EP0547946B2 - Procédé de production d'oxygène impur - Google Patents

Procédé de production d'oxygène impur Download PDF

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Publication number
EP0547946B2
EP0547946B2 EP92403330A EP92403330A EP0547946B2 EP 0547946 B2 EP0547946 B2 EP 0547946B2 EP 92403330 A EP92403330 A EP 92403330A EP 92403330 A EP92403330 A EP 92403330A EP 0547946 B2 EP0547946 B2 EP 0547946B2
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EP
European Patent Office
Prior art keywords
column
pressure
nitrogen
impure
vaporization
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 - Lifetime
Application number
EP92403330A
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German (de)
English (en)
French (fr)
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EP0547946B1 (fr
EP0547946A1 (fr
Inventor
Jean-Louis Girault
Philippe Mazières
Jean-Pierre Tranier
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Priority to EP96200235A priority Critical patent/EP0713069B1/fr
Publication of EP0547946A1 publication Critical patent/EP0547946A1/fr
Publication of EP0547946B1 publication Critical patent/EP0547946B1/fr
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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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • 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
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—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
    • F25J3/04406—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
    • F25J3/04418—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 with thermally overlapping high and low pressure columns
    • 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
    • F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/52—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the high pressure column of a double pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • 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
    • 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
    • F25J2250/10—Boiler-condenser with superposed stages
    • 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
    • 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
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/939—Partial feed stream expansion, air

Definitions

  • the present invention relates to a production process of impure oxygen by air distillation in an air distillation installation double column, in accordance with preamble to claim 1.
  • Such a process is known, for example, from document US-A-5,069,699.
  • the applications concerned by the invention are those which consume large amounts of impure oxygen.
  • a known means of exploiting this pressure consists in combining the air distillation apparatus with a gas turbine: the air to be separated is taken wholly or partially at discharge of the compressor from this turbine, and the low waste gas pressure from the distillation apparatus is returned after compression to the gas turbine, impure oxygen and nitrogen being sent for use under the pressure of the column that produces them.
  • US-A-5,069,699 describes an air distillation process in an installation comprising a double column and a column operating at very high pressure.
  • One of the two condensers in the column low pressure is supplied by an air flow or a nitrogen flow from of the column operating at very high pressure.
  • the invention aims to further reduce energy expenditure necessary for the production of impure oxygen and to overcome the defects of previous systems.
  • the subject of the invention is a method according to claim 1.
  • a second, more volatile vaporizing gas can be condensed as said first vaporizing gas but less volatile than top nitrogen of the medium pressure column, at an intermediate level between those of said condensations.
  • FIG 1 represent schematically an embodiment of the method air distillation according to the invention.
  • the modes of shown in Figures 2 to 4 are not covered by the revendications.
  • the installation shown in Figure 1 is intended to produce oxygen at a purity of the order 85% under a pressure of the order of 7.4 bar absolute. It essentially comprises a double column 1 of air distillation, consisting of a medium column pressure (or “MP column”) 2 operating at 15.7 bars absolute and a low pressure column (or “BP column”) 3 operating at 6.3 bar absolute, an exchange line main thermal 4, a sub-cooler 5, a auxiliary vaporizer-condenser 6 and a turbine 7 blowing air into the low pressure column.
  • the column 3 is superimposed on column 2 and contains in tank a vaporizer-condenser 8 and, above it, a second vaporizer-condenser 9.
  • the air to be distilled arrives below average pressure via line 10 and enters the line 4. Most of this air is cooled to the vicinity of its dew point and exit at the end cold of the exchange line, the rest having left the exchange line at an intermediate temperature, relaxed at low pressure in turbine 7 to ensure the keeping the installation cold, and blown to a intermediate level in column BP 3.
  • a fraction of the fully cooled air is introduced, via a pipe 11, at the base of the column MP 2, and the rest is condensed in the vaporizer-condenser 6; part of the liquid obtained is introduced via a pipe 12 at an intermediate point from column 2, and the rest is, after sub-cooling at 5 and expansion in an expansion valve 13, introduced at an intermediate point in column BP 3.
  • the approximately pure nitrogen produced at the head of the MP column is partly evacuated from the installation in as a product, after reheating in the line exchange, via line 16, and, for the rest, sent in gaseous form via line 17, below average pressure, in the upper evaporator-condenser 9. After condensation, this nitrogen is returned to reflux in head of the MP column via a pipe 18.
  • impure nitrogen gas withdrawn in an intermediate point in column 2 and, in this example, at the same level as the lean liquid, is sent via a line 19, at medium pressure, in the lower vaporizer-condenser 8.
  • the liquid thus obtained is returned to reflux in the MP column, about close to the same level, via line 20.
  • the temperature of the liquid in the bottom of the LP column is determined by that of the gas condensed in this vaporizer-condenser.
  • the temperature of the tank liquid, which is impure oxygen is relatively high. Therefore, for a desired purity of this impure oxygen, the pressure of the BP column, i.e. the low pressure, can be increased.
  • the vaporizer-condenser upper 9 is used to provide the necessary reflux at the top in the MP column.
  • the impure oxygen is withdrawn in the form gas from column BP 3, and is simply reheated in exchange line 4 before being evacuated via the driving 24. This is particularly interesting when impure oxygen is desired under low pressure. Consequently, the vaporizer-condenser 6 is deleted.
  • a fraction of the average air pressure cooled near its dew point is sent, via a line 26, into the vaporizer-condenser lower 8 instead of the intermediate gas of the Figure 1.
  • This intermediate gas feeds a intermediate vaporizer-condenser 27 located between the vaporizers-condensers lower 8 and higher 9.
  • Liquefied air from vaporizer-condenser 8 is sent in part, via line 28, in the MP column and in part, after sub-cooling in 5 and expansion in the valve trigger 13, in the LP column.
  • the impure oxygen is withdrawn under liquid form of the BP column tank and then it is brought by a pump 23 at the desired production pressure, then vaporized and heated under this pressure in the exchange line 4 before being evacuated from the installation via line 24.
  • This average nitrogen pressure combined with a medium pressure nitrogen stream taken from line 16, is compressed again by a compressor 33 at a vaporization pressure of impure oxygen compressed by pump 23, liquefied in the exchange line, then, after expansion in a valve trigger 34, introduced at reflux at the top of the column MP.
  • the installation in Figure 4 includes also a BP 3 column with minaret 30. However, unlike the previous case, it's high air pressure, boosted to a vaporization pressure of impure oxygen by a booster 35, which ensures the vaporization of impure oxygen in the exchange line 4. In this example, this air is, after liquefaction and expansion valve in expansion valve 36 and in the trigger 13, distributed between the two columns 2 and 3. by therefore, the compressor 33 and the expansion valve 34 from Figure 3 are deleted.
  • This nitrogen pressure can be chosen between average pressure and the pressure at which nitrogen condenses at the cold end of the exchange line.

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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)
EP92403330A 1991-12-18 1992-12-09 Procédé de production d'oxygène impur Expired - Lifetime EP0547946B2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP96200235A EP0713069B1 (fr) 1991-12-18 1992-12-09 Procédé et installation de séparation d'air

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9115705 1991-12-18
FR9115705A FR2685459B1 (fr) 1991-12-18 1991-12-18 Procede et installation de production d'oxygene impur.

Related Child Applications (2)

Application Number Title Priority Date Filing Date
EP96200235.8 Division-Into 1992-12-09
EP96200235A Division EP0713069B1 (fr) 1991-12-18 1992-12-09 Procédé et installation de séparation d'air

Publications (3)

Publication Number Publication Date
EP0547946A1 EP0547946A1 (fr) 1993-06-23
EP0547946B1 EP0547946B1 (fr) 1996-10-09
EP0547946B2 true EP0547946B2 (fr) 2000-03-22

Family

ID=9420168

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EP92403330A Expired - Lifetime EP0547946B2 (fr) 1991-12-18 1992-12-09 Procédé de production d'oxygène impur
EP96200235A Expired - Lifetime EP0713069B1 (fr) 1991-12-18 1992-12-09 Procédé et installation de séparation d'air

Family Applications After (1)

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EP96200235A Expired - Lifetime EP0713069B1 (fr) 1991-12-18 1992-12-09 Procédé et installation de séparation d'air

Country Status (9)

Country Link
US (1) US5392609A (zh)
EP (2) EP0547946B2 (zh)
CN (1) CN1068428C (zh)
AU (1) AU654601B2 (zh)
BR (1) BR9205050A (zh)
CA (1) CA2085561A1 (zh)
DE (2) DE69230975T2 (zh)
ES (2) ES2092661T3 (zh)
FR (1) FR2685459B1 (zh)

Families Citing this family (28)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5251451A (en) * 1992-08-28 1993-10-12 Air Products And Chemicals, Inc. Multiple reboiler, double column, air boosted, elevated pressure air separation cycle and its integration with gas turbines
US5355682A (en) * 1993-09-15 1994-10-18 Air Products And Chemicals, Inc. Cryogenic air separation process producing elevated pressure nitrogen by pumped liquid nitrogen
US5454227A (en) * 1994-08-17 1995-10-03 The Boc Group, Inc. Air separation method and apparatus
US5463871A (en) * 1994-10-04 1995-11-07 Praxair Technology, Inc. Side column cryogenic rectification system for producing lower purity oxygen
US5669237A (en) * 1995-03-10 1997-09-23 Linde Aktiengesellschaft Method and apparatus for the low-temperature fractionation of air
US5546767A (en) * 1995-09-29 1996-08-20 Praxair Technology, Inc. Cryogenic rectification system for producing dual purity oxygen
US5600970A (en) * 1995-12-19 1997-02-11 Praxair Technology, Inc. Cryogenic rectification system with nitrogen turboexpander heat pump
US5611219A (en) * 1996-03-19 1997-03-18 Praxair Technology, Inc. Air boiling cryogenic rectification system with staged feed air condensation
US5666824A (en) * 1996-03-19 1997-09-16 Praxair Technology, Inc. Cryogenic rectification system with staged feed air condensation
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DE69214409D1 (de) 1996-11-14
EP0547946B1 (fr) 1996-10-09
EP0713069B1 (fr) 2000-04-26
CA2085561A1 (fr) 1993-06-19
ES2145967T3 (es) 2000-07-16
US5392609A (en) 1995-02-28
AU654601B2 (en) 1994-11-10
CN1068428C (zh) 2001-07-11
DE69230975T2 (de) 2000-10-05
FR2685459A1 (fr) 1993-06-25
DE69230975D1 (de) 2000-05-31
DE69214409T3 (de) 2000-07-13
CN1088301A (zh) 1994-06-22
DE69214409T2 (de) 1997-05-22
AU3022192A (en) 1993-06-24
FR2685459B1 (fr) 1994-02-11
EP0713069A1 (fr) 1996-05-22
BR9205050A (pt) 1993-08-10
ES2092661T3 (es) 1996-12-01
EP0547946A1 (fr) 1993-06-23

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