[go: up one dir, main page]

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

Info

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
Authority
US
United States
Prior art keywords
stream
column
oxygen
pressure column
withdrawing
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.)
Abandoned
Application number
US10/527,002
Inventor
Lasad Jaouani
Frederic 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 a Directoire et Conseil de Surveillance 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 a Directoire et Conseil de Surveillance pour lEtude et lExploitation des Procedes Georges Claude filed Critical LAir Liquide SA a Directoire et Conseil de Surveillance pour lEtude et lExploitation des Procedes Georges Claude
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
Abandoned legal-status Critical Current

Links

Images

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 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.

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)

Abstract

A method and an apparatus for producing oxygen and noble gases by cryogenic distillation. A first stream of cooled and purified air is sent to a medium pressure column where it is separated. A first nitrogen enriched stream is withdrawn from the medium pressure column, and part of this stream is sent to a low pressure column. An intermediate stream is withdrawn from an intermediate level of the medium pressure column. This intermediate stream is then sent to the low pressure column. A stream, which is enriched in oxygen relative to the intermediate stream, is withdrawn from the bottom of the medium pressure column and sent to an auxiliary column. The auxiliary column also receives at liquid stream of nitrogen which is used for reflux. A second nitrogen rich stream is withdrawn from the top of the low pressure column. A second oxygen rich liquid stream, which is suitable for use as a product, is withdrawn from the low pressure column. Finally, a final oxygen enriched stream which is also enriched with krypton and xenon, is withdrawn from the auxiliary column.

