EP0024962B1 - Procédé cryogénique de séparation d'air avec production d'oxygène sous haute pression - Google Patents

Procédé cryogénique de séparation d'air avec production d'oxygène sous haute pression Download PDF

Info

Publication number
EP0024962B1
EP0024962B1 EP80401045A EP80401045A EP0024962B1 EP 0024962 B1 EP0024962 B1 EP 0024962B1 EP 80401045 A EP80401045 A EP 80401045A EP 80401045 A EP80401045 A EP 80401045A EP 0024962 B1 EP0024962 B1 EP 0024962B1
Authority
EP
European Patent Office
Prior art keywords
pressure
oxygen
fluid
air
high pressure
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.)
Expired
Application number
EP80401045A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0024962A1 (fr
Inventor
Gérard Vandenbussche
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 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 pour lEtude et lExploitation des Procedes Georges Claude filed Critical LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority to AT80401045T priority Critical patent/ATE1531T1/de
Publication of EP0024962A1 publication Critical patent/EP0024962A1/fr
Application granted granted Critical
Publication of EP0024962B1 publication Critical patent/EP0024962B1/fr
Expired 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
    • F25J3/04078—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
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams 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
    • F25J3/04248—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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen

Definitions

  • the present invention relates to a cryogenic air separation process with production of oxygen under high pressure.
  • This method has the advantage, compared to the first method mentioned above, of avoiding the use of an oxygen compressor, but has the disadvantage of leading to higher overall energy consumption when the oxygen production pressure is high.
  • This second process can only be acceptable from an energy point of view if the oxygen vaporization temperature remains lower than that of high pressure air condensing in counter-current to the vaporization of this oxygen. Therefore, an oxygen pressure as moderate as 15-20 bars requires an air pressure already reaching 50-60 bars. For many applications, the oxygen pressure is between 40 and 100 bars, so that the condition stated above can no longer be fulfilled, the equipment used, in particular the exchangers, not allowing the pressure to be raised. air significantly above these pressure levels.
  • the present invention relates to a process which makes it possible to economically obtain oxygen under high pressure by compression of a fraction of oxygen in the liquid state and this result is obtained by ensuring that at a temperature intermediate between the hot and cold temperatures of said heat exchange an expansion of the second fluid at the average pressure in a turbine.
  • the first fluid under high pressure is itself air and in an alternative embodiment this first fluid under high pressure is nitrogen in a closed circuit.
  • the intermediate pressure of the second fluid is between 8 and 20 bars and preferably of the order of 15 bars, while the high oxygen pressure is between 15 and 100 bars and preferably of the order of 65 to 40 bars.
  • a cryogenic air separation installation comprises an upstream separation zone 2 formed by a “medium pressure” column 3 and a downstream separation zone 4 formed by a “low pressure” column 5, superimposed on column 3 with the interposition of a vaporizer-condenser 6.
  • the medium pressure column 3 is supplied with air to be separated under medium pressure, for example of the order of 6 bars, by a pipe 10 connected to the outlet of a regulator 11, the inlet of which is connected by a pipe 12 to the second stage 13 of a compression assembly 14, also comprising a first stage 15 whose suction 16 is supplied with air at atmospheric pressure.
  • the first compression stage 15 compresses atmospheric air at a pressure of the order of 15 bars, while the second compression stage provides final compression from 15 bars to 50 bars.
  • Line 12 conveying air at 50 bars comprises heat exchange passages 20 extending from a hot end 21 to a cold end 22 of an exchanger 23. It is noted that part of the air in line 12 is diverted at 12 'and after expansion to low pressure at 11' introduced into the low pressure column 5.
  • Part of the compressed air at the outlet of the compression stage 15 is diverted by a pipe 25 to passages 26, extending in the exchanger 23 from a hot end 21 to a level 27 located at a distance both from the hot end 21 and from the cold end 22, therefore at an intermediate temperature between the hot temperature of the end 21 and the cold temperature of the end 22.
  • These heat exchange passages 26 open out into a transfer line 28 to an expansion turbine 29 braked by a device, the exhaust of this turbine 29 communicating with a pipe 30 opening directly at a low level of the medium pressure column 3.
  • the oxygen-rich fraction condensed in the bottom of the medium-pressure column 3 is transferred, via a pipe 40, if necessary after sub-cooling in an exchanger 41 to an expansion device 42 before being introduced, at an intermediate level, in the low pressure column 4.
  • the lean liquid which essentially comprises nitrogen, is taken off at an intermediate level of the medium pressure column and is transferred by a pipe 43 to the sub-cooling exchanger 41 before being expanded in the expansion device 45 and introduced at 46 at the head of the low pressure column.
  • a fraction of liquid oxygen 47 is formed, a main part of which is derived in a pipe 48 to be compressed at high pressure by a pump 49 before being introduced into heat exchange passages 50 s extending from the cold end 22 to the hot end 21 of the exchanger 23, these passages 50 communicating, at the outlet, with a high pressure oxygen distribution pipe 51.
  • Another part of the fraction of liquid oxygen, of lower flow rate, is diverted by a pipe 54 to the subcooling exchanger 41, to be transferred by a pipe 55 to a storage, not shown, of liquid oxygen under- cooled.
  • a fraction of liquid nitrogen is taken off at the head of the medium pressure column 3 through a pipe 56 to be sub-cooled in the exchanger 41 before being expanded in an expansion device 57 and to reach a separator 58 comprising a tank withdrawal line 59 for a liquid fraction and a head withdrawal line 60 for a gaseous fraction.
  • This pipe 60 for the gas fraction is also connected to a pipe 61 of nitrogen gas coming from the head of the low pressure column to form a common gas pipe 62 towards heating passages 63 in the subcooling exchanger 41 , the outlet of these passages 63 communicating via a pipe 64 with heating passages 65 extending over the entire length of the exchanger 23 to ensure in an outlet pipe 66, the grouping of impure nitrogen in the gaseous state and under low pressure.
  • the results obtained are reported below with an overall air flow rate of 1,000 Nm 3 , a pressure of 50 bars at the outlet of the second compression stage 15, an intermediate pressure at the outlet of the first stage compression 13 successively of 10, 12 and 15 bars, the flow rate of vaporized oxygen always being at 40 bars: *
  • the reference value (100%) is that obtained for oxygen at 40 bars, produced at atmospheric pressure with a device of the usual type, then compressed by turbocharger.
  • FIG. 2 in which the same reference signs as in FIG. 1 designate the same elements, an alternative embodiment is described in which an auxiliary nitrogen cycle is used.
  • a separation installation with a medium pressure column 3 and a low pressure column 5.
  • the exchanger 123 (of the same type as the exchanger 23 in Figure 1), there are heating passages with vaporization liquid oxygen 150 (similar to passages 50 in Figure 1), heating passages for impure nitrogen 165 (similar to passages 65 in Figure 1) cooling passages for a first high pressure fluid 120 (similar to the passages 20 in FIG. 2) and the cooling passages 126 for a second fluid, which is also air, under intermediate pressure similar to the passages 26 in FIG. 1.
  • the first fluid is no longer air, as in FIG. 1, but nitrogen which is drawn off at medium pressure at the head of the medium pressure column 3 via a pipe 70 to be introduced into additional passages. 71 of the exchanger 123, then be directed via a line 72 to a compressor 73 raising the nitrogen pressure from medium pressure (for example 6 bars) to high pressure (for example 50 bars).
  • the nitrogen thus compressed passes through the passages 120 of the exchanger 123, then is expanded in an expansion device 111 to be reintroduced at the head of the medium pressure column 3.
  • all the air flow to be separated is here compressed by the compressor 115 before passing through the passages 126, the expansion turbine 29 and via the pipe 30 in the tank of the medium pressure column 3.

