EP1995537A2 - Procédé et dispositif de séparation cryogénique d'air - Google Patents

Procédé et dispositif de séparation cryogénique d'air Download PDF

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Publication number
EP1995537A2
EP1995537A2 EP08008679A EP08008679A EP1995537A2 EP 1995537 A2 EP1995537 A2 EP 1995537A2 EP 08008679 A EP08008679 A EP 08008679A EP 08008679 A EP08008679 A EP 08008679A EP 1995537 A2 EP1995537 A2 EP 1995537A2
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EP
European Patent Office
Prior art keywords
single column
pure oxygen
residual fraction
column
heat exchanger
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP08008679A
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German (de)
English (en)
Other versions
EP1995537A3 (fr
Inventor
Stefan Lochner
Michael Lauter
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
Publication of EP1995537A2 publication Critical patent/EP1995537A2/fr
Publication of EP1995537A3 publication Critical patent/EP1995537A3/fr
Withdrawn legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F25J3/0426—The cryogenic component does not participate in the fractionation
    • 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
    • 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
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • 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
    • 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
    • F25J3/0443—A main column system not otherwise provided, e.g. a modified double column flowsheet
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—Nitrogen
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/56—Ultra high purity oxygen, i.e. generally more than 99,9% O2
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/50—Separating low boiling, i.e. more volatile components from oxygen, e.g. N2, Ar
    • 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
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams

Definitions

  • the invention relates to a method for cryogenic air separation according to the preamble of patent claim 1.
  • the invention is therefore based on the object to provide a method of the type mentioned above and a corresponding device in which a relatively large amount of pure oxygen product can be produced.
  • This object is achieved in that the pure oxygen product stream is evaporated in the main heat exchanger against feed air and warmed and finally recovered as a gaseous product.
  • the aim of the invention is different:
  • the product evaporation serves primarily to recover the liquefaction refrigeration contained in the liquid withdrawn pure oxygen product stream. It has been found that the limiting factor in the amount of oxygen product through the Refrigeration capacity of the system is formed.
  • the liquefaction refrigeration which is discharged in the known method with the oxygen product, transferred in the main heat exchanger to the feed air or to a partial flow of the feed air and thus remains the process (except for the usual exchange losses).
  • the "main heat exchanger” is preferably formed by a single heat exchanger block. For larger systems, it may be useful to realize the main heat exchanger by a plurality of parallel with respect to the temperature profile strands, which are formed by separate components. In principle, it is possible that the main heat exchanger or each of these strands is formed by two or more blocks connected in series.
  • evaporation here includes a pseudo-evaporation under supercritical pressure.
  • the pressure at which the pure oxygen product stream is introduced into the main heat exchanger can thus also be above the critical pressure, as can the pressure of the heat carrier, which is (pseudo) condensed against the pure oxygen product stream.
  • a warm oxygen compressor can be dispensed with or at least made relatively small.
  • cold compressor is meant here a compressor which is operated at an inlet temperature of less than 200 K, preferably less than 150 K, in particular between 90 and 120 K.
  • a second residual fraction is taken from the lower region of the single column and expanded work in a relaxation machine, the mechanical energy generated during the work-relaxing relaxation at least partially for recompression of the first Residual fraction is used.
  • the transmission of mechanical energy to the recompressor is done directly mechanically, for example via a common wave of expansion machine and recompressor.
  • the recompressor is designed as a cold compressor, preferably only a part of the mechanical energy generated by the expansion machine is transferred to the recompressor; the rest goes to a warm braking device, z.
  • a brake fan a generator or a dissipative brake.
  • the single column has a top condenser, in which vapor from the upper region of the single column is at least partially condensed, wherein in the top condenser, the first residual fraction before its recompression and / or the second residual fraction at least partially evaporated prior to their work expansion become.
  • At least a portion of the condensate recovered in the top condenser is fed as reflux to the single column. If the two residual fractions have the same composition, they can be passed together through the top condenser. Preferably, however, they are in separate passages of the top condenser, especially if they have different composition.
  • the first residual fraction can in principle be withdrawn together with the second from the single column, for example at the bottom (see EP 412793 B2 ). In many cases, however, it is more favorable if the first residual fraction has a higher nitrogen content than the second residual fraction. Then, the first residual fraction is withdrawn from an intermediate point of the single column, which is arranged above the sump, in particular above the point at which the second residual fraction is removed. The two residual fractions are then evaporated separately in the top condenser and fed to the recompression or work-performing expansion.
  • the invention relates to a device for cryogenic air separation according to claim 8.
  • Atmospheric air 1 is drawn in via a filter 2 from an air compressor and there compressed to an absolute pressure of 6 to 20 bar, preferably about 9 bar.
  • the compressed air 6 is cleaned in a cleaning device 7, which has a pair of containers filled with adsorption material, preferably molecular sieve.
  • the purified air 8 is cooled in a main heat exchanger 9 to about dew point and partially liquefied.
  • a first part 11 of the cooled air 10 is introduced via a throttle valve 51 into a single column 12.
  • the feed is preferably some practical or theoretical soils above the sump.
  • the operating pressure of the single column 12 (at the top) is 6 to 20 bar, preferably about 9 bar.
  • Your top condenser is cooled with a first residual fraction 18 and a second residual fraction 14.
  • the second residual fraction 14 is withdrawn from the sump of the single column 12, the first residual fraction 14 from an intermediate point some practical or theoretical soils above the air supply or at the same level as this.
  • gaseous nitrogen 15, 16 is withdrawn at the top, warmed in the main heat exchanger 9 to about ambient temperature and finally withdrawn via line 17 as gaseous pressure product (PGAN).
  • a portion 53 of the condensate 52 from the top condenser 13 may be recovered as liquid nitrogen product (PLIN); the remainder 54 is given up as reflux to the head of the single column.
  • the first residual fraction 18 is vaporized in the top condenser 13 under a pressure of 2 to 9 bar, preferably about 4 bar and flows in gaseous form via line 29 to a cold compressor 30 in which it is recompressed to about the operating pressure of the single column.
  • the recompressed residual fraction 31 is in the main heat exchanger. 9 cooled again to column temperature and finally fed via line 32 of the single column 12 at the bottom again.
  • the second residual fraction 14 is vaporized in the top condenser 13 under a pressure of 2 to 9 bar, preferably about 4 bar and flows in gaseous form via line 19 to the cold end of the main heat exchanger 9. From this it is removed again at an intermediate temperature (line 20) and in a relaxation machine 21, which is designed in the example as turboexpander, work-performing relaxed to about 300 mbar above atmospheric pressure.
  • the expansion machine is mechanically coupled to the cold compressor 30 and a braking device 22, which is formed in the embodiment by an oil brake.
  • the relaxed second residual fraction 23 is heated in the main heat exchanger 9 to about ambient temperature.
  • the warm second residual fraction 24 is blown off into the atmosphere (line 25) and / or used as regeneration gas 26, 27 in the cleaning device 7, optionally after heating in the heating device 28.
  • An oxygen-containing stream 36 that is substantially free of less volatile impurities is withdrawn from an intermediate location of the single column 12 in the liquid state, which is located 5 to 25 theoretical or practical trays above the air feed.
  • the oxygen-containing stream 36 is optionally undercooled in a sump evaporator 37 of a pure oxygen column 38 and fed via line 39 and throttle valve 40 to the top of the pure oxygen column 38.
  • the operating pressure of the pure oxygen column 38 (at the top) is 1.3 to 4 bar, preferably about 2.5 bar.
  • the sump evaporator 37 of the pure oxygen column 38 is also cooled by means of a second part 42 of the cooled feed air 10.
  • the feed air stream 42 is at least partially, for example, completely condensed and flows via line 43 to the single column 12, where it is introduced approximately at the level of the feed of the remaining feed air 11.
  • a pure oxygen product stream 41 is removed in the liquid state, brought by a pump 55 to an elevated pressure of 2 to 100 bar, preferably about 12 bar, via line 56 to the cold end the main heat exchanger 9 out there, evaporated there under the increased pressure and warmed to about ambient temperature and finally recovered via line 57 as a gaseous product (GOX-IC).
  • a pump 55 to an elevated pressure of 2 to 100 bar, preferably about 12 bar, via line 56 to the cold end the main heat exchanger 9 out there, evaporated there under the increased pressure and warmed to about ambient temperature and finally recovered via line 57 as a gaseous product (GOX-IC).
  • the head gas 58 of the pure oxygen column 38 is added to the expanded second residual fraction 23. If necessary, a portion of the feed air for pumping prevention of the cold compressor 30 is led to its inlet via a bypass line 59 (anti-surge control).
  • a liquid oxygen can be removed as a liquid product (not shown in the drawing).
  • an external liquid for example, liquid argon, liquid nitrogen or liquid oxygen from a liquid tank, may be vaporized in the main heat exchanger 9 in indirect heat exchange with the feed air (not shown in the drawing).

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP08008679A 2007-05-24 2008-05-08 Procédé et dispositif de séparation cryogénique d'air Withdrawn EP1995537A3 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE102007024168A DE102007024168A1 (de) 2007-05-24 2007-05-24 Verfahren und Vorrichtung zur Tieftemperatur-Luftzerlegung

Publications (2)

Publication Number Publication Date
EP1995537A2 true EP1995537A2 (fr) 2008-11-26
EP1995537A3 EP1995537A3 (fr) 2009-04-15

Family

ID=39734126

Family Applications (1)

Application Number Title Priority Date Filing Date
EP08008679A Withdrawn EP1995537A3 (fr) 2007-05-24 2008-05-08 Procédé et dispositif de séparation cryogénique d'air

Country Status (6)

Country Link
US (1) US20080289362A1 (fr)
EP (1) EP1995537A3 (fr)
KR (1) KR20080103474A (fr)
CN (1) CN101311653A (fr)
DE (1) DE102007024168A1 (fr)
TW (1) TW200912229A (fr)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2236964A1 (fr) 2009-03-24 2010-10-06 Linde AG Procédé et dispositif de séparation de l'air à basse température
DE102010060595A1 (de) 2010-11-16 2012-05-16 Stefan Buchner Stromerzeugung aus tiefkalt verflüssigten Gasen
WO2015003785A1 (fr) 2013-07-09 2015-01-15 Linde Aktiengesellschaft Procédé et dispositif de production d'un flux de gaz comprimé et procédé et dispositif de séparation d'air à basse température
WO2014173496A3 (fr) * 2013-04-25 2015-08-20 Linde Aktiengesellschaft Procédé permettant d'obtenir un produit air dans une installation de séparation de l'air à stockage temporaire et installation de séparation de l'air
WO2020083525A1 (fr) 2018-10-23 2020-04-30 Linde Aktiengesellschaft Procédé et installation de séparation d'air à basse température
WO2021104668A1 (fr) 2019-11-26 2021-06-03 Linde Gmbh Procédé et installation pour fractionnement à basse température de l'air
WO2022214214A1 (fr) * 2021-04-09 2022-10-13 Linde Gmbh Procédé et installation de fractionnement à basse température d'air
US12710228B2 (en) 2021-04-09 2026-08-18 Linde Gmbh Method and plant for low temperature fractionation of air

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102007051184A1 (de) 2007-10-25 2009-04-30 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Tieftemperatur-Luftzerlegung
CN102322726A (zh) * 2011-06-13 2012-01-18 开封空分集团有限公司 交替生产氮气和液氮的空气分离装置及方法
CN102320581A (zh) * 2011-08-30 2012-01-18 开封黄河空分集团有限公司 一种氮气制取工艺
CN114413571A (zh) * 2022-01-24 2022-04-29 四川空分集团工程有限公司 一种低能耗低压压力氧空分装置
EP4477980A1 (fr) 2023-06-15 2024-12-18 Linde GmbH Procédé et dispositif pour la production de produits pneumatiques à partir d'une fraction d'oxygène

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EP0412793B2 (fr) 1989-08-11 2001-07-11 The Boc Group, Inc. Procédé et dispositif pour la production d'azote à partir d'air
EP0807792B1 (fr) 1996-05-14 2001-12-19 The Boc Group, Inc. Procédé et dispositif de séparation d'air
US20070204652A1 (en) 2006-02-21 2007-09-06 Musicus Paul Process and apparatus for producing ultrapure oxygen

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US5934106A (en) * 1998-01-27 1999-08-10 The Boc Group, Inc. Apparatus and method for producing nitrogen
US5934105A (en) * 1998-03-04 1999-08-10 Praxair Technology, Inc. Cryogenic air separation system for dual pressure feed
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EP2236964A1 (fr) 2009-03-24 2010-10-06 Linde AG Procédé et dispositif de séparation de l'air à basse température
DE102010060595A1 (de) 2010-11-16 2012-05-16 Stefan Buchner Stromerzeugung aus tiefkalt verflüssigten Gasen
WO2014173496A3 (fr) * 2013-04-25 2015-08-20 Linde Aktiengesellschaft Procédé permettant d'obtenir un produit air dans une installation de séparation de l'air à stockage temporaire et installation de séparation de l'air
EP2989400B1 (fr) 2013-04-25 2021-12-29 Linde GmbH Procédé permettant d'obtenir un produit air dans une installation de séparation de l'air à stockage temporaire et installation de séparation de l'air
WO2015003785A1 (fr) 2013-07-09 2015-01-15 Linde Aktiengesellschaft Procédé et dispositif de production d'un flux de gaz comprimé et procédé et dispositif de séparation d'air à basse température
WO2020083525A1 (fr) 2018-10-23 2020-04-30 Linde Aktiengesellschaft Procédé et installation de séparation d'air à basse température
WO2021104668A1 (fr) 2019-11-26 2021-06-03 Linde Gmbh Procédé et installation pour fractionnement à basse température de l'air
CN113924452A (zh) * 2019-11-26 2022-01-11 林德有限责任公司 用于低温分离空气的方法和设备
WO2022214214A1 (fr) * 2021-04-09 2022-10-13 Linde Gmbh Procédé et installation de fractionnement à basse température d'air
US12710228B2 (en) 2021-04-09 2026-08-18 Linde Gmbh Method and plant for low temperature fractionation of air

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CN101311653A (zh) 2008-11-26
EP1995537A3 (fr) 2009-04-15
DE102007024168A1 (de) 2008-11-27
TW200912229A (en) 2009-03-16
US20080289362A1 (en) 2008-11-27

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