Description

  • 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.
  • However, in the case of a unit producing oxygen by what are called “pumped” methods, about 30% of the krypton and of the xenon present in the air are “lost” in the liquid oxygen withdrawn from the low-pressure column.
  • 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:
      • i) at least one stream of cooled and purified air is sent to the medium-pressure column where it is separated;
      • ii) at least a first nitrogen-enriched stream is withdrawn from the medium-pressure column and at least one portion of this stream is sent directly or indirectly to the low-pressure column;
      • iii) an intermediate stream is withdrawn from an intermediate level of the medium-pressure column;
      • iv) a stream, enriched with oxygen relative to the intermediate stream, is withdrawn from the bottom of the medium-pressure column and sent to the bottom of the auxiliary column;
      • v) a nitrogen-rich stream is withdrawn from the top of the low-pressure column;
      • vi) an oxygen-rich liquid stream is withdrawn from the low-pressure column as product, optionally after a vaporization step in order to form a gaseous product; and
      • vii) an oxygen-enriched stream, which is also enriched with krypton and with xenon relative to the second oxygen-enriched stream, is withdrawn from the auxiliary column, characterized in that the intermediate stream is sent to the low-pressure column and a liquid stream containing at least 78 mol % nitrogen is sent as reflux to the auxiliary column.
  • Preferably, 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. According to optional aspects:
      • the bottom of the auxiliary column is heated by an overhead gas from an argon column;
      • the liquefied air and/or the liquid enriched with nitrogen relative to the air is produced by heat exchange with the oxygen-rich liquid stream coming from the bottom of the low-pressure column, optionally after a pressurization step;
      • the nitrogen-enriched liquid contains at least 80 mol % nitrogen;
      • the liquefied air does not come from the medium-pressure column, the liquid stream sent to the top of the auxiliary column is richer in nitrogen than the intermediate stream; at least 10% of the oxygen produced is withdrawn in liquid form from the low-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:
      • i) means for sending at least one stream of cooled and purified air to the medium-pressure column where it is separated;
      • ii) means for withdrawing at least a first nitrogen-enriched stream from the medium-pressure column and means for sending at least one portion of this stream directly or indirectly to the low-pressure column;
      • iii) means for withdrawing a nitrogen-rich stream from the top of the low-pressure column;
      • iv) means for withdrawing an intermediate stream from an intermediate level of the medium-pressure column;
      • v) means for sending a stream, richer in oxygen than the intermediate stream, from the bottom of medium-pressure column into the bottom of the auxiliary column;
      • vi) means for sending a liquid stream as reflux to the auxiliary column;
      • vii) means for withdrawing an oxygen-rich liquid stream from the bottom of the low-pressure column as product, optionally after a vaporization step in order to form a gaseous product; and
      • viii) means for withdrawing a third oxygen-enriched stream, which is also enriched with krypton and with xenon relative to the second oxygen-enriched stream, from the auxiliary column,
        characterized in that it includes means for sending, as reflux stream to the auxiliary column, liquefied air or a liquid stream enriched with nitrogen relative to a liquid air stream sent to the medium-pressure column.
  • According to other optional aspects, the plant includes:
      • a purification column, means for sending the third oxygen-enriched stream into the top of the purification column and means for withdrawing a fourth oxygen-enriched stream, constituting a mixture enriched with krypton and xenon, at least a few theoretical stages lower down in the column; and
      • an exchange line in which the liquefied air and/or the liquid enriched with nitrogen relative to the air is produced by heat exchange with the oxygen-rich liquid stream coming from the bottom of the low-pressure column, optionally after a pressurization step.
  • The invention will now be described with reference to FIGS. 1 to 9, which are diagrams showing the principle of plants according to the invention.
  • In the example shown in FIG. 1, a double air separation column comprises a medium-pressure column K01 and a low-pressure column K02 that are thermally coupled by means of a principal vaporizer E02 that is used to condense at least part of the gaseous overhead nitrogen of the column K01 by heat exchange with oxygen from the bottom of the column K02.
  • An argon column K10 is fed with an argon-enriched fluid 7 coming from the low-pressure column K02 and an argon-enriched liquid 9 is returned from the argon column K10 to the low-pressure column K02. An argon-rich stream ARGON is withdrawn from the top of the column K10.
  • In the case of pumped units, 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 K01, the low-pressure column K02 and the auxiliary column K05, 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 K01.
  • The principle of the present invention is to concentrate the krypton and the xenon in a rich liquid RL2, which will then be treated in an auxiliary column K05.