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)
  • Oxygen, Ozone, And Oxides In General (AREA)
EP80401045A 1979-07-20 1980-07-11 Procédé cryogénique de séparation d'air avec production d'oxygène sous haute pression Expired EP0024962B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT80401045T ATE1531T1 (de) 1979-07-20 1980-07-11 Tieftemperatur-lufzerlegungsverfahren mit herstellung von hochdrucksauerstoff.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR7918772 1979-07-20
FR7918772A FR2461906A1 (fr) 1979-07-20 1979-07-20 Procede et installation cryogeniques de separation d'air avec production d'oxygene sous haute pression

Publications (2)

Publication Number Publication Date
EP0024962A1 EP0024962A1 (fr) 1981-03-11
EP0024962B1 true EP0024962B1 (fr) 1982-09-08

Family

ID=9228097

Family Applications (1)

Application Number Title Priority Date Filing Date
EP80401045A Expired EP0024962B1 (fr) 1979-07-20 1980-07-11 Procédé cryogénique de séparation d'air avec production d'oxygène sous haute pression

Country Status (7)

Country Link
US (1) US4303428A (pt)
EP (1) EP0024962B1 (pt)
JP (1) JPS5620980A (pt)
AT (1) ATE1531T1 (pt)
CA (1) CA1146724A (pt)
DE (1) DE3060825D1 (pt)
FR (1) FR2461906A1 (pt)

