EP1623172A1 - Verfahren und system zur herstellung von druckluftgas durch kryogene destillation von luft - Google Patents

Verfahren und system zur herstellung von druckluftgas durch kryogene destillation von luft

Info

Publication number
EP1623172A1
EP1623172A1 EP04742833A EP04742833A EP1623172A1 EP 1623172 A1 EP1623172 A1 EP 1623172A1 EP 04742833 A EP04742833 A EP 04742833A EP 04742833 A EP04742833 A EP 04742833A EP 1623172 A1 EP1623172 A1 EP 1623172A1
Authority
EP
European Patent Office
Prior art keywords
air
turbine
column
pressure
booster
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP04742833A
Other languages
English (en)
French (fr)
Other versions
EP1623172B1 (de
Inventor
Patrick Le Bot
Olivier Decayeux
Frédéric Judas
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
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
LAir Liquide SA a Directoire et Conseil de Surveillance 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 Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude, LAir Liquide SA a Directoire et Conseil de Surveillance pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Priority to PL04742833T priority Critical patent/PL1623172T3/pl
Publication of EP1623172A1 publication Critical patent/EP1623172A1/de
Application granted granted Critical
Publication of EP1623172B1 publication Critical patent/EP1623172B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—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
    • F25J3/04006—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
    • F25J3/0409—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
    • F25J3/04151—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
    • F25J3/04248—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
    • F25J3/04284—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
    • F25J3/04309—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 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.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/42—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being air