  • Two rich liquids RL1 and RL2 are therefore withdrawn from the medium-pressure column K01, 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, RL1, and a rich bottoms liquid concentrated with krypton and xenon, RL2. This “conventional” rich liquid RL1 can then be sent to the column K02 after having been subcooled.
  • The rich bottoms liquid RL2 is sent to the K10 argon mixture condenser E10 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 K05. A portion of the reflux from this column is provided by a portion 5 of the liquid air LIQ AIR not feeding the column K01, 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 K02 via the line 13 and containing at least 80 mol % nitrogen. A gas 16 is withdrawn from the intermediate level of the column K05 below the points of reflux injection, and constitutes the vaporized rich liquid. It is then recycled in the column K02. The overhead gas WN2′ from the column K05 constitutes a portion of the waste gas WN2 leaving the cold box.
  • The purge PURGE from the mixture condenser E10 contains most of the krypton and xenon that are present in the air and have been treated by the columns K01 and K05. This flow feeds a device for concentrating the rare gases. For example, it may be sent into the weak krypton/xenon mixture column (K90). The bottom of this column contains the product to be beneficiated. The vapor 17 coming from the column K90 is sent back into the bottom of the column K05.
  • The column K90 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 K01 and/or to the low-pressure column K02.
  • The production of liquid oxygen LO is withdrawn as bottoms from the column K02, level with the principal vaporizer E02. Unlike the conventional scheme for krypton and xenon production, 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. Alternatively, a nitrogen cycle may serve to vaporize the liquid oxygen LO.
  • In the following figures, various alternative embodiments deriving from FIG. 1 will be presented. The elements common with FIG. 1 will not be described a second time.
  • In the case of FIG. 2, all of the liquid air LIQ AIR coming from the main exchange line is sent into the column K01. An intermediate fluid in liquid form 1′ is withdrawn from the column K01 (preferably at the level where the liquid air is introduced or at a level above this level). Next, after having been subcooled, it is distributed between the column K02 and the column K05 as two streams 3 and 5. Stream 11 containing at least 80 mol % nitrogen is sent to the top of the column K05.
  • In the case of FIG. 3, based on FIG. 1, one top section of the column K05 has been removed. The reflux from this column is provided only by liquid air 5, preferably subcooled. This liquid air is produced by vaporization of the liquid oxygen LO pumped and vaporized in the exchange line. All the lean liquid 13 is sent to the low-pressure column K02.
  • In addition, all of the liquid air LIQ AIR present at the outlet of the exchange line can be withdrawn from the column K01 (preferably at the point of introduction of the liquid air) and then distributed between the column K02 and the column K05 after having been subcooled, as shown in FIG. 4.
  • In the case of FIGS. 5 and 6, based on FIGS. 3 and 4, the waste gas WN2′ from the column K05 is sent back into the column K02 below the point of injection of the lean liquid 13.
  • In the case of FIG. 7, based on FIG. 5, the stream 16 is omitted and replaced with a stream of waste nitrogen WN2′ sent from the top of the auxiliary column K05 to an intermediate point on the low-pressure column.
  • In all the figures described above (FIGS. 1 to 7), it is possible to couple the plant with the conventional scheme for producing krypton and xenon. To do this, it is necessary to install stages for enrichment of the bottom in the column K02. The liquid oxygen LO is produced a few stages above the principal vaporizer E02. A purge 21 is withdrawn level with the principal vaporizer E02. It contains about 70 mol % krypton and all of the xenon present in the column K02. It is sent to the column K90 in order to recover the rare gases.
  • An example is given in FIG. 8.
  • In all the above figures (FIGS. 1 to 8), the coproduction of argon is mentioned. However, it is possible to fit the plants described above to a unit that does not produce argon. For example, it is sufficient to install an exchanger for condensing a fraction of the gas 7 withdrawn from the column K02. Once liquefied, it is sent (9) into the column K02. This thus provides the reboiling in the column K05.
  • An example is given in FIG. 9.
  • In the case of a scheme with a blowing turbine, the blown air is sent into the bottom of the column K05 so as to recover the krypton and xenon that it contains.
  • In addition, 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). In this case, it is possible to modify the top condenser of an Etienne column, by replacing the argon column K10 of FIGS. 1 to 9 with an Etienne column according to the same principle: addition of stages above the condenser in order to concentrate the rare gases.
  • It is perhaps also advantageous not to send all of the liquid air into the top of the auxiliary column but to introduce, at this inlet of the column, only a stream that ensures an L/V (the ratio of the falling liquid flow rate to the rising gas flow rate in the distillation section) needed to concentrate the Kr and Xe in the bottom of K05, thereby limiting the oxygen concentration in the bottom of K05. The remainder of the liquid air stream is then sent, with the rich liquid RL2, into the bottom of the auxiliary column.