Families Citing this family (55)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2079428A (en) * 1980-06-17 1982-01-20 Air Prod & Chem A method for producing gaseous oxygen
GB2080929B (en) * 1980-07-22 1984-02-08 Air Prod & Chem Producing gaseous oxygen
JPS58133587A (ja) * 1982-02-03 1983-08-09 株式会社日立製作所 液体窒素の採取方法
JPS60194274A (ja) * 1984-03-14 1985-10-02 株式会社日立製作所 窒素精製装置
JPS61130769A (ja) * 1984-11-30 1986-06-18 株式会社日立製作所 低温廃ガスを利用した寒冷発生方法
US4662918A (en) * 1986-05-30 1987-05-05 Air Products And Chemicals, Inc. Air separation process
US4662916A (en) * 1986-05-30 1987-05-05 Air Products And Chemicals, Inc. Process for the separation of air
US4662917A (en) * 1986-05-30 1987-05-05 Air Products And Chemicals, Inc. Process for the separation of air
US4947649A (en) * 1989-04-13 1990-08-14 Air Products And Chemicals, Inc. Cryogenic process for producing low-purity oxygen
JPH02293576A (ja) * 1989-05-08 1990-12-04 Hitachi Ltd 空気分離装置
FR2651035A1 (fr) * 1989-08-18 1991-02-22 Air Liquide Procede de production d'azote par distillation
GB8921428D0 (en) * 1989-09-22 1989-11-08 Boc Group Plc Separation of air
FR2652409A1 (fr) * 1989-09-25 1991-03-29 Air Liquide Procede de production frigorifique, cycle frigorifique correspondant et leur application a la distillation d'air.
GB9008752D0 (en) * 1990-04-18 1990-06-13 Boc Group Plc Air separation
US5148680A (en) * 1990-06-27 1992-09-22 Union Carbide Industrial Gases Technology Corporation Cryogenic air separation system with dual product side condenser
FR2670278B1 (fr) * 1990-12-06 1993-01-22 Air Liquide Procede et installation de distillation d'air en regime variable de production d'oxygene gazeux.
US5123947A (en) * 1991-01-03 1992-06-23 Air Products And Chemicals, Inc. Cryogenic process for the separation of air to produce ultra high purity nitrogen
GB9100814D0 (en) * 1991-01-15 1991-02-27 Boc Group Plc Air separation
FR2685460B1 (fr) * 1991-12-20 1997-01-31 Maurice Grenier Procede et installation de production d'oxygene gazeux sous pression par distillation d'air
JP2909678B2 (ja) * 1991-03-11 1999-06-23 レール・リキード・ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード 圧力下のガス状酸素の製造方法及び製造装置
FR2674011B1 (fr) * 1991-03-11 1996-12-20 Maurice Grenier Procede et installation de production d'oxygene gazeux sous pression.
DE4109945A1 (de) * 1991-03-26 1992-10-01 Linde Ag Verfahren zur tieftemperaturzerlegung von luft
JPH0623879A (ja) * 1991-05-10 1994-02-01 Kenkichi Kobashigawa 紙筒製作具
US5163296A (en) * 1991-10-10 1992-11-17 Praxair Technology, Inc. Cryogenic rectification system with improved oxygen recovery
GB9124242D0 (en) * 1991-11-14 1992-01-08 Boc Group Plc Air separation
FR2685459B1 (fr) * 1991-12-18 1994-02-11 Air Liquide Procede et installation de production d'oxygene impur.
CN1071444C (zh) * 1992-02-21 2001-09-19 普拉塞尔技术有限公司 生产气体氧的低温空气分离系统
US5228297A (en) * 1992-04-22 1993-07-20 Praxair Technology, Inc. Cryogenic rectification system with dual heat pump
US5233838A (en) * 1992-06-01 1993-08-10 Praxair Technology, Inc. Auxiliary column cryogenic rectification system
FR2692664A1 (fr) * 1992-06-23 1993-12-24 Lair Liquide Procédé et installation de production d'oxygène gazeux sous pression.
FR2697325B1 (fr) * 1992-10-27 1994-12-23 Air Liquide Procédé et installation de production d'azote et d'oxygène.
FR2701553B1 (fr) * 1993-02-12 1995-04-28 Maurice Grenier Procédé et installation de production d'oxygène sous pression.
FR2702040B1 (fr) * 1993-02-25 1995-05-19 Air Liquide Procédé et installation de production d'oxygène et/ou d'azote sous pression.
US5471843A (en) * 1993-06-18 1995-12-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the production of oxygen and/or nitrogen under pressure at variable flow rate
FR2706595B1 (fr) * 1993-06-18 1995-08-18 Air Liquide Procédé et installation de production d'oxygène et/ou d'azote sous pression à débit variable.
US5379598A (en) * 1993-08-23 1995-01-10 The Boc Group, Inc. Cryogenic rectification process and apparatus for vaporizing a pumped liquid product
US5379599A (en) * 1993-08-23 1995-01-10 The Boc Group, Inc. Pumped liquid oxygen method and apparatus
FR2709538B1 (fr) * 1993-09-01 1995-10-06 Air Liquide Procédé et installation de production d'au moins un gaz de l'air sous pression.
FR2711778B1 (fr) * 1993-10-26 1995-12-08 Air Liquide Procédé et installation de production d'oxygène et/ou d'azote sous pression.
US5398514A (en) * 1993-12-08 1995-03-21 Praxair Technology, Inc. Cryogenic rectification system with intermediate temperature turboexpansion
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
FR2721383B1 (fr) * 1994-06-20 1996-07-19 Maurice Grenier Procédé et installation de production d'oxygène gazeux sous pression.
FR2724011B1 (fr) * 1994-08-29 1996-12-20 Air Liquide Procede et installation de production d'oxygene par distillation cryogenique
US5564290A (en) * 1995-09-29 1996-10-15 Praxair Technology, Inc. Cryogenic rectification system with dual phase turboexpansion
EP0955509B1 (de) 1998-04-30 2004-12-22 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von hochreinem Sauerstoff
US6000239A (en) * 1998-07-10 1999-12-14 Praxair Technology, Inc. Cryogenic air separation system with high ratio turboexpansion
FR2782544B1 (fr) * 1998-08-19 2005-07-08 Air Liquide Pompe pour un liquide cryogenique ainsi que groupe de pompage et colonne de distillation equipes d'une telle pompe
US6053008A (en) * 1998-12-30 2000-04-25 Praxair Technology, Inc. Method for carrying out subambient temperature, especially cryogenic, separation using refrigeration from a multicomponent refrigerant fluid
US6112550A (en) * 1998-12-30 2000-09-05 Praxair Technology, Inc. Cryogenic rectification system and hybrid refrigeration generation
FR2854683B1 (fr) * 2003-05-05 2006-09-29 Air Liquide Procede et installation de production de gaz de l'air sous pression par distillation cryogenique d'air
US6925818B1 (en) * 2003-07-07 2005-08-09 Cryogenic Group, Inc. Air cycle pre-cooling system for air separation unit
EP1726900A1 (en) * 2005-05-20 2006-11-29 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for the separation of air by cryogenic distillation
US7487648B2 (en) * 2006-03-10 2009-02-10 Praxair Technology, Inc. Cryogenic air separation method with temperature controlled condensed feed air
DE102006012241A1 (de) * 2006-03-15 2007-09-20 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
US10712088B1 (en) * 2017-05-05 2020-07-14 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Temperature balancing for thermal integration of an air separation unit (ASU) with a power generation system

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2520862A (en) * 1946-10-07 1950-08-29 Judson S Swearingen Air separation process
FR1148546A (fr) * 1956-09-27 1957-12-11 Air Liquide Procédé de séparation de l'air en ses éléments
DE1124529B (de) * 1957-07-04 1962-03-01 Linde Eismasch Ag Verfahren und Einrichtung zur Durchfuehrung von Waermeaustauschvorgaengen in einer mit vorgeschalteten Regeneratoren arbeitenden Gaszerlegungsanlage
FR1250454A (fr) * 1958-09-24 1961-01-13 Lindes Eismaschinen Ag Procédé pour la réalisation d'un bilan frigorifique équilibré lors de l'obtention, depuis la rectification, de mélanges de gaz ou de composants de mélanges de gaz sous haute pression, ou non
DE1103363B (de) * 1958-09-24 1961-03-30 Linde Eismasch Ag Verfahren und Vorrichtung zur Erzeugung eines ausgeglichenen Kaeltehaushaltes bei der Gewinnung von unter hoeherem Druck stehenden Gasgemischen und/oder Gasgemisch-komponenten durch Rektifikation
DE1112997B (de) * 1960-08-13 1961-08-24 Linde Eismasch Ag Verfahren und Einrichtung zur Gaszerlegung durch Rektifikation bei tiefer Temperatur
FR1433585A (fr) * 1965-02-18 1966-04-01 Air Liquide Procédé de séparation des constituants de l'air à l'état gazeux et à l'état liquide
FR1479127A (fr) * 1966-05-10 1967-04-28 Linde Ag Procédé pour la récupération d'oxygène par rectification d'air à basse température
DE1907525A1 (de) * 1969-02-14 1970-08-20 Vnii Kriogennogo Masinostrojen Verfahren zur Trennung von Stickstoff und Sauerstoff aus der Luft
DE2535132C3 (de) * 1975-08-06 1981-08-20 Linde Ag, 6200 Wiesbaden Verfahren und Vorrichtung zur Herstellung von Drucksauerstoff durch zweistufige Tieftemperaturrektifikation von Luft
US4202678A (en) * 1975-08-25 1980-05-13 Air Products & Chemicals, Inc. Air separation liquefaction process
DE2557453C2 (de) * 1975-12-19 1982-08-12 Linde Ag, 6200 Wiesbaden Verfahren zur Gewinnung von gasförmigem Sauerstoff

Also Published As

Publication number Publication date
FR2461906A1 (fr) 1981-02-06
CA1146724A (fr) 1983-05-24
DE3060825D1 (en) 1982-10-28
ATE1531T1 (de) 1982-09-15
US4303428A (en) 1981-12-01
EP0024962A1 (fr) 1981-03-11
JPH0132433B2 (pt) 1989-06-30
JPS5620980A (en) 1981-02-27