Definitions

  • the present invention relates to a method and an installation for producing gas from pressurized air by cryogenic distillation of air.
  • Some processes such as those described in EP-A-0 504 029, produce oxygen under high pressure (> 15 bar) using a single compressor to compress the air at a pressure well above the pressure of the medium pressure column. These processes are adapted to a context in which the investment takes precedence because they suffer from a very important energy consumption when no production of liquid is required.
  • Temperatures are considered to be close if they differ at most 10 ° C, preferably at most 5 ° C.
  • the exchange line is the main heat exchanger where the gases produced by the column system are heated and where the air for distillation is cooled.
  • An object of the invention is to propose an alternative for producing process diagrams making it possible to improve the energy performances by type 1 processes while keeping a lower need for exchange volume than cold compression type 2 schemes as described below.
  • a process for separating air by cryogenic distillation in a column system comprising a double column or a triple column, the column operating at the highest pressure operating at a so-called average pressure.
  • pressure in which: a) all air is heated to a high pressure at least 5 to 10 bar above the medium pressure.
  • a portion of the air comprising between 10% and 50% of the air flow under high pressure, is withdrawn from an exchange line, at a temperature close to the (pseudo) vaporization temperature of the liquid, su ⁇ ressée from at least the high pressure by means of a cold su ⁇ resseur, then is returned in the exchange line, and at least a portion liquefies the cold end, then is sent in at least one column of the system of columns after expansion, c) another fraction of the air at least the high pressure, possibly constituting the rest of the air at high pressure, is expanded in a Claude turbine and then sent into the medium pressure column.
  • the cold su ⁇ resseur is coupled to a drive device among: i) a turbine (ii) an electric motor; (iii) a combination of an expansion turbine and an electric motor.
  • At least a portion of the high pressure air is overpressed before entering the main exchange line in a hot booster and then cools in the exchange line. all the air to be distilled is overpressed at a pressure higher than the high pressure in the hot booster.
  • a part of the air coming from the hot booster is sent to the Claude turbine at the outlet pressure of the hot booster.
  • a part of the air coming from the hot booster cools in the exchange line, is expanded, liquefied and sent to at least one column of the column system.
  • a nitrogen-enriched gas flow from a column of the column system is partially heated in the exchange line, is expanded in the expansion turbine constituting the (or part of) the entrainment device and is heated in the exchange line.
  • An air flow is expanded in the expansion turbine constituting the (or part of) the drive device and the expanded air is sent to a column of the column system, in particular to the low pressure column.
  • the liquid from the columns which vaporizes is enriched in oxygen with respect to air.
  • the suction temperature of the cold booster is close to, preferably substantially equal to that of vaporization of the liquid withdrawn from the columns and introduced pressurized into the exchange line.
  • the suction temperature of the Claude turbine is lower than the suction temperature of the cold booster.
  • the suction temperature of the turbine constituting the or part of the drive device is greater than the suction temperature of the cold booster.
  • an air separation installation by cryogenic distillation comprising: a) a heat exchange line b) a double or triple air separation column whose column operating at the highest pressure operates at a medium pressure c) a Claude turbine d) a hot booster coupled to the turbine Claude e) a cold booster f) a cold su ⁇ resseur drive device consisting of a turbine, an electric motor or a combination of the two, g) means for sending all the compressed air for distillation to the hot booster, means for sending the pressurized air to the heat exchange line; h) means for withdrawing a first part of the air at an intermediate level of the exchange line, preferably constituting
  • the turbine constituting the drive device or forming part thereof may be an air expansion turbine, in particular an insufflation turbine, or a nitrogen expansion turbine.
  • Figures 1 to 4 each represent an air separation apparatus according to the invention.
  • air is compressed to a pressure of about 15 bar in a compressor (not shown) and then purified to remove impurities (not shown).
  • the purified air is supercharged at a pressure of about 18 bar in a booster 5.
  • the supercharged air cools by heat exchange with a refrigerant such as water and is sent to the hot end of the exchange line 9. All air cools down to an intermediate temperature of the exchange line and then air is divided in two.
  • a first portion of the air 11 comprising between 10% and 50% of the air flow under high pressure is sent to a su ⁇ resseur 23 aspiring at a cryogenic temperature.
  • the supercharged air is then sent to the exchange line, without being cooled at the outlet of the su ⁇ resseur, at a pressure of about 31 bar, continues cooling and liquefies in particular by heat exchange with a flow of liquid oxygen pumped 25 which pseudo vaporizes.
  • the remainder of the air 13 comprising between 50 and 90% of the high-pressure air cools to a temperature lower than the suction temperature of the booster 23 and is expanded in a Claude turbine 17 and sent to the middle column pressure, thus constituting the only flow of gaseous air sent to the double column.
  • a nitrogen-enriched gas flow 31 from the medium pressure column 100 heats up in the exchange line, leaves at a temperature higher than the inlet temperature of the Claude 17 turbine and is sent to an expansion turbine 119.
  • Nitrogen expanded substantially at low pressure and substantially at the temperature of the cold end of the exchange line is reintroduced into the exchange line where it heats up or joins a nitrogen-enriched gas 33 withdrawn from the lower column. pressure and the nitrogen flow formed 29 is heated through completely the exchange line.
  • the nitrogen turbine 119 is coupled to the cold booster 23 while the Claude turbine 17 is coupled to the hot booster 5.
  • the expansion turbine 119 is not an essential element of the invention and the drive of the cold booster 23 can be replaced by an electric motor. Similarly, the expansion turbine 119 may be replaced by an air expansion turbine.
  • the column system of FIG. 1 and all the figures is a conventional air separation apparatus consisting of a medium pressure column 100 thermally connected to a low pressure column 200 by means of a bottom reboiler of the low pressure column. heated by a medium pressure nitrogen flow. Other types of reboiling can obviously be considered.
  • the medium pressure column 100 operates at a pressure of 5.5 bar but can operate at a higher pressure.
  • the gaseous air 35 from the turbine 17 is sent to the bottom of the medium pressure column 100.
  • the liquefied air 37 is expanded in the valve 39, divided in two, a part being sent to the medium pressure column 100 and the rest to the low pressure column 200.
  • Rich liquid 51, lower lean liquid 53 and upper lean liquid 55 are sent from the medium pressure column 100 to the low pressure column 200 after expansion steps in the valves and subcooling.
  • Oxygen enriched fluids 57 and nitrogen enriched 59 are optionally withdrawn as final products of the double column.
  • Oxygen-enriched liquid is pressurized by the pump 500 and sent as a pressurized liquid to the exchange line 9.
  • other liquids, pressurized or otherwise such as other liquid oxygen different pressure, liquid nitrogen and liquid argon, can vaporize in the exchange line 9.
  • Residual nitrogen 27 is withdrawn at the top of the low pressure column and is heated in the exchange line 9, after being used to subcool the reflux liquids 51, 53, 55.
  • the column may optionally produce argon by treating a flow rate withdrawn in low pressure column 200.
  • a portion 41 of the high pressure air unpressurized in su ⁇ ressor 23 can be liquefied in the exchange line by heat exchange with the vaporizing oxygen, is expanded in a valve 43 to the medium pressure and mixes with the liquefied air 37. 11 will be understood that if the air is at supercritical pressure output of su ⁇ resseur 5, the liquefaction will take place after relaxation in the valves 39, 43.
  • FIG. 2 differs from FIG. 1 in that there is no medium gas pressure nitrogen withdrawal at the head of the medium pressure column 100.
  • the medium pressure nitrogen turbine 119 is replaced by an insufflation turbine 119A. Part 61 of the air coming from the Claude turbine 17 is sent to the blowing turbine and the air expanded in the turbine 119A is sent to the low pressure column 200.
  • the hot su ⁇ resseur 5 is always coupled to the turbine Claude but the cold booster 23 is coupled to the insufflation turbine.
  • the liquid air relief valves are also different in Figure 2 because the liquid flow rates are only relaxed after division to form the flow rates for the medium pressure and low pressure columns.
  • This kind of process is more suitable for producing low purity oxygen.
  • Figure 3 is similar to Figures 1 and 2 but does not include any turbine apart from the Claude turbine.
  • the cold booster 23 is coupled to a motor 61 and the hot booster 5 is coupled to the turbine Claude.