Claims (19)

1-12. (canceled)
13. A method which may be used producing oxygen and rare gases by distillation, said method comprising:
a) separating at least one stream of cooled and purified air in a medium pressure column;
b) withdrawing at least a first nitrogen enriched stream from said medium pressure column;
c) sending at least part of said first nitrogen enriched stream to a low pressure column;
d) withdrawing an intermediate stream from an intermediate level of said medium pressure column;
e) withdrawing a first oxygen enriched stream from the bottom of said medium pressure column, wherein said first oxygen enriched stream is richer in oxygen than said intermediate stream;
f) sending said first oxygen enriched stream to the bottom of at least one auxiliary column;
g) withdrawing a second nitrogen rich stream from the top of said low pressure column;
h) withdrawing a second oxygen rich liquid stream from said low pressure column;
i) withdrawing a third oxygen enriched stream from said auxiliary column, wherein said third oxygen enriched stream is also enriched with xenon and krypton as compared to said second oxygen rich stream;
j) sending said intermediate stream to said low pressure column; and
k) sending at least one liquid reflux stream to said auxiliary column, wherein said reflux stream comprises about 78 mol % nitrogen.
14. The method of claim 13, further comprising vaporizing said second oxygen rich liquid stream to obtain a gaseous product.
15. The method of claim 13, further comprising indirectly sending at least part of said first nitrogen enriched stream to said low pressure column.
16. The method of claim 13, further comprising:
a) sending said third oxygen enriched stream to the top of a purification column; and
b) withdrawing a final oxygen enriched stream from a final location on said purification column, wherein:
1) said final oxygen enriched stream comprises a mixture enriched with krypton and xenon; and
2) said final location is at least about three theoretical stages down from the top of said purification column.
17. The method of claim 13, wherein said liquid reflux stream comprises at least one member selected from the group consisting of:
a) liquefied air; and
b) a liquid stream richer in nitrogen than a liquid air stream which is sent to said medium pressure column.
18. The method of claim 13, wherein the bottom of said auxiliary column is heated by an overhead gas from an argon column.
19. The method of claim 17, further comprising producing said liquid reflux stream by heat exchange with said second oxygen rich liquid stream.
20. The method of claim 19, wherein said heat exchange takes place after a pressurization step.
21. The method of claim 17, wherein said reflux stream comprises at least about 80 mol % nitrogen.
22. The method of claim 17, wherein said liquefied air does not originate from said medium pressure column.
23. The method of claim 13, wherein said reflux stream is richer in nitrogen than said intermediate stream.
24. The method of claim 13, further comprising withdrawing at least about 10% of all the oxygen produced by said method from said low pressure column.
25. An apparatus which may be used for producing oxygen and rare gases by distillation, said apparatus comprising:
a) at least one medium pressure column;
b) a low pressure column;
c) an auxiliary column;
d) a first distribution means for sending at least one stream of cooled and purified air to said medium pressure column, wherein said cooled and purified stream is then separated;
e) a first withdrawing means for withdrawing at least a first nitrogen enriched stream from said medium pressure column;
f) a second distribution means for sending at least a portion of said first nitrogen enriched stream to said low pressure column;
g) a second withdrawing means for withdrawing a second nitrogen rich stream from the top of said low pressure column;
h) a third withdrawing means for withdrawing an intermediate stream from an intermediate level of said medium pressure column;
i) a third distribution means for sending a first oxygen enriched stream from said medium pressure column to said auxiliary column, wherein said first oxygen enriched stream is richer in oxygen than said intermediate stream;
j) a fourth distribution means for sending a liquid reflux stream to said auxiliary column;
k) a fourth withdrawing means for withdrawing a second oxygen rich stream from the bottom of said low pressure column, wherein said second oxygen rich stream is withdrawn as a liquid and is suitable for use as product;
l) a fifth withdrawing means for withdrawing a third oxygen enriched stream from said auxiliary column, wherein:
1) said third oxygen enriched stream is richer in krypton and xenon than said second oxygen rich stream; and
2) said fifth withdrawing means comprises a fifth distribution means for sending a second reflux stream to said auxiliary column, wherein said second reflux stream comprises at least one member selected from the group consisting of:
i) liquefied air; and
ii) a liquid stream richer in nitrogen than a liquid air stream which is sent to said medium pressure column.
26. The apparatus of claim 25, wherein said second oxygen rich liquid stream is vaporized prior to withdrawal in order to obtain a gaseous product.
27. The apparatus of claim 25, wherein said second distribution means indirectly sends at least a portion of said first nitrogen enriched stream to said low pressure column.
28. The apparatus of claim 25, further comprising:
a) a purification column;
b) a purification distribution means for sending said third oxygen enriched stream into the top of said purification column;
c) a purification withdraw means for withdrawing a final oxygen enriched stream, wherein:
1) said final oxygen enriched stream comprises a mixture enriched with krypton and xenon; and
2) said final oxygen enriched stream is withdrawn at least about three theoretical stages down from the top of said purification column.
29. The apparatus of claim 25, further comprising an exchange line, wherein said second reflux stream is produced in said exchange line by heat exchange with fourth oxygen rich stream.
30. The apparatus of claim 29, wherein said second reflux stream is produced after a pressurization step.
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
FR0210922A FR2844039B1 (en) 2002-09-04 2002-09-04 PROCESS AND PLANT FOR PRODUCING OXYGEN AND RARE GASES BY CRYOGENIC AIR DISTILLATION
FR02/10922 2002-09-04
PCT/FR2003/002420 WO2004023054A1 (en) 2002-09-04 2003-07-30 Method and installation for production of noble gases and oxygen by means of cryogenic air distillation

Publications (1)

Publication Number Publication Date
US20060021380A1 true US20060021380A1 (en) 2006-02-02

Family

ID=31503096

Family Applications (1)

Application Number Title Priority Date Filing Date
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

Country Status (8)

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

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 (en) 2006-05-11 2012-08-01 Raindance Technologies, Inc. Microfluidic devices
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 (en) * 2015-03-13 2016-09-14 Linde Aktiengesellschaft Distillation column system and method for the production of oxygen by cryogenic decomposition of 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
JP2010538236A (en) * 2007-08-30 2010-12-09 リンデ・エルエルシー Method for producing a sterile cryogenic fluid
RU2481658C2 (en) * 2011-06-30 2013-05-10 Александр Прокопьевич Елохин Concentration and utilisation method and system of inert radioactive gases from gas-aerosol emissions of power units of nuclear power plants
RU2528786C1 (en) * 2013-03-20 2014-09-20 Открытое акционерное общество "Газпром" Methods for two-step fractionation separation of inert gases from tail gases and apparatus therefor
RU2528792C1 (en) * 2013-03-20 2014-09-20 Открытое акционерное общество "Газпром" Method for single-step fractionation separation of inert gases from tail gases and apparatus therefor
FR3013431B1 (en) * 2013-11-21 2018-11-09 L'air Liquide,Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION
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
CN112781321B (en) * 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 Air separation device with nitrogen liquefier and method

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2051576A (en) * 1936-04-06 1936-08-18 Air Reduction Recovery of krypton and xenon
US4401448A (en) * 1982-05-24 1983-08-30 Union Carbide Corporation Air separation process for the production of krypton and xenon
US4647299A (en) * 1984-08-16 1987-03-03 Union Carbide Corporation Process to produce an oxygen-free krypton-xenon concentrate
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
US6612129B2 (en) * 2001-10-31 2003-09-02 Linde Aktiengesellschaft Process and apparatus for producing krypton and/or xenon by low-temperature fractionation of air

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2605305A1 (en) * 1976-02-11 1977-08-18 Messer Griesheim Gmbh Separation of krypton and xenon from crude oxygen - by taking fraction from base of medium pressure column
DE19855486A1 (en) * 1998-12-01 1999-06-10 Linde Ag Extraction of krypton or xenon-rich mixture
RU2146552C1 (en) * 1999-08-30 2000-03-20 Савинов Михаил Юрьевич Method of production of krypton-zenon concentrate and device for its embodiment
DE10000017A1 (en) * 1999-11-22 2000-06-29 Linde Ag Process for recovery of krypton and/or xenon comprises removing oxygen-enriched fraction from the pressure column at an intermediate point

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2051576A (en) * 1936-04-06 1936-08-18 Air Reduction Recovery of krypton and xenon
US4401448A (en) * 1982-05-24 1983-08-30 Union Carbide Corporation Air separation process for the production of krypton and xenon
US4647299A (en) * 1984-08-16 1987-03-03 Union Carbide Corporation Process to produce an oxygen-free krypton-xenon concentrate
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
US6612129B2 (en) * 2001-10-31 2003-09-02 Linde Aktiengesellschaft Process and apparatus for producing krypton and/or xenon by low-temperature fractionation of air

Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2481815A1 (en) 2006-05-11 2012-08-01 Raindance Technologies, Inc. Microfluidic devices
US20080289362A1 (en) * 2007-05-24 2008-11-27 Stefan Lochner Process and apparatus for low-temperature air fractionation
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
US8443625B2 (en) 2008-08-14 2013-05-21 Praxair Technology, Inc. Krypton and xenon recovery method
US20100037656A1 (en) * 2008-08-14 2010-02-18 Neil Mark Prosser Krypton and xenon recovery method
WO2010019308A3 (en) * 2008-08-14 2013-11-21 Praxair Technology, Inc. Krypton and xenon recovery method
US20100071412A1 (en) * 2008-09-22 2010-03-25 David Ross Parsnick Method and apparatus for producing high purity oxygen
US8479535B2 (en) 2008-09-22 2013-07-09 Praxair Technology, Inc. Method and apparatus for producing high purity oxygen
US20110126585A1 (en) * 2009-12-02 2011-06-02 David Ross Parsnick Krypton xenon recovery from pipeline oxygen
US8484992B2 (en) 2009-12-02 2013-07-16 Praxair Technology, Inc. Krypton xenon recovery from pipeline oxygen
WO2011068634A2 (en) 2009-12-02 2011-06-09 Praxair Technology, Inc. Krypton xenon recovery from pipeline oxygen
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
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
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
EP3067649A1 (en) * 2015-03-13 2016-09-14 Linde Aktiengesellschaft Distillation column system and method for the production of oxygen by cryogenic decomposition of 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
US12104850B2 (en) * 2021-05-06 2024-10-01 Air Products And Chemicals, Inc. Fluid recovery process and apparatus for xenon and or krypton recovery

Also Published As

Publication number Publication date
JP2005538335A (en) 2005-12-15
CN100420908C (en) 2008-09-24
WO2004023054A1 (en) 2004-03-18
RU2005109412A (en) 2005-10-10
CN1678875A (en) 2005-10-05
FR2844039B1 (en) 2005-04-29
UA85167C2 (en) 2009-01-12
RU2319084C2 (en) 2008-03-10
FR2844039A1 (en) 2004-03-05
EP1552230A1 (en) 2005-07-13

Similar Documents

Publication Publication Date Title
US20060021380A1 (en) Method and installation for production of noble gases and oxygen by means of cryrogenic air distillation
US8826692B2 (en) Method and device for low-temperature air separation
JP2003165712A (en) Method and apparatus for producing krypton and/or xenon by low-temperature air separation
US5682764A (en) Three column cryogenic cycle for the production of impure oxygen and pure nitrogen
EP0793069A1 (en) Dual purity oxygen generator with reboiler compressor
EP1134526A2 (en) Process for the production of oxygen and nitrogen
JP2002327982A (en) Three-tower type air-separation installation, argon- production method and system with crude argon tower
KR100790911B1 (en) Method and apparatus for separating air by cryogenic distillation
US5123947A (en) Cryogenic process for the separation of air to produce ultra high purity nitrogen
EP0823606B1 (en) Process to produce nitrogen using a double column plus an auxiliary low pressure separation zone
US6536232B2 (en) Method for plant and separating air by cryogenic distillation
KR100660243B1 (en) Process and apparatus for producing pressurized oxygen and krypton/xenon by low-temperature fractionation of air
JP4540182B2 (en) Cryogenic distillation system for air separation
JP2001349669A (en) Method and apparatus for manufacturing oxygen-rich fluid by low temperature distillation
JP2000346547A (en) Cryogenic distillation for separating air
KR100775877B1 (en) Cryogenic Distillation Unit for Air Separation
US20060075779A1 (en) Process for the cryogenic distillation of air
US6662593B1 (en) Process and apparatus for the cryogenic separation of air
CN106016969B (en) System and method for generating oxygen by cryogenic air separation
JP3097064B2 (en) Ultra-pure liquid oxygen production method
US11602713B2 (en) Method for cryogenic separation of air, and air separation plant
JP2007064617A (en) Method of manufacturing krypton and/or xenon by cryogenic air separation
US5768914A (en) Process to produce oxygen and argon using divided argon column
US6318120B1 (en) Cryogenic distillation system for air separation
US6385996B2 (en) Process and installation for separation of air by cryogenic distillation

Legal Events

Date Code Title Description
AS Assignment

Owner name: L'AIR LIQUIDE, SOCIETE ANONYME A DIRECTOIRE ET CON

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:JAOUANI, LASAD;JUDAS, FREDERIC;SAULNIER, BERNARD;REEL/FRAME:017060/0767

Effective date: 20050221

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION