EP2369281A1 - Procédé et dispositif destinés à la décomposition à basse température d'air - Google Patents

Procédé et dispositif destinés à la décomposition à basse température d'air Download PDF

Info

Publication number
EP2369281A1
EP2369281A1 EP10002439A EP10002439A EP2369281A1 EP 2369281 A1 EP2369281 A1 EP 2369281A1 EP 10002439 A EP10002439 A EP 10002439A EP 10002439 A EP10002439 A EP 10002439A EP 2369281 A1 EP2369281 A1 EP 2369281A1
Authority
EP
European Patent Office
Prior art keywords
air
pressure
heat exchanger
main heat
compressed
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Withdrawn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
EP10002439A
Other languages
German (de)
English (en)
Inventor
Lochner Stefan
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 EP10002439A priority Critical patent/EP2369281A1/fr
Priority to PCT/EP2011/001002 priority patent/WO2011110301A2/fr
Publication of EP2369281A1 publication Critical patent/EP2369281A1/fr
Withdrawn legal-status Critical Current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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest 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
    • F25J3/04006—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
    • F25J3/04054—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 of 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
    • F25J3/04078—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
    • F25J3/04084—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 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
    • 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
    • F25J3/04296—Claude expansion, i.e. expanded into the main or 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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft

Definitions

  • the invention relates to a method for the cryogenic separation of air according to the preamble of patent claim 1.
  • the distillation column system of the invention can be designed as a two-column system for nitrogen-oxygen separation (for example as a classic Linde double column system) or as a three-column or multi-column system. It may in addition to the columns for nitrogen-oxygen separation, further devices for obtaining high purity products and / or other air components, in particular of noble gases, for example, an argon production and / or a krypton-xenon recovery.
  • the invention has for its object to provide a method of the type mentioned above and a corresponding device, which are economically particularly favorable to operate by having an increased product yield, a particularly high product purity, lower energy consumption and / or lower investment costs.
  • This object is achieved in that the second air flow is formed by a different part of the compressed feed air than the first air flow.
  • the invention waives this increase in pressure in the turbine flow.
  • Both air streams are preferably introduced into the high-pressure column in the process according to the invention after their (pseudo) liquefaction) or work-performing expansion.
  • at least a portion of the first and / or the second air stream may be introduced into the low-pressure column, in particular after flowing through a separator for phase separation and optionally after supercooling.
  • the "main heat exchanger” may be formed of one or more parallel and / or serially connected heat exchanger sections, for example one or more plate heat exchanger blocks.
  • the first pressure, to which the total air is compressed is "significantly higher” than the operating pressure of the high-pressure column.
  • the pressure difference between the first pressure and the operating pressure of the high-pressure column not only corresponds to the natural pressure drop through lines, heat exchangers and other apparatus, but at least 1 bar, preferably at least 3 bar, most preferably at least 5 bar.
  • the pressure difference between the first pressure and the operating pressure of the high-pressure column is, for example, 5 to 25 bar, preferably 7 to 15 bar. (All pressures given here and below are absolute pressures.)
  • the first pressure is 10 to 25 bar, preferably 13 to 20 bar
  • the operating pressure of the high-pressure column is 4 to 8 bar, preferably 5 to 7 bar.
  • the second pressure downstream of the Cold compressor is for example 11.5 to 55 bar, preferably 21 to 44 bar, the increased pressure of the product pressure stream, for example 6 to 50 bar, preferably 6 to 35 bar.
  • every level of product pressure is possible, in particular also a plurality of pressure levels.
  • liquid oxygen can be brought to 30 bar in an internal compression pump and divided in cold into two partial streams upstream of the main heat exchanger, one of which is throttled to a lower pressure before it is vaporized and warmed in the main heat exchanger.
  • one or more liquid nitrogen streams in the main heat exchanger are evaporated.
  • the pressures of the pressurized product stream and the first air stream are subcritical, they are vaporized or liquefied in the main heat exchanger. At supercritical pressure no real phase transition takes place, then the corresponding stream is pseudo-vaporized or pseudo-liquefied.
  • the entire introduced into the main heat exchanger compressed feed air divided into the first and the second air flow. So there is no third air flow, but the entire feed air is either under the second pressure (pseudo) liquefied (first air flow) or supplied under the first pressure of the work-performing expansion (second air flow).
  • first air flow the second pressure liquefied
  • second air flow the first pressure of the work-performing expansion
  • a second part of the process is used to generate process refrigeration transferred during the work-relaxing relaxation generated mechanical energy to a warm braking device.
  • This can basically be formed by a compressor operating in warm, by an electric generator or a dissipative braking device.
  • a dissipative brake for example an oil brake, or an electric generator is used in the invention. Ideal would be an oil brake or a high-frequency generator, which sits on the shaft between the wheels for turbine and cold compressor.
  • the outlet pressure of the work-performing expansion is preferably approximately equal to the operating pressure of the high-pressure column. "About equal to” includes small pressure differences on the order of magnitude of the natural pressure drop between the discharge pressure of the work-performing expansion and the operating pressure of the high-pressure column.
  • total amount of liquid products is meant here the molar amount of liquid products such as liquid oxygen, liquid nitrogen and possibly liquid argon, which are obtained in the process as a final product.
  • the invention also relates to a device for cryogenic separation of air according to claims 8 to 11.
  • Atmospheric air 1 is sucked in via a filter 2 from an air compressor 3 and there compressed as feed air to a first pressure of about 17 bar. Subsequently, the compressed feed air flows through a direct contact cooler 4 and is cooled there in direct contact with cooling water 5.
  • the cooled feed air 6 is cleaned in a cleaning device 7.
  • the cleaning device 7 comprises a pair of containers filled with adsorbent material, preferably molecular sieve.
  • the purified feed air 8 is - apart from a not shown Removal possibility for instrument air - completely divided into a first air flow 9 and a second air flow 10. Both air streams are then fed to the warm end of a main heat exchanger 11 and cooled there against backflow.
  • the first air stream is removed via line 12 at a first intermediate temperature of about 140 K from the corresponding cooling passage of the main heat exchanger 11 and densified in a cold compressor 13 from the first pressure to a second pressure of about 31 bar.
  • a second intermediate temperature of about 170 K the recompressed second air stream 14 is again introduced into the main heat exchanger 11 where it is further cooled and liquefied and finally introduced via line 15 and a throttle valve 16 in the high pressure column 17 of a distillation column system for nitrogen-oxygen separation , which also has a low-pressure column 18 and a main condenser 19, which is designed as a condenser-evaporator.
  • the operating pressures are (at the top of the head) 5 to 6.5 bar in the high-pressure column and 1.3 bar in the low-pressure column.
  • the second air stream 10 is cooled in the embodiment separately from the first air stream 9 in the main heat exchanger 11 to a third intermediate temperature of about 139 K. Typically, this temperature is in the range of the boiling temperature (s) of the vaporized product stream (s).
  • the second air flow is supplied under this intermediate temperature and the first pressure of a relaxation machine 21 and there relaxes work to about the operating pressure of the high pressure column.
  • the working expanded second air stream 22 occurs immediately above the sump in the high-pressure column 17 a.
  • the expansion machine 21 is formed in the embodiment by a TurboExpander. It is mechanically coupled to the cold compressor 13 and an oil brake 23 via a common shaft. Contrary to the drawing, the oil brake is arranged directly on the shaft, the turbine 21 and cold compressor 13 connects and is located between them.
  • the head nitrogen 24 of the high-pressure column is introduced to a first part 25 in the liquefaction space of the main condenser 19 and practically completely liquefied there.
  • the resulting liquid nitrogen 26 is fed to a first part 27 as reflux to the high-pressure column 17, to a second part 28 it is fed via a supercooling countercurrent 29, line 30 and throttle valve 31 in the head of the low pressure column 18.
  • the oxygen-enriched bottom product 32 of the high pressure column 17 is also cooled in the subcooling countercurrent 29 and then fed via line 33 and throttle valve 34 of the low pressure column 18 at an intermediate point.
  • a second part 35 of the top nitrogen 24 of the high-pressure column 17 is warmed in the main heat exchanger 11 to about ambient temperature and finally discharged via line 36 as a pressure nitrogen product or as instrument or sealing gas (seal gas).
  • the oxygen in the bottom of the low pressure column 18 is removed via line 37 as a liquid product stream, brought in a pump 38 to an elevated pressure of 30 bar, evaporated under this increased pressure in the main heat exchanger and finally withdrawn as gaseous pressure product stream 39 (GOX IC).
  • a gaseous nitrogen stream 40 is removed, slightly below a gaseous impure nitrogen stream 41. Both are heated in the supercooling countercurrent 29 and further in the main heat exchanger 11.
  • the warm pure nitrogen 42 from the low-pressure column head is obtained downstream of the main heat exchanger to a first part 43 as a gaseous low pressure product (GAN); the remainder 44 is brought in a nitrogen compressor 45 to a product pressure of, for example, 15 bar and withdrawn downstream of an aftercooler 46 via line 47 as another gaseous pressure product (GAN EC).
  • the impure nitrogen 48 is vented downstream of the main heat exchanger 11 into the atmosphere (line 49) and / or used as regeneration gas 50, 51 in the cleaning device 7, optionally after heating in a heater 52nd
  • a second embodiment corresponds largely to the first, but a portion of the liquid nitrogen 26 is brought from the main condenser as a further liquid product stream in a nitrogen pump to an elevated product pressure and in the main heat exchanger 11 (pseudo) evaporated and heated to about ambient temperature and finally as a further gaseous Obtained compressed product stream in the form of high-pressure nitrogen.
  • a portion of the liquid high-pressure oxygen downstream of the oxygen pump 38 is throttled to a pressure which is between the "elevated pressure" (the discharge pressure of the oxygen pump 38) and the operating pressure of the low-pressure column 18.
  • This stream is also vaporized and warmed in the main heat exchanger and finally recovered as the third pressure product stream in the form of intermediate pressure oxygen.

