EP3207320A1 - Procédé et dispositif de récupération variable d'argon par fractionnement à basse température - Google Patents

Procédé et dispositif de récupération variable d'argon par fractionnement à basse température

Info

Publication number
EP3207320A1
EP3207320A1 EP15771022.9A EP15771022A EP3207320A1 EP 3207320 A1 EP3207320 A1 EP 3207320A1 EP 15771022 A EP15771022 A EP 15771022A EP 3207320 A1 EP3207320 A1 EP 3207320A1
Authority
EP
European Patent Office
Prior art keywords
argon
column
gaseous
crude
pure
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.)
Granted
Application number
EP15771022.9A
Other languages
German (de)
English (en)
Other versions
EP3207320B1 (fr
Inventor
Stefan Lochner
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.)
Linde GmbH
Original Assignee
Linde GmbH
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 Linde GmbH filed Critical Linde GmbH
Priority to PL15771022T priority Critical patent/PL3207320T3/pl
Publication of EP3207320A1 publication Critical patent/EP3207320A1/fr
Application granted granted Critical
Publication of EP3207320B1 publication Critical patent/EP3207320B1/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

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
    • F25J3/04406—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
    • F25J3/04648—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
    • F25J3/04703—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 being arranged in more than one vessel
    • 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
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude argon
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/58—Processes or apparatus involving steps for recycling of process streams the recycled stream being argon or crude argon

