray of said air rectifying column before said liquid oxygen flows into the sump of said air rectifying column, passing a stream of oxygen containing increased quantities of krypton, xenon and hydrocarbons from below the bottom tray in said air rectifying column to below the bottom tray in said concentrating rectifying column, adjusting the discharge of said liquid oxygen into the top of said concentrating rectifying column to provide a liquid-tovapor ratio at which krypton and xenon are substantially completely washed out of the vapor rising through said concentrating rectifying column, withdrawing gaseous oxygen containing some of said hydrocarbons but substantially free of krypton and xenon from the top of said concentrating rectifying column,

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)
US00196447A 1970-11-10 1971-11-08 Concentrating krypton and xenon in air separation by liquid oxygen wash Expired - Lifetime US3751934A (en)

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DE19702055099 DE2055099A1 (de) 1970-11-10 1970-11-10 Verfahren zur Anreicherung von Krypton und Xenon in Luftzerlegungsanlagen

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DE (1) DE2055099A1 (xx)
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NL (1) NL7113832A (xx)

Cited By (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4055625A (en) * 1974-07-31 1977-10-25 Commissariat A L'energie Atomique Method of treatment of a mixture of air and at least partially radioactive rare gases
US4401448A (en) * 1982-05-24 1983-08-30 Union Carbide Corporation Air separation process for the production of krypton and xenon
US4568528A (en) * 1984-08-16 1986-02-04 Union Carbide Corporation Process to produce a krypton-xenon concentrate and a gaseous oxygen product
US4574006A (en) * 1984-08-16 1986-03-04 Union Carbide Corporation Process to produce a krypton-xenon concentrate from a liquid feed
US4647299A (en) * 1984-08-16 1987-03-03 Union Carbide Corporation Process to produce an oxygen-free krypton-xenon concentrate
US4790866A (en) * 1986-11-24 1988-12-13 The Boc Group Plc Air separation
US5063746A (en) * 1991-02-05 1991-11-12 Air Products And Chemicals, Inc. Cryogenic process for the production of methane-free, krypton/xenon product
US5067976A (en) * 1991-02-05 1991-11-26 Air Products And Chemicals, Inc. Cryogenic process for the production of an oxygen-free and methane-free, krypton/xenon product
US5069698A (en) * 1990-11-06 1991-12-03 Union Carbide Industrial Gases Technology Corporation Xenon production system
US5122173A (en) * 1991-02-05 1992-06-16 Air Products And Chemicals, Inc. Cryogenic production of krypton and xenon from air
US5186007A (en) * 1990-10-13 1993-02-16 Kyodo Oxygen Co., Ltd. Controlled process for xenon concentration
US5309719A (en) * 1993-02-16 1994-05-10 Air Products And Chemicals, Inc. Process to produce a krypton/xenon enriched stream from a cryogenic nitrogen generator
US5313802A (en) * 1993-02-16 1994-05-24 Air Products And Chemicals, Inc. Process to produce a krypton/xenon enriched stream directly from the main air distillation column
US6164089A (en) * 1999-07-08 2000-12-26 Air Products And Chemicals, Inc. Method and apparatus for recovering xenon or a mixture of krypton and xenon from air
US6351970B1 (en) * 1998-05-26 2002-03-05 Linde Gas Aktiengesellschaft Method for extracting xenon
US6658894B2 (en) 2001-11-19 2003-12-09 Air Products And Chemicals, Inc. Process and adsorbent for the recovery of krypton and xenon from a gas or liquid stream
US6694775B1 (en) * 2002-12-12 2004-02-24 Air Products And Chemicals, Inc. Process and apparatus for the recovery of krypton and/or xenon
US20100037656A1 (en) * 2008-08-14 2010-02-18 Neil Mark Prosser Krypton and xenon recovery method
FR3020867A1 (fr) * 2014-05-07 2015-11-13 Air Liquide Procede et appareil de separation d’air par distillation cryogenique pour la production d’un melange de krypton et de xenon
RU2573432C2 (ru) * 2010-05-27 2016-01-20 Линде Акциенгезелльшафт Способ и устройство для разделения смеси веществ перегонкой
US20170030641A1 (en) * 2015-07-31 2017-02-02 Neil M. Prosser Method and apparatus for argon recovery in a cryogenic air separation unit integrated with a pressure swing adsorption system
US10012438B2 (en) 2015-07-31 2018-07-03 Praxair Technology, Inc. Method and apparatus for argon recovery in a cryogenic air separation unit integrated with a pressure swing adsorption system
US10012437B2 (en) 2015-07-31 2018-07-03 Praxair Technology, Inc. Method and apparatus for argon recovery in a cryogenic air separation unit integrated with a pressure swing adsorption system
US10066871B2 (en) 2015-07-31 2018-09-04 Praxair Technology, Inc. Method and apparatus for argon rejection and recovery
US11262125B2 (en) 2018-01-02 2022-03-01 Praxair Technology, Inc. System and method for flexible recovery of argon from a cryogenic air separation unit

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0218741B1 (en) * 1985-10-14 1989-12-13 Union Carbide Corporation Process to produce a krypton-xenon concentrate and a gaseous oxygen product
DE4332870C2 (de) * 1993-09-27 2003-02-20 Linde Ag Verfahren und Vorrichtung zur Gewinnung eines Krypton-/Xenon-Konzentrats durch Tieftemperaturzerlegung von Luft
DE102013017590A1 (de) 2013-10-22 2014-01-02 Linde Aktiengesellschaft Verfahren zur Gewinnung eines Krypton und Xenon enthaltenden Fluids und hierfür eingerichtete Luftzerlegungsanlage

Citations (7)

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US1963809A (en) * 1931-11-14 1934-06-19 Linde Eismasch Ag Process of obtaining constituents of air having a higher boiling point than oxygen
US2423274A (en) * 1945-07-06 1947-07-01 Air Reduction Recovery of the components of air
US2547177A (en) * 1948-11-02 1951-04-03 Linde Air Prod Co Process of and apparatus for separating ternary gas mixtures
US2824428A (en) * 1957-03-19 1958-02-25 Union Carbide Corp Process and apparatus for separating air
US3127260A (en) * 1964-03-31 Separation of air into nitrogen
US3264830A (en) * 1963-08-09 1966-08-09 Air Reduction Separation of the elements of air
US3596471A (en) * 1968-03-15 1971-08-03 Messer Griesheim Gmbh Process for recovering a mixture of krypton and xenon from air with argon stripper

Patent Citations (7)

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Publication number Priority date Publication date Assignee Title
US3127260A (en) * 1964-03-31 Separation of air into nitrogen
US1963809A (en) * 1931-11-14 1934-06-19 Linde Eismasch Ag Process of obtaining constituents of air having a higher boiling point than oxygen
US2423274A (en) * 1945-07-06 1947-07-01 Air Reduction Recovery of the components of air
US2547177A (en) * 1948-11-02 1951-04-03 Linde Air Prod Co Process of and apparatus for separating ternary gas mixtures
US2824428A (en) * 1957-03-19 1958-02-25 Union Carbide Corp Process and apparatus for separating air
US3264830A (en) * 1963-08-09 1966-08-09 Air Reduction Separation of the elements of air
US3596471A (en) * 1968-03-15 1971-08-03 Messer Griesheim Gmbh Process for recovering a mixture of krypton and xenon from air with argon stripper

Cited By (38)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4055625A (en) * 1974-07-31 1977-10-25 Commissariat A L'energie Atomique Method of treatment of a mixture of air and at least partially radioactive rare gases
US4401448A (en) * 1982-05-24 1983-08-30 Union Carbide Corporation Air separation process for the production of krypton and xenon
EP0096610A1 (en) * 1982-05-24 1983-12-21 Union Carbide Corporation Air separation process for the production of krypton and xenon
US4568528A (en) * 1984-08-16 1986-02-04 Union Carbide Corporation Process to produce a krypton-xenon concentrate and a gaseous oxygen product
US4574006A (en) * 1984-08-16 1986-03-04 Union Carbide Corporation Process to produce a krypton-xenon concentrate from a liquid feed
US4647299A (en) * 1984-08-16 1987-03-03 Union Carbide Corporation Process to produce an oxygen-free krypton-xenon concentrate
US4790866A (en) * 1986-11-24 1988-12-13 The Boc Group Plc Air separation
US5186007A (en) * 1990-10-13 1993-02-16 Kyodo Oxygen Co., Ltd. Controlled process for xenon concentration
US5069698A (en) * 1990-11-06 1991-12-03 Union Carbide Industrial Gases Technology Corporation Xenon production system
US5067976A (en) * 1991-02-05 1991-11-26 Air Products And Chemicals, Inc. Cryogenic process for the production of an oxygen-free and methane-free, krypton/xenon product
US5122173A (en) * 1991-02-05 1992-06-16 Air Products And Chemicals, Inc. Cryogenic production of krypton and xenon from air
US5063746A (en) * 1991-02-05 1991-11-12 Air Products And Chemicals, Inc. Cryogenic process for the production of methane-free, krypton/xenon product
US5309719A (en) * 1993-02-16 1994-05-10 Air Products And Chemicals, Inc. Process to produce a krypton/xenon enriched stream from a cryogenic nitrogen generator
US5313802A (en) * 1993-02-16 1994-05-24 Air Products And Chemicals, Inc. Process to produce a krypton/xenon enriched stream directly from the main air distillation column
EP0611935A1 (en) * 1993-02-16 1994-08-24 Air Products And Chemicals, Inc. Process to produce a krypton/xenon enriched stream directly from the main air distillation column
US6351970B1 (en) * 1998-05-26 2002-03-05 Linde Gas Aktiengesellschaft Method for extracting xenon
US6164089A (en) * 1999-07-08 2000-12-26 Air Products And Chemicals, Inc. Method and apparatus for recovering xenon or a mixture of krypton and xenon from air
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NL7113832A (xx) 1972-05-15
DE2055099A1 (de) 1972-05-18
FR2113843B3 (xx) 1974-02-15
FR2113843A3 (xx) 1972-06-30
JPS5536905B1 (xx) 1980-09-24

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