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)
EP04742833.9A 2003-05-05 2004-04-06 Verfahren und vorrichtung zur erzeugung eines durch tieftemperaturzerlegung von luft gewonnenen druckgases Expired - Lifetime EP1623172B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PL04742833T PL1623172T3 (pl) 2003-05-05 2004-04-06 Sposób i instalacja do wytwarzania gazu ze sprężonego powietrza z wykorzystaniem destylacji kriogenicznej powietrza

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR0350142A FR2854683B1 (fr) 2003-05-05 2003-05-05 Procede et installation de production de gaz de l'air sous pression par distillation cryogenique d'air
PCT/FR2004/050146 WO2004099691A1 (fr) 2003-05-05 2004-04-06 Procede et installation de production de gaz de l'air sous pression par distillation cryogenique d'air

Publications (2)

Publication Number Publication Date
EP1623172A1 true EP1623172A1 (de) 2006-02-08
EP1623172B1 EP1623172B1 (de) 2015-12-09

Family

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP04742833.9A Expired - Lifetime EP1623172B1 (de) 2003-05-05 2004-04-06 Verfahren und vorrichtung zur erzeugung eines durch tieftemperaturzerlegung von luft gewonnenen druckgases

Country Status (8)

Country Link
US (1) US9945606B2 (de)
EP (1) EP1623172B1 (de)
JP (1) JP4728219B2 (de)
CN (1) CN1784579B (de)
FR (1) FR2854683B1 (de)
HU (1) HUE026528T2 (de)
PL (1) PL1623172T3 (de)
WO (1) WO2004099691A1 (de)

Families Citing this family (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2865024B3 (fr) * 2004-01-12 2006-05-05 Air Liquide Procede et installation de separation d'air par distillation cryogenique
US7487648B2 (en) * 2006-03-10 2009-02-10 Praxair Technology, Inc. Cryogenic air separation method with temperature controlled condensed feed air
FR2913759B1 (fr) * 2007-03-13 2013-08-16 Air Liquide Procede et appareil de production de gaz de l'air sous forme gazeuse et liquide a haute flexibilite par distillation cryogenique.
FR2913760B1 (fr) * 2007-03-13 2013-08-16 Air Liquide Procede et appareil de production de gaz de l'air sous forme gazeuse et liquide a haute flexibilite par distillation cryogenique
DE102007031765A1 (de) * 2007-07-07 2009-01-08 Linde Ag Verfahren zur Tieftemperaturzerlegung von Luft
BRPI0721930A2 (pt) * 2007-08-10 2014-03-18 Air Liquide Processo e aparelho para a separação de ar por destilação criogênica
EP2176610B1 (de) * 2007-08-10 2019-04-24 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Verfahren zur trennung von luft durch kryogene destillation
FR2953915B1 (fr) * 2009-12-11 2011-12-02 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
EP2369281A1 (de) * 2010-03-09 2011-09-28 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
DE102010055448A1 (de) * 2010-12-21 2012-06-21 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
FR2973485B1 (fr) * 2011-03-29 2017-11-24 L'air Liquide Sa Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de separation d'air par distillation cryogenique
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US20060277944A1 (en) 2006-12-14
PL1623172T3 (pl) 2016-06-30
CN1784579A (zh) 2006-06-07
FR2854683B1 (fr) 2006-09-29
HUE026528T2 (en) 2016-06-28
CN1784579B (zh) 2010-10-06
JP2006525487A (ja) 2006-11-09
FR2854683A1 (fr) 2004-11-12
WO2004099691A1 (fr) 2004-11-18
EP1623172B1 (de) 2015-12-09
US9945606B2 (en) 2018-04-17
JP4728219B2 (ja) 2011-07-20

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