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)
EP10002439A 2010-03-09 2010-03-09 Procédé et dispositif destinés à la décomposition à basse température d'air Withdrawn EP2369281A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP10002439A EP2369281A1 (fr) 2010-03-09 2010-03-09 Procédé et dispositif destinés à la décomposition à basse température d'air
PCT/EP2011/001002 WO2011110301A2 (fr) 2010-03-09 2011-03-01 Procédé et dispositif de séparation de l'air à basse température

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP10002439A EP2369281A1 (fr) 2010-03-09 2010-03-09 Procédé et dispositif destinés à la décomposition à basse température d'air

Publications (1)

Publication Number Publication Date
EP2369281A1 true EP2369281A1 (fr) 2011-09-28

Family

ID=42727812

Family Applications (1)

Application Number Title Priority Date Filing Date
EP10002439A Withdrawn EP2369281A1 (fr) 2010-03-09 2010-03-09 Procédé et dispositif destinés à la décomposition à basse température d'air

Country Status (2)

Country Link
EP (1) EP2369281A1 (fr)
WO (1) WO2011110301A2 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3010778A1 (fr) * 2013-09-17 2015-03-20 Air Liquide Procede et appareil de production d'oxygene gazeux par distillation cryogenique de l'air
CN112392558A (zh) * 2019-08-13 2021-02-23 江苏国富氢能技术装备有限公司 一种低温气液化用透平膨胀装置

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102012017488A1 (de) 2012-09-04 2014-03-06 Linde Aktiengesellschaft Verfahren zur Erstellung einer Luftzerlegungsanlage, Luftzerlegungsanlage und zugehöriges Betriebsverfahren
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

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0672877A1 (fr) * 1994-03-15 1995-09-20 The BOC Group plc Séparation d'air par voie cryogénique
US5475980A (en) 1993-12-30 1995-12-19 L'air Liquide, Societe Anonyme Pour L'etude L'exploitation Des Procedes Georges Claude Process and installation for production of high pressure gaseous fluid
WO2004099691A1 (fr) 2003-05-05 2004-11-18 L'air Liquide Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et installation de production de gaz de l'air sous pression par distillation cryogenique d'air
US20050126221A1 (en) * 2003-12-10 2005-06-16 Bao Ha Process and apparatus for the separation of air by cryogenic distillation
US20070017251A1 (en) * 2003-05-05 2007-01-25 Bot Patrick L Cryogenic distillation method and system for air separation
US20080223075A1 (en) * 2005-09-23 2008-09-18 L'air Liquide Societe Anonyme Pour L'etude Et L'exloitation Des Procedes Georges Claude Process and Apparatus for the Separation of Air by Cryogenic Distillation
FR2913760A1 (fr) * 2007-03-13 2008-09-19 Air Liquide Procede et appareil de production de gaz de l'air sous forme gazeuse et liquide a haute flexibilite par distillation cryogenique

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1067345B1 (fr) * 1999-07-05 2004-06-16 Linde Aktiengesellschaft Procédé et dispositif pour la séparation cryogénique des constituants de l'air
FR2851330B1 (fr) * 2003-02-13 2006-01-06 Air Liquide Procede et installation de production sous forme gazeuse et sous haute pression d'au moins un fluide choisi parmi l'oxygene, l'argon et l'azote par distillation cryogenique de l'air

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5475980A (en) 1993-12-30 1995-12-19 L'air Liquide, Societe Anonyme Pour L'etude L'exploitation Des Procedes Georges Claude Process and installation for production of high pressure gaseous fluid
EP0672877A1 (fr) * 1994-03-15 1995-09-20 The BOC Group plc Séparation d'air par voie cryogénique
WO2004099691A1 (fr) 2003-05-05 2004-11-18 L'air Liquide Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et installation de production de gaz de l'air sous pression par distillation cryogenique d'air
US20060277944A1 (en) * 2003-05-05 2006-12-14 Patrick Le Bot Method and system for the production of pressurized air gas by cryogenic distillation of air
US20070017251A1 (en) * 2003-05-05 2007-01-25 Bot Patrick L Cryogenic distillation method and system for air separation
US20050126221A1 (en) * 2003-12-10 2005-06-16 Bao Ha Process and apparatus for the separation of air by cryogenic distillation
US20080223075A1 (en) * 2005-09-23 2008-09-18 L'air Liquide Societe Anonyme Pour L'etude Et L'exloitation Des Procedes Georges Claude Process and Apparatus for the Separation of Air by Cryogenic Distillation
FR2913760A1 (fr) * 2007-03-13 2008-09-19 Air Liquide Procede et appareil de production de gaz de l'air sous forme gazeuse et liquide a haute flexibilite par distillation cryogenique

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
"Tieftemperaturtechnik", 1985, pages: 281 - 337

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3010778A1 (fr) * 2013-09-17 2015-03-20 Air Liquide Procede et appareil de production d'oxygene gazeux par distillation cryogenique de l'air
WO2015040306A3 (fr) * 2013-09-17 2015-06-11 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de production d'oxygène gazeux par distillation cryogénique de l'air
US9976803B2 (en) 2013-09-17 2018-05-22 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitattion Des Procedes Georges Claude Process and apparatus for producing gaseous oxygen by cryogenic distillation of air
CN112392558A (zh) * 2019-08-13 2021-02-23 江苏国富氢能技术装备有限公司 一种低温气液化用透平膨胀装置
CN112392558B (zh) * 2019-08-13 2024-05-03 江苏国富氢能技术装备股份有限公司 一种低温气液化用透平膨胀装置

Also Published As

Publication number Publication date
WO2011110301A2 (fr) 2011-09-15
WO2011110301A3 (fr) 2012-08-23

Similar Documents

Publication Publication Date Title
EP3164654B1 (fr) Procédé et dispositif de fractionnement de l'air à basse température à consommation d'énergie variable
EP1139046B1 (fr) Procédé et installation de production d'oxygène sous haute pression par séparation cryogénique de l'air
WO2007104449A1 (fr) Procédé et dispositif de décomposition de l'air à basse température
EP2015012A2 (fr) Procédé pour la séparation cryogénique d'air
DE102010052545A1 (de) Verfahren und Vorrichtung zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
EP2466236A1 (fr) Procédé de production d'un produit d'impression gazeux par décomposition à basse température de l'air
EP2963370B1 (fr) Procede et dispositif cryogeniques de separation d'air
EP2520886A1 (fr) Procédé et dispositif de production d'un produit comprimé à oxygène gazeux par décomposition à basse température d'air
EP3343158A1 (fr) Procédé de production d'un ou plusieurs produits pneumatiques et unité de fractionnement d'air
EP3410050B1 (fr) Procédé de production d'un ou de plusieurs produits pneumatiques et installation de séparation d'air
EP2299221A2 (fr) Procédé et dispositif destinés à la décomposition à basse température d'air
EP2963369B1 (fr) Procede et dispositif cryogeniques de separation d'air
EP3290843A2 (fr) Procédé et dispositif destiné à fabriquer de l'azote pressurisé et liquide par décomposition à basse température de l'air
EP2489968A1 (fr) Procédé et dispositif destinés à la décomposition à basse température d'air
EP2369281A1 (fr) Procédé et dispositif destinés à la décomposition à basse température d'air
EP2551619A1 (fr) Procédé et dispositif destinés à l'obtention d'oxygène pressurisé et d'azote pressurisé par la décomposition à basse température de l'air
WO2017108187A1 (fr) Procédé et dispositif de production d'azote pur et d'oxygène pur par séparation cryogénique d'air
EP3924677A1 (fr) Procédé et installation pour fournir un ou plusieurs produits présents dans l'air, gazeux et à teneur élevée en oxygène
DE102007042462A1 (de) Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
EP2600090B1 (fr) Procédé et dispositif destinés à la production d'oxygène sous pression par décomposition à basse température de l'air
DE102011121314A1 (de) Verfahren zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft
EP3343159A1 (fr) Procédé et dispositif de production d'oxygène gazeux et azote comprimé gazeux
EP1199532A1 (fr) Système de séparation d'air cryogénique à trois colonnes
EP2963371B1 (fr) Procede et dispositif de production d'un produit de gaz sous pression par decomposition a basse temperature d'air
EP2906889A2 (fr) Procédé et installation de production de produits d'oxygène liquides et gazeux par fractionnement cryogénique de l'air

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION HAS BEEN WITHDRAWN

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO SE SI SK SM TR

AX Request for extension of the european patent

Extension state: AL BA ME RS

18W Application withdrawn

Effective date: 20110913