Definitions

  • the invention relates to a method according to the preamble of patent claim 1.
  • the crude argon column can be carried out in one part or in several parts. It has a top condenser, which is cooled with a liquid from the air separation process in the strict sense, in particular with bottom liquid of the high-pressure column. Usually, the entire liquid pure argon product stream is withdrawn from the bottom of the pure argon column as the final product. For example, the final product is recovered directly as a liquid product and introduced into a liquid tank.
  • the liquid from the pure argon column or from the tank is taken out of the liquid from the pure argon column or from the tank, brought to liquid pressure and warmed in the main heat exchanger and fed directly to a consumer as compressed gas product.
  • the argon is often sold as a liquid product.
  • the invention has for its object to increase in a process mentioned above, the efficiency of oxygen production at relative to the main product demand fluctuating argon demand. Under "efficiency" of oxygen separation is here
  • Top condenser the pure argon column or the top condenser deducted to reduce pure argon production or shut down completely.
  • the gaseous argon return stream is warmed without mixing with another stream in a separate passage of the main heat exchanger.
  • the gaseous argon reflux has an argon content that is at least twice that of the argon-enriched stream from the low pressure column (measured in molar quantities).
  • the cold contained in it is in the
  • Recovered main heat exchanger by at least one of the following measures: - A portion of the gaseous argon reflux is introduced according to a variant of the invention in a return flow from the low pressure column.
  • the gaseous argon return stream is warmed without mixing with another stream in a separate passage of the main heat exchanger.
  • the crude argon column or a part of it can be driven with variable throughput of argon at a constant rate or with the nominal or maximum throughput for which the process is designed.
  • the oxygen yield and the oxygen purity remain constant high.
  • the entire amount of pure argon product is removed as the final product.
  • the "second mode of operation" may then be formed by any mode in which the final product quantity is less than in the first mode of operation.
  • the excess portion of the pure argon product amount is then as gasfömiger argon reflux back before the pure argon column or from the
  • the part of the gaseous argon reflux can be mixed with any return flow from the low pressure column, if this is possible from the pressure level.
  • at least one of the following reflux streams is selected:
  • Evaporative coolers are used meaningfully.
  • the absolute total amount of argon taken from the crude argon column and the pure argon column is maintained substantially constant.
  • substantially constant is meant a deviation of less than 5 mol%, in particular less than 2.5%.
  • Argon product amount and the amount of argon contained in the residual gas from the head of the pure argon column For example, if no argon product is recovered at all in the second mode of operation, the argon contained in the argon back or streams and the amount of argon contained in the tail gas from the top of the pure argon column add up to the total argon volume.
  • the gaseous argon reflux is through at least part of the
  • the gaseous argon return stream is withdrawn from an intermediate point of the crude argon column, ie with a higher argon content than the crude argon fraction.
  • the gaseous argon reflux can also:
  • the gaseous argon return stream are withdrawn from the top of the first section of the crude argon column.
  • Atmospheric air is drawn in by a filter 2 from an air compressor 3.
  • the compressed air 4 from the air compressor 3 is cooled in a pre-cooler 5 and cleaned in a cleaning device 6.
  • the purified air 7 becomes one
  • Main heat exchanger 8 supplied.
  • a first cold air stream 9 is introduced in gaseous form into the high-pressure column 10.
  • the high-pressure column 10 is part of a double column, which also has a low-pressure column 11 and a main capacitor 12. These apparatus are part of a distillation column system.
  • a second cold air stream 13 which may have been branched off from the stream 7 and compressed to a high pressure, is expanded in a valve 14 and, for the most part, introduced into the high-pressure column 10 in liquid form (15). A portion 16 of this liquid is immediately withdrawn, cooled in a supercooling countercurrent 17 and introduced via line 8 into the low-pressure column 11.
  • oxygen-enriched fraction 19 from the bottom of the high-pressure column 10 is cooled in the subcooling countercurrent 17.
  • the cooled oxygenated fraction 20 is added to a first part 21 by the sump heater 91 of FIG.
  • a portion of the head of nitrogen 25 of the high-pressure column 10 is condensed in the main condenser 12 and fed to a first part 26 on the high-pressure column.
  • One second portion 27 of the liquid nitrogen flows through the subcooling countercurrent 17 and through line 28 to the top of the low pressure column.
  • GAN-EC Gaseous compressed nitrogen outside
  • An argon-enriched stream 80 from the low-pressure column 11 is introduced into a crude argon column, which in the example is formed as a divided crude argon column with two sections 81, 82.
  • first operating mode the overhead vapor 70 of the first section 81 is completely introduced into the second section 82 via line 70a.
  • Head condenser 90 return fluid is generated.
  • the liquid 87 arriving in the bottom of the second section 82 is fed by means of a pump 88 via line 89 to the top of the first section 81.
  • the liquid 84, which collects in the bottom of the first section 81, is also pumped and returned via line 6 in the low-pressure column 1 1.
  • a gaseous crude argon fraction 71 is removed and introduced in full gaseous into the pure argon column 83.
  • a liquid pure argon product stream 72 is removed.
  • a residual gas stream 73 is withdrawn and blown off into the atmosphere (ATM).
  • the gaseous argon reflux or a portion of it is formed by a portion of the overhead vapor 70 of the first section 81 of the crude argon column. It is guided by means of the lines 101, 102a, 105, 106, 107 through the separate passage 108 of the main heat exchanger. A portion 102b may be introduced into the impurity nitrogen 32 downstream of the subcooling countercurrent 17; alternatively, the introduction may be performed upstream of the subcooling countercurrent 17.
  • the gaseous argon reflux is formed by a part of the crude argon fraction 71 or by the entire crude argon fraction 71 and passed via the lines 103, 104, 106 into the separate passage 108 of the main heat exchanger. Some of it may be diverted into the gaseous nitrogen product stream 30 downstream of the subcooling countercurrent 17 (lines 103, 104, 105); Alternatively, the introduction
  • Main heat exchanger 8 understood that flows through the same stream.
  • Main heat exchanger 8 are combined.
  • the line 101 is opened and 0 to 3.5% of the overhead vapor 70 or the rising vapor in the crude argon column 81, 82 are fed into the main heat exchanger 8.
  • the "second pure argon product amount" is thus 70% of the maximum argon product.
  • the argon return stream 101 then comprises, for example, 1% of the overhead vapor 70.
  • the remainder of the head vapor 70 of the Rohargonklale is further introduced via line 70a in the second section 82 of the crude argon column.

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

L'invention concerne un procédé et un dispositif permettant la récupération variable d'argon par fractionnement à basse température. De l'air de charge (1, 4, 7) est refroidi dans un échangeur de chaleur principal (8) puis dans un système de colonnes de distillation, qui comporte une colonne haute pression (10) et une colonne basse pression (11). Au cours d'une récupération d'argon au moyen d'une colonne d'argon brut (81, 82) d'une colonne d'argon pur (3), un flux de produit liquide d'argon pur (72) est produit à partir d'un flux enrichi en argon (80) provenant de la colonne basse pression (11). Dans un premier mode de fonctionnement, une première quantité de produit d'argon pur est évacuée sous la forme d'un produit final et, dans un deuxième mode de fonctionnement, une quantité réduite de produit d'argon pur. Dans le deuxième mode de fonctionnement, un courant de retour d'argon gazeux (101, 103) est extrait de la colonne d'argon brut ou de la colonne d'argon pur et chauffé dans un passage séparé (108) de l'échangeur de chaleur principal (8).
EP15771022.9A 2014-10-16 2015-09-23 Procédé et dispositif destinés à l'obtention variable d'argon par la décomposition à basse température de l'air Active EP3207320B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PL15771022T PL3207320T3 (pl) 2014-10-16 2015-09-23 Sposób i urządzenie do zmiennego pozyskiwania argonu przez rozkład niskotemperaturowy

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP14003544 2014-10-16
PCT/EP2015/001886 WO2016058666A1 (fr) 2014-10-16 2015-09-23 Procédé et dispositif de récupération variable d'argon par fractionnement à basse température

Publications (2)

Publication Number Publication Date
EP3207320A1 true EP3207320A1 (fr) 2017-08-23
EP3207320B1 EP3207320B1 (fr) 2021-06-30

Family

ID=51751883

Family Applications (1)

Application Number Title Priority Date Filing Date
EP15771022.9A Active EP3207320B1 (fr) 2014-10-16 2015-09-23 Procédé et dispositif destinés à l'obtention variable d'argon par la décomposition à basse température de l'air

Country Status (11)

Country Link
US (1) US10690408B2 (fr)
EP (1) EP3207320B1 (fr)
JP (1) JP2017536523A (fr)
KR (1) KR20170070172A (fr)
CN (1) CN107076512B (fr)
BR (1) BR112017006788A2 (fr)
CA (1) CA2963023A1 (fr)
CL (1) CL2017000874A1 (fr)
PL (1) PL3207320T3 (fr)
RU (1) RU2700970C2 (fr)
WO (1) WO2016058666A1 (fr)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108731376A (zh) * 2018-04-18 2018-11-02 衢州杭氧气体有限公司 一种氩气生产工艺及其生产线
CN109764638B (zh) * 2018-12-13 2021-11-19 包头钢铁（集团）有限责任公司 一种大型制氧机组氩***变负荷方法
WO2022174976A1 (fr) 2021-02-16 2022-08-25 Linde Gmbh Fourniture d'un produit d'azote
EP3992560A1 (fr) 2021-05-27 2022-05-04 Linde GmbH Procédé de conception d'une installation de fractionnement de l'air à basse température à production d'argon

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SU658372A1 (ru) * 1976-12-20 1979-04-25 Научно-Исследовательский Институт Технологии Криогенного Машиностроения Установка разделени воздуха
JPS5449978A (en) * 1977-09-28 1979-04-19 Hitachi Ltd Air separation plant
US5133790A (en) * 1991-06-24 1992-07-28 Union Carbide Industrial Gases Technology Corporation Cryogenic rectification method for producing refined argon
CA2142317A1 (fr) * 1994-02-24 1995-08-25 Anton Moll Methode et appareil pour la recuperation d'argon pur
JPH1082582A (ja) * 1996-09-06 1998-03-31 Nippon Sanso Kk 空気液化分離装置及びその起動方法
WO1999054673A1 (fr) * 1998-04-21 1999-10-28 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et installation de distillation d'air avec production d'argon
DE10334560A1 (de) * 2003-05-28 2004-12-16 Linde Ag Verfahren und Vorrichtung zur Gewinnung von Krypton und/oder Xenon durch Tieftemperaturzerlegung von Luft
FR2943773B1 (fr) * 2009-03-27 2012-07-20 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
US8899075B2 (en) * 2010-11-18 2014-12-02 Praxair Technology, Inc. Air separation method and apparatus

Also Published As

Publication number Publication date
CN107076512B (zh) 2020-05-19
CL2017000874A1 (es) 2017-12-11
BR112017006788A2 (pt) 2017-12-26
CN107076512A (zh) 2017-08-18
RU2017116601A (ru) 2018-11-19
RU2700970C2 (ru) 2019-09-24
KR20170070172A (ko) 2017-06-21
WO2016058666A1 (fr) 2016-04-21
PL3207320T3 (pl) 2021-12-13
JP2017536523A (ja) 2017-12-07
RU2017116601A3 (fr) 2019-03-28
EP3207320B1 (fr) 2021-06-30
US20170299262A1 (en) 2017-10-19
CA2963023A1 (fr) 2016-04-21
US10690408B2 (en) 2020-06-23

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