Similar Documents

Publication Publication Date Title
EP0024962B1 (fr) Procédé cryogénique de séparation d'air avec production d'oxygène sous haute pression
EP0576314B1 (fr) Procédé et installation de production d'oxygène gazeux sous pression
EP2122282B1 (fr) Procédé de séparation d'un mélange de monoxyde de carbone, de méthane, d'hydrogène et d'azote par distillation cryogénique
US6477860B2 (en) Process for obtaining gaseous and liquid nitrogen with a variable proportion of liquid product
EP0504029A1 (fr) Procédé de production d'oxygène gazeux sous pression
JPH11504104A (ja) 流体流の冷却
EP1711765B1 (fr) Procédé et installationde de séparation d'air par distillation cryogénique
EP1447634A1 (fr) Procédé et installation de production sous forme gazeuse et sous haute pression d'au moins un fluide choisi parmi l'oxygène, l'argon et l'azote par distillation cryogénique de l'air
EP0789208A1 (fr) Procédé et installation de production d'oxygène gazeux sous haute pression
FR3066809A1 (fr) Procede et appareil pour la separation de l'air par distillation cryogenique
FR2723184A1 (fr) Procede et installation de production d'oxygene gazeux sous pression a debit variable
EP2140216B1 (fr) Procédé et appareil de séparation d'un mélange comprenant au moins de l'hydrogène, de l'azote et du monoxyde de carbone par distillation cryogénique
EP0677713B1 (fr) Procédé et installation pour la production de l'oxygène par distillation de l'air
CA2115399C (fr) Procede et installation de production d'oxygene sous pression
EP1409937B1 (fr) Procede de production de vapeur d'eau et de distillation d'air
WO2009112744A2 (fr) Appareil de separation d'air par distillation cryogenique
EP2938414B1 (fr) Procédé et appareil de séparation d'un gaz riche en dioxyde de carbone
FR2915271A1 (fr) Procede et appareil de separation des gaz de l'air par distillation cryogenique
FR2929697A1 (fr) Procede de production d'azote gazeux variable et d'oxygene gazeux variable par distillation d'air
EP4279848A1 (fr) Procédé et appareil de refroidissement d'un débit riche en co2
EP4375602A1 (fr) Procédé et appareil de liquéfaction et éventuellement de séparation de co2 par distillation
EP1692443A1 (fr) Compresseur de gaz, appareil de separation d'un melange gazeux incorporant un tel compresseur et procede de separation d'un melange gazeux incorporant un tel compresseur
CN116547488A (zh) 用于空气低温分离的方法和设备
FR2685460A1 (fr) Procede et installation de production d'oxygene gazeux sous pression par distillation d'air.
FR2842589A1 (fr) Procede et installation de separation d'air par distillation cryogenique

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

AK Designated contracting states

Designated state(s): AT BE CH DE FR GB IT LU NL SE

17P Request for examination filed

Effective date: 19810109

ITF It: translation for a ep patent filed
GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Designated state(s): AT BE CH DE FR GB IT LU NL SE

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Free format text: THE PATENT HAS BEEN ANNULLED BY A DECISION OF A NATIONAL AUTHORITY

Effective date: 19820908

Ref country code: NL

Effective date: 19820908

REF Corresponds to:

Ref document number: 1531

Country of ref document: AT

Date of ref document: 19820915

Kind code of ref document: T

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: AT

Effective date: 19821001

REF Corresponds to:

Ref document number: 3060825

Country of ref document: DE

Date of ref document: 19821028

NLV1 Nl: lapsed or annulled due to failure to fulfill the requirements of art. 29p and 29m of the patents act
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: CH

Payment date: 19910619

Year of fee payment: 12

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: LU

Payment date: 19910628

Year of fee payment: 12

EPTA Lu: last paid annual fee
PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 19920711

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LI

Effective date: 19920731

Ref country code: CH

Effective date: 19920731

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

ITTA It: last paid annual fee
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 19960624

Year of fee payment: 17

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 19970731

BERE Be: lapsed

Owner name: L' AIR LIQUIDE S.A. POUR L'ETUDE ET L'EXPLOITATION

Effective date: 19970731

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 19990615

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 19990618

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 19990628

Year of fee payment: 20

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION

Effective date: 20000710

REG Reference to a national code

Ref country code: GB

Ref legal event code: PE20

Effective date: 20000710

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

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

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT