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EP0605262A1 - Process and apparatus for the production of gaseous oxygen under pressure - Google Patents

Process and apparatus for the production of gaseous oxygen under pressure Download PDF

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Publication number
EP0605262A1
EP0605262A1 EP93402665A EP93402665A EP0605262A1 EP 0605262 A1 EP0605262 A1 EP 0605262A1 EP 93402665 A EP93402665 A EP 93402665A EP 93402665 A EP93402665 A EP 93402665A EP 0605262 A1 EP0605262 A1 EP 0605262A1
Authority
EP
European Patent Office
Prior art keywords
column
low pressure
oxygen
pressure
pressure column
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
EP93402665A
Other languages
German (de)
French (fr)
Other versions
EP0605262B1 (en
Inventor
Alain Guillard
Norbert Rieth
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
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Publication date
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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
Publication of EP0605262A1 publication Critical patent/EP0605262A1/en
Application granted granted Critical
Publication of EP0605262B1 publication Critical patent/EP0605262B1/en
Anticipated expiration legal-status Critical
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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
    • F25J3/042—Division of the main heat exchange line in consecutive sections having different functions having an intermediate feed connection
    • 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
    • F25J3/04157—Afterstage cooling and so-called "pre-cooling" of the feed air upstream the air purification unit and main heat exchange line
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F25J3/0426—The cryogenic component does not participate in the fractionation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • 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
    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04854—Safety aspects of operation
    • F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/0489—Modularity and arrangement of parts of the air fractionation unit, in particular of the cold box, e.g. pre-fabrication, assembling and erection, dimensions, horizontal layout "plot"
    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04945—Details of internal structure; insulation and housing of the cold box
    • 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
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/50—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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F25J2240/44—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 nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank
    • 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
    • Y10S62/912—External refrigeration system
    • Y10S62/913—Liquified gas

Definitions

  • the present invention relates to a process for producing gaseous oxygen under pressure by means of a double distillation column.
  • gaseous oxygen under pressure is generally carried out either by compression of gaseous oxygen withdrawn from the low pressure column under a pressure close to atmospheric pressure, or by vaporization of liquid oxygen brought by pump to the production pressure.
  • the corresponding installations are complex, because they require special rotating machines such as an oxygen compressor or one or more expansion turbines.
  • the object of the invention is to provide a process which makes it possible to produce oxygen gas in a particularly economical manner under moderate pressure.
  • the invention also relates to an installation intended for the implementation of such a method.
  • This installation of the type comprising: an air compressor; a compressed air cleaning device; a double column for the distillation of purified air, itself comprising a medium pressure column and a low pressure column coupled by a vaporizer-condenser; a heat exchange line for cooling the purified air by indirect heat exchange with the products coming from the double column; and means for keeping the installation cold, is characterized in that the low pressure column operates under a pressure markedly higher than atmospheric pressure and slightly higher than the oxygen production pressure, this low pressure being in particular of l '' from 2 to 5 bars, in that an oxygen production pipe is directly connected to the tank of the low pressure column to extract gaseous oxygen therefrom, and in that the means for keeping cold include an expansion valve free of at least one gaseous product leaving the low pressure column.
  • the double column can in particular be isolated under vacuum, in particular by a vacuum envelope which contains only the double column and pipe sections, the rest of the cold parts of the installation, with the possible exception sources of liquid nitrogen and / or liquid oxygen and the pipes which leave therefrom, being insulated by a cold box at atmospheric pressure containing a solid insulator, in particular particulate.
  • the installation represented in FIG. 1 essentially comprises an air compressor 1, an apparatus 2 for purification by adsorption, a heat exchange line 3, a sub-cooler 4 and a double distillation column 5.
  • the latter is essentially consisting of a medium pressure column 6 surmounted by a low pressure column 7, and of a vaporizer-condenser 8 which brings the head vapor (practically pure nitrogen) of column 6 and the tank liquid (oxygen at the desired purity) from column 7.
  • the air to be distilled is compressed in 1 to a pressure, called medium pressure, of the order of 8 to 16 bars, purified in water and in carbon dioxide in 2, cooled near its dew point in 3 and introduced into the tank of column 6.
  • the "rich liquid” (oxygen-enriched air) collected in the tank of this column is sub-cooled in 4, expanded in an expansion valve 9 at a pressure, called low pressure, which is substantially the production pressure, of the order from 2 to 5 bars, and introduced at an intermediate level of column 7 via a pipe 10.
  • "Lean liquid” (practically pure nitrogen) collected at the top of column 6 is sub-cooled at 4, expanded in a valve trigger 11 at low pressure, and introduced at the head of column 7 via a pipe 12.
  • the production oxygen is withdrawn in the gaseous form from the tank of column 7, heated in the exchange line 3 and recovered directly in as a product via a production line 13.
  • the residual gas W (impure nitrogen), drawn off at the top of the column 7 via a pipe 14, is expanded in free expansion to a pressure slightly higher than atmospheric pressure in a valve. expansion 15, heated in the sub-cooler 4 then in the exchange line 3, and evacuated via a pipe 16. This gas can be used to regenerate the adsorbers of the device 2.
  • the installation shown is thermally insulated as follows.
  • the double column 5 is placed in a vacuum envelope 22, which ensures high performance insulation.
  • This envelope contains, in addition to the double column, only the sections of pipe which terminate there or leave it, these pipes passing through the envelope by means of appropriate fittings 23. In practice, it is advantageous to gather all the fittings 23 in one envelope region.
  • the vacuum envelope can have a diameter closely adapted to the outside diameter of the double column, which can be of constant diameter over its entire height, which makes it possible to produce an assembly double column 5-envelope 22 conveniently transportable.
  • this solution is also very advantageous, although it is much less expensive than vacuum insulation enclosing the entire installation.
  • 75 to 85% of the heat losses are borne by the double column and, in the heat exchange line, the losses are concentrated in the coldest part.
  • the insulation performance of the 22-24 assembly is of the order of 90% of that which would be obtained with vacuum insulation of the entire installation.
  • the double column may comprise a "minaret", that is to say an upper section of the low pressure column 7 making it possible to produce nitrogen gas at its top under low pressure.
  • this nitrogen gas can also be expanded in an expansion valve to the vicinity of atmospheric pressure to produce cold, before being heated in 4 and then in 3 and then being recovered as a second product of the installation.
  • the simplicity of the installation according to the invention makes it particularly advantageous for the production of moderate quantities, for example of the order of a few tens of tonnes per day, of gaseous oxygen under a pressure of a few bars.
  • the cold resistance of the installation is effected by free expansion of the waste gas W at 15, supplemented by a supply of liquid oxygen coming from a source 19 constituted as previously from a storage 19A at atmospheric pressure and a pump 19B.
  • the additional liquid oxygen pumped in 19B at a pressure somewhat higher than the low pressure, is injected, at an intermediate point 25 of the heat exchange line 3, in gaseous oxygen during heating.
  • a liquid oxygen purge pipe 26, fitted with a valve 27, leaves from the tank of the column 7 and opens into the storage 19A to supply it in part, the additional liquid oxygen being supplied by tankers 28.
  • the purge intended to evacuate the hydrocarbons from column 7, corresponds to approximately 0.2% of the flow of treated air and is preferably carried out batchwise, generally automatically; it is independent of the "bottle feeding" of the installation by liquid oxygen.
  • the injection point 25 is chosen so that the liquid oxygen vaporizes at a sufficiently high temperature so that the hydrocarbons no longer present a danger of explosion or flammability during the vaporization of the oxygen.
  • This temperature can thus be of the order of -100 ° C.

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Abstract

According to this process, which employs a double air distillation column (5): - the low-pressure column (7) is operated under a pressure which is markedly greater than atmospheric pressure, in particular of the order of from 2 to 5 bar, and the medium-pressure column (6) is operated under a corresponding pressure, in particular of the order of from 8 to 16 bar; - the production gaseous oxygen is directly recovered in the tank of the low-pressure column, and - the apparatus is kept cold, at least partly, by free expansion of at least one gaseous product leaving the low-pressure column. Application to the production of gaseous oxygen under a pressure of a few bar. <IMAGE>

Description

La présente invention est relative à un procédé de production d'oxygène gazeux sous pression au moyen d'une double colonne de distillation.The present invention relates to a process for producing gaseous oxygen under pressure by means of a double distillation column.

Les pressions dont il est question dans le présent mémoire sont des pressions absolues.The pressures discussed in this brief are absolute pressures.

La production d'oxygène gazeux sous pression s'effectue généralement soit par compression d'oxygène gazeux soutiré de la colonne basse pression sous une pression voisine de la pression atmosphérique, soit par vaporisation d'oxygène liquide amené par pompe à la pression de production. Les installations correspondantes sont complexes, car elles nécessitent des machines tournantes spéciales tel qu'un compresseur d'oxygène ou une ou plusieurs turbines de détente.The production of gaseous oxygen under pressure is generally carried out either by compression of gaseous oxygen withdrawn from the low pressure column under a pressure close to atmospheric pressure, or by vaporization of liquid oxygen brought by pump to the production pressure. The corresponding installations are complex, because they require special rotating machines such as an oxygen compressor or one or more expansion turbines.

L'invention a pour but de fournir un procédé permettant de produire de façon particulièrement économique de l'oxygène gazeux sous une pression modérée.The object of the invention is to provide a process which makes it possible to produce oxygen gas in a particularly economical manner under moderate pressure.

A cet effet, le procédé suivant l'invention est caractérisé en ce que :

  • on fait fonctionner la colonne basse pression sous une pression nettement supérieure à la pression atmosphérique et légèrement supérieure à la pression de production d'oxygène, cette basse pression étant notamment de l'ordre de 2 à 5 bars, et on fait fonctionner la colonne moyenne pression sous une pression correspondante, notamment de l'ordre de 8 à 16 bars;
  • on récupère directement l'oxygène gazeux de production en cuve de la colonne basse pression, et
  • on maintient en froid l'installation, au moins en partie, par détente libre d'au moins un produit gazeux sortant de la colonne basse pression.
To this end, the method according to the invention is characterized in that:
  • the low pressure column is operated at a pressure markedly higher than atmospheric pressure and slightly higher than the oxygen production pressure, this low pressure being in particular of the order of 2 to 5 bars, and the medium column is operated pressure under a corresponding pressure, in particular of the order of 8 to 16 bars;
  • the production gaseous oxygen is directly recovered from the bottom of the low pressure column, and
  • the installation is kept cold, at least in part, by free expansion of at least one gaseous product leaving the low pressure column.

Suivant d'autres caractéristiques :

  • on détend par détente libre un gaz résiduaire soutiré de la tête de la colonne basse pression;
  • on injecte dans la colonne basse pression un débit d'azote liquide provenant d'une source extérieure à la double colonne;
  • on injecte dans la colonne basse pression un débit d'oxygène liquide provenant d'une source extérieure à la double colonne;
  • on injecte dans l'oxygène gazeux, en un point intermédiaire de la ligne d'échange thermique associée à la double colonne, un débit d'oxygène liquide provenant d'une source extérieure à la double colonne, et on envoie dans ladite source de l'oxygène liquide de purge soutiré de la cuve de la colonne basse pression;
  • on prérefroidit l'air à traiter, avant son épuration par adsorption, au moyen d'un groupe frigorifique.
According to other characteristics:
  • a residual gas is released by free expansion withdrawn from the head of the low pressure column;
  • a flow of liquid nitrogen from a source external to the double column is injected into the low pressure column;
  • a flow of liquid oxygen from a source external to the double column is injected into the low pressure column;
  • is injected into the gaseous oxygen, at an intermediate point of the heat exchange line associated with the double column, a flow of liquid oxygen from a source external to the double column, and is sent into said source of l liquid purge oxygen withdrawn from the tank of the low pressure column;
  • the air to be treated is precooled, before it is purified by adsorption, by means of a refrigeration unit.

L'invention a également pour objet une installation destinée à la mise en oeuvre d'un tel procédé. Cette installation, du type comprenant : un compresseur d'air; un appareil d'épuration de l'air comprimé; une double colonne de distillation de l'air épuré, comprenant elle-même une colonne moyenne pression et une colonne basse pression couplées par un vaporiseur-condenseur; une ligne d'échange thermique pour refroidir l'air épuré par échange de chaleur indirect avec les produits provenant de la double colonne; et des moyens de maintien en froid de l'installation, est caractérisée en ce que la colonne basse pression fonctionne sous une pression nettement supérieure à la pression atmosphérique et légèrement supérieure à la pression de production d'oxygène, cette basse pression étant notamment de l'ordre de 2 à 5 bars, en ce qu'une conduite de production d'oxygène est directement reliée à la cuve de la colonne basse pression pour en soutirer de l'oxygène gazeux, et en ce que les moyens de maintien en froid comprennent une vanne de détente libre d'au moins un produit gazeux sortant de la colonne basse pression.The invention also relates to an installation intended for the implementation of such a method. This installation, of the type comprising: an air compressor; a compressed air cleaning device; a double column for the distillation of purified air, itself comprising a medium pressure column and a low pressure column coupled by a vaporizer-condenser; a heat exchange line for cooling the purified air by indirect heat exchange with the products coming from the double column; and means for keeping the installation cold, is characterized in that the low pressure column operates under a pressure markedly higher than atmospheric pressure and slightly higher than the oxygen production pressure, this low pressure being in particular of l '' from 2 to 5 bars, in that an oxygen production pipe is directly connected to the tank of the low pressure column to extract gaseous oxygen therefrom, and in that the means for keeping cold include an expansion valve free of at least one gaseous product leaving the low pressure column.

Dans une telle installation, la double colonne peut en particulier être isolée sous vide, notamment par une enveloppe sous vide qui ne contient que la double colonne et des tronçons de conduite, le reste des parties froides de l'installation, à l'exception éventuellement des sources d'azote liquide et/ou d'oxygène liquide et des conduites qui en partent, étant isolées par une boîte froide à la pression atmosphérique contenant un isolant solide, notamment particulaire.In such an installation, the double column can in particular be isolated under vacuum, in particular by a vacuum envelope which contains only the double column and pipe sections, the rest of the cold parts of the installation, with the possible exception sources of liquid nitrogen and / or liquid oxygen and the pipes which leave therefrom, being insulated by a cold box at atmospheric pressure containing a solid insulator, in particular particulate.

Des exemples de mise en oeuvre de l'invention vont maintenant être décrits en regard des dessins annexés, sur lesquels :

  • la Figure 1 représente schématiquement une installation de production d'oxygène conforme à l'invention; et
  • la Figure 2 représente schématiquement une variante.
Examples of implementation of the invention will now be described with reference to the accompanying drawings, in which:
  • Figure 1 schematically shows an oxygen production installation according to the invention; and
  • Figure 2 schematically shows a variant.

L'installation représentée à la Figure 1 comprend essentiellement un compresseur d'air 1, un appareil 2 d'épuration par adsorption, une ligne d'échange thermique 3, un sous-refroidisseur 4 et une double colonne de distillation 5. Cette dernière est essentiellement constituée d'une colonne moyenne pression 6 surmontée d'une colonne basse pression 7, et d'un vaporiseur-condenseur 8 qui met en relation d'échange thermique indirect la vapeur de tête (azote pratiquement pur) de la colonne 6 et le liquide de cuve (oxygène à la pureté désirée) de la colonne 7.The installation represented in FIG. 1 essentially comprises an air compressor 1, an apparatus 2 for purification by adsorption, a heat exchange line 3, a sub-cooler 4 and a double distillation column 5. The latter is essentially consisting of a medium pressure column 6 surmounted by a low pressure column 7, and of a vaporizer-condenser 8 which brings the head vapor (practically pure nitrogen) of column 6 and the tank liquid (oxygen at the desired purity) from column 7.

En fonctionnement, l'air à distiller est comprimé en 1 à une pression, dite moyenne pression, de l'ordre de 8 à 16 bars, épuré en eau et en anhydride carbonique en 2, refroidi au voisinage de son point de rosée en 3 et introduit en cuve de la colonne 6. Le "liquide riche" (air enrichi en oxygène) recueilli en cuve de cette colonne est sous-refroidi en 4, détendu dans une vanne de détente 9 à une pression, dite basse pression, qui est sensiblement la pression de production, de l'ordre de 2 à 5 bars, et introduit à un niveau intermédiaire de la colonne 7 via une conduite 10. Du "liquide pauvre" (azote pratiquement pur) recueilli en tête de la colonne 6 est sous-refroidi en 4, détendu dans une vanne de détente 11 à la basse pression, et introduit en tête de la colonne 7 via une conduite 12. L'oxygène de production est soutiré sous forme gazeuse de la cuve de la colonne 7, réchauffé dans la ligne d'échange 3 et récupéré directement en tant que produit via une conduite de production 13.In operation, the air to be distilled is compressed in 1 to a pressure, called medium pressure, of the order of 8 to 16 bars, purified in water and in carbon dioxide in 2, cooled near its dew point in 3 and introduced into the tank of column 6. The "rich liquid" (oxygen-enriched air) collected in the tank of this column is sub-cooled in 4, expanded in an expansion valve 9 at a pressure, called low pressure, which is substantially the production pressure, of the order from 2 to 5 bars, and introduced at an intermediate level of column 7 via a pipe 10. "Lean liquid" (practically pure nitrogen) collected at the top of column 6 is sub-cooled at 4, expanded in a valve trigger 11 at low pressure, and introduced at the head of column 7 via a pipe 12. The production oxygen is withdrawn in the gaseous form from the tank of column 7, heated in the exchange line 3 and recovered directly in as a product via a production line 13.

Pour assurer le maintien en froid de l'installation, le gaz résiduaire W (azote impur), soutiré au sommet de la colonne 7 via une conduite 14, est détendu en détente libre à une pression légèrement supérieure à la pression atmosphérique dans une vanne de détente 15, réchauffé dans le sous-refroidisseur 4 puis dans la ligne d'échange 3, et évacué via une conduite 16. Ce gaz peut servir à régénérer les adsorbeurs de l'appareil 2.To keep the installation cold, the residual gas W (impure nitrogen), drawn off at the top of the column 7 via a pipe 14, is expanded in free expansion to a pressure slightly higher than atmospheric pressure in a valve. expansion 15, heated in the sub-cooler 4 then in the exchange line 3, and evacuated via a pipe 16. This gas can be used to regenerate the adsorbers of the device 2.

Si le froid produit par cette détente libre est insuffisant, on peut le compléter par l'un au moins des moyens suivants, représentés en trait mixte sur le dessin.

  • Une source 17 d'azote liquide sous la basse pression, reliée à la tête de la colonne 7 via une conduite 18 et munie de moyens de régulation de débit. Comme représenté, il peut s'agir notamment d'un stockage 17A d'azote liquide sous la pression atmosphérique muni à sa sortie d'une pompe 17B.
  • Une source 19 d'oxygène liquide sous la basse pression, reliée à la cuve de la colonne 7 via une conduite 20 et munie de moyens de régulation de débit. Comme représenté, il peut s'agir de nouveau d'un stockage 19A d'oxygène liquide sous la pression atmosphérique muni à sa sortie d'une pompe 19B.
  • Un groupe frigorifique 21, par exemple à l'ammoniac, monté entre le compresseur 1 et l'appareil d'épuration 2 et prérefroidissant l'air comprimé jusqu'à une température de l'ordre de 0 à +° 5°C par exemple.
If the cold produced by this free expansion is insufficient, it can be supplemented by at least one of the following means, shown in phantom in the drawing.
  • A source 17 of liquid nitrogen under low pressure, connected to the head of the column 7 via a pipe 18 and provided with flow control means. As shown, it may especially be a storage 17A of liquid nitrogen at atmospheric pressure provided at its outlet with a pump 17B.
  • A source 19 of liquid oxygen under low pressure, connected to the tank of the column 7 via a pipe 20 and provided with flow regulation means. As shown, it may again be a storage 19A of liquid oxygen under atmospheric pressure provided at its outlet with a pump 19B.
  • A refrigeration unit 21, for example with ammonia, mounted between the compressor 1 and the purification device 2 and pre-cooling the compressed air to a temperature of the order of 0 to + 5 ° C for example .

L'installation représentée est isolée thermiquement de la manière suivante.The installation shown is thermally insulated as follows.

D'une part, la double colonne 5 est disposée dans une enveloppe sous vide 22, qui en assure une isolation à haute performance. Cette enveloppe ne contient, outre la double colonne, que les tronçons de conduite qui y aboutissent ou en partent, ces conduites traversant l'enveloppe au moyen de raccords appropriés 23. En pratique, il est avantageux de rassembler tous les raccords 23 dans une même région de l'enveloppe.On the one hand, the double column 5 is placed in a vacuum envelope 22, which ensures high performance insulation. This envelope contains, in addition to the double column, only the sections of pipe which terminate there or leave it, these pipes passing through the envelope by means of appropriate fittings 23. In practice, it is advantageous to gather all the fittings 23 in one envelope region.

D'autre part, à l'exception des sources de liquides cryogéniques 17 et 19 et des conduites qui en partent, qui possèdent leur propre isolation, généralement sous vide, toutes les autres parties froides de l'installation sont isolées au moyen d'une boîte froide 24 sous la pression atmosphérique contenant un matériau isolant solide particulaire, qui est de préférence de la perlite.On the other hand, with the exception of the sources of cryogenic liquids 17 and 19 and the pipes which leave therefrom, which have their own insulation, generally under vacuum, all the other cold parts of the installation are insulated by means of a cold box 24 at atmospheric pressure containing a particulate solid insulating material, which is preferably perlite.

Ce mode d'isolation est très avantageux d'une part, l'enveloppe sous vide peut avoir un diamètre étroitement adapté au diamètre extérieur de la double colonne, laquelle peut être de diamètre constant sur toute sa hauteur, ce qui permet de réaliser un ensemble double colonne 5-enveloppe 22 commodément transportable.This isolation method is very advantageous on the one hand, the vacuum envelope can have a diameter closely adapted to the outside diameter of the double column, which can be of constant diameter over its entire height, which makes it possible to produce an assembly double column 5-envelope 22 conveniently transportable.

De plus, tous les accessoires froids tels que 9, 11, 15 sont facilement accessibles puisqu'ils sont constamment à la pression atmosphérique.In addition, all cold accessories such as 9, 11, 15 are easily accessible since they are constantly at atmospheric pressure.

Du point de vue énergétique, cette solution est également très avantageuse, bien qu'elle soit beaucoup moins coûteuse qu'une isolation sous vide renfermant l'ensemble de l'installation. En effet, dans une installation de distillation d'air, 75 à 85% des pertes thermiques sont supportées par la double colonne et, dans la ligne d'échange thermique, les pertes sont concentrées dans la partie la plus froide. Au total, les performances d'isolation de l'ensemble 22-24 sont de l'ordre de 90% de celles qui seraient obtenues avec une isolation sous vide de l'ensemble de l'installation.From an energy point of view, this solution is also very advantageous, although it is much less expensive than vacuum insulation enclosing the entire installation. In fact, in an air distillation installation, 75 to 85% of the heat losses are borne by the double column and, in the heat exchange line, the losses are concentrated in the coldest part. In total, the insulation performance of the 22-24 assembly is of the order of 90% of that which would be obtained with vacuum insulation of the entire installation.

En variante, la double colonne peut comporter un "minaret", c'est-à-dire un tronçon supérieur de la colonne basse pression 7 permettant de produire à son sommet de l'azote gazeux sous la basse pression. Dans ce cas, cet azote gazeux peut également être détendu dans une vanne de détente jusqu'au voisinage de la pression atmosphérique pour produire du froid, avant d'être réchauffé en 4 puis en 3 puis d'être récupéré en tant que second produit de l'installation.As a variant, the double column may comprise a "minaret", that is to say an upper section of the low pressure column 7 making it possible to produce nitrogen gas at its top under low pressure. In this case, this nitrogen gas can also be expanded in an expansion valve to the vicinity of atmospheric pressure to produce cold, before being heated in 4 and then in 3 and then being recovered as a second product of the installation.

La simplicité de l'installation suivant l'invention rend celle-ci particulièrement intéressante pour la production de quantités modérées, par exemple de l'ordre de quelques dizaines de tonnes par jour, d'oxygène gazeux sous une pression de quelques bars.The simplicity of the installation according to the invention makes it particularly advantageous for the production of moderate quantities, for example of the order of a few tens of tonnes per day, of gaseous oxygen under a pressure of a few bars.

Dans la variante représentée à la Figure 2 sans son isolation thermique, la tenue en froid de l'installation s'effectue par détente libre du gaz résiduaire W en 15, complétée par un apport d'oxygène liquide provenant d'une source 19 constituée comme précédemment d'un stockage 19A à la pression atmosphérique et d'une pompe 19B.In the variant shown in Figure 2 without its thermal insulation, the cold resistance of the installation is effected by free expansion of the waste gas W at 15, supplemented by a supply of liquid oxygen coming from a source 19 constituted as previously from a storage 19A at atmospheric pressure and a pump 19B.

Toutefois, dans cette variante, l'oxygène liquide d'appoint, pompé en 19B à une pression quelque peu supérieure à la basse pression, est injecté, en un point intermédiaire 25 de la ligne d'échange thermique 3, dans l'oxygène gazeux en cours de réchauffement.However, in this variant, the additional liquid oxygen, pumped in 19B at a pressure somewhat higher than the low pressure, is injected, at an intermediate point 25 of the heat exchange line 3, in gaseous oxygen during heating.

De plus, une conduite 26 de purge d'oxygène liquide, munie d'une vanne 27, part de la cuve de la colonne 7 et débouche dans le stockage 19A pour l'alimenter en partie, le complément d'oxygène liquide étant apporté par des camions-citernes 28.In addition, a liquid oxygen purge pipe 26, fitted with a valve 27, leaves from the tank of the column 7 and opens into the storage 19A to supply it in part, the additional liquid oxygen being supplied by tankers 28.

La purge, destinée à évacuer les hydrocarbures de la colonne 7, correspond à environ 0,2% du débit d'air traité et s'effectue de préférence en discontinu, généralement automatiquement; elle est indépendante du "biberonnage" de l'installation par l'oxygène liquide.The purge, intended to evacuate the hydrocarbons from column 7, corresponds to approximately 0.2% of the flow of treated air and is preferably carried out batchwise, generally automatically; it is independent of the "bottle feeding" of the installation by liquid oxygen.

Le point d'injection 25 est choisi de manière que l'oxygène liquide se vaporise à une température suffisamment élevée pour que les hydrocarbures ne présentent plus de danger d'explosion ou d'inflammabilité lors de la vaporisation de l'oxygène. Cette température peut ainsi être de l'ordre de -100°C.The injection point 25 is chosen so that the liquid oxygen vaporizes at a sufficiently high temperature so that the hydrocarbons no longer present a danger of explosion or flammability during the vaporization of the oxygen. This temperature can thus be of the order of -100 ° C.

Claims (13)

1 - Procédé de production d'oxygène gazeux sous pression au moyen d'une double colonne de distillation (5), caractérisé en ce que : - on fait fonctionner la colonne basse pression (7) sous une pression nettement supérieure à la pression atmosphérique et légèrement supérieure à la pression de production d'oxygène, cette basse pression étant notamment de l'ordre de 2 à 5 bars, et on fait fonctionner la colonne moyenne pression (6) sous une pression correspondante, notamment de l'ordre de 8 à 16 bars; - on récupère directement l'oxygène gazeux de production en cuve de la colonne basse pression, et - on maintient en froid l'installation, au moins en partie, par détente libre d'au moins un produit gazeux sortant de la colonne basse pression. 1 - Process for the production of gaseous oxygen under pressure by means of a double distillation column (5), characterized in that: - the low pressure column (7) is operated under a pressure markedly higher than atmospheric pressure and slightly higher than the oxygen production pressure, this low pressure being in particular of the order of 2 to 5 bars, and operating the medium pressure column (6) under a corresponding pressure, in particular of the order of 8 to 16 bars; the production gaseous oxygen is directly recovered from the bottom of the low pressure column, and - The installation is kept cold, at least in part, by free expansion of at least one gaseous product leaving the low pressure column. 2 - Procédé suivant la revendication 1, caractérisé en ce qu'on détend par détente libre un gaz résiduaire (W) soutiré de la tête de la colonne basse pression (7). 2 - A method according to claim 1, characterized in that by free expansion a waste gas (W) withdrawn from the head of the low pressure column (7). 3 - Procédé suivant la revendication 1 ou 2, caractérisé en ce qu'on injecte (en 18) dans la colonne basse pression (7) un débit d'azote liquide provenant d'une source (17) extérieure à la double colonne (5). 3 - Process according to claim 1 or 2, characterized in that one injects (at 18) into the low pressure column (7) a flow of liquid nitrogen coming from a source (17) external to the double column (5 ). 4 - Procédé suivant l'une quelconque des revendications 1 à 3, caractérisé en ce qu'on injecte (en 20) dans la colonne basse pression (7) un débit d'oxygène liquide provenant d'une source (19) extérieure à la double colonne (5). 4 - Method according to any one of claims 1 to 3, characterized in that one injects (in 20) into the low pressure column (7) a flow of liquid oxygen coming from a source (19) external to the double column (5). 5 - Procédé suivant l'une quelconque des revendications 1 à 3, caractérisé en ce qu'on injecte dans l'oxygène gazeux (en 25), en un point intermédiaire de la ligne d'échange thermique (3) associée à la double colonne (5), un débit d'oxygène liquide provenant d'une source extérieure à la double colonne, et en ce qu'on envoie dans ladite source (19) de l'oxygène liquide de purge soutiré (en 26) de la cuve de la colonne basse pression (7). 5 - Method according to any one of claims 1 to 3, characterized in that one injects into the gaseous oxygen (at 25), at an intermediate point of the heat exchange line (3) associated with the double column (5), a flow of liquid oxygen from a source external to the double column, and in that one sends into said source (19) purge liquid oxygen withdrawn (at 26) from the tank of the low pressure column (7). 6 - Procédé suivant l'une quelconque des revendications 1 à 5, caractérisé en ce qu'on prérefroidit l'air à traiter, avant son épuration par adsorption (en 2), au moyen d'un groupe frigorifique (21). 6 - Process according to any one of claims 1 to 5, characterized in that the air to be treated is precooled, before its purification by adsorption (in 2), by means of a refrigeration unit (21). 7 - Installation de production d'oxygène gazeux sous pression, du type comprenant : un compresseur d'air (1); un appareil (2) d'épuration de l'air comprimé; une double colonne (5) de distillation de l'air épuré, comprenant elle-même une colonne moyenne pression (6) et une colonne basse pression (7) couplées par un vaporiseur-condenseur (8); une ligne d'échange thermique (3) pour refroidir l'air épuré par échange de chaleur indirect avec les produits provenant de la double colonne; et des moyens (15, 17-18, 19-20, 21) de maintien en froid de l'installation, caractérisée en ce que la colonne basse pression (7) fonctionne sous une pression nettement supérieure à la pression atmosphérique et légèrement supérieure à la pression de production d'oxygène, cette basse pression étant notamment de l'ordre de 2 à 5 bars, en ce qu'une conduite (13) de production d'oxygène est directement reliée à la cuve de la colonne basse pression pour en soutirer de l'oxygène gazeux, et en ce que les moyens de maintien en froid comprennent une vanne (15) de détente libre d'au moins un produit gazeux sortant de la colonne basse pression (7). 7 - Installation for producing gaseous oxygen under pressure, of the type comprising: an air compressor (1); an apparatus (2) for purifying compressed air; a double column (5) for the distillation of purified air, itself comprising a medium pressure column (6) and a low pressure column (7) coupled by a vaporizer-condenser (8); a heat exchange line (3) for cooling the purified air by indirect heat exchange with the products coming from the double column; and means (15, 17-18, 19-20, 21) for keeping the installation cold, characterized in that the low-pressure column (7) operates at a pressure markedly higher than atmospheric pressure and slightly higher than the oxygen production pressure, this low pressure being in particular of the order of 2 to 5 bars, in that an oxygen production pipe (13) is directly connected to the tank of the low pressure column in order to draw off gaseous oxygen, and in that the means for maintaining cold comprise a valve (15) for free expansion of at least one gaseous product leaving the low pressure column (7). 8 - Installation suivant la revendication 7, caractérisée en ce que la vanne de détente (15) est montée dans une conduite (14) d'évacuation de gaz résiduaire (W) partant de la tête de la colonne basse pression (7). 8 - Installation according to claim 7, characterized in that the expansion valve (15) is mounted in a pipe (14) for discharging residual gas (W) starting from the head of the low pressure column (7). 9 - Installation suivant la revendication 7 ou 8, caractérisée en ce que les moyens de maintien en froid comprennent une source (17) d'azote liquide sous la basse pression reliée à la tête de la colonne basse pression (7) pour y injecter un débit déterminé d'azote liquide. 9 - Installation according to claim 7 or 8, characterized in that the means for maintaining cold comprise a source (17) of liquid nitrogen under low pressure connected to the head of the low pressure column (7) for injecting a determined flow rate of liquid nitrogen. 10 - Installation suivant l'une quelconque des revendications 7 à 9, caractérisée en ce que les moyens de maintien en froid comprennent une source (19) d'oxygène liquide sous la basse pression reliée à la cuve de la colonne basse pression (7) pour y injecter un débit déterminé d'oxygène liquide. 10 - Installation according to any one of claims 7 to 9, characterized in that the means for keeping cold comprise a source (19) of liquid oxygen under low pressure connected to the tank of the low pressure column (7) to inject a determined flow of liquid oxygen into it. 11 - Installation suivant l'une quelconque des revendications 7 à 9, caractérisée en ce que les moyens de maintien en froid comprennent une source (19) d'oxygène liquide sous la basse pression reliée, en un point intermédiaire de la ligne d'échange thermique (3), aux passages de réchauffement d'oxygène gazeux, et en ce qu'une conduite de purge (26) relie la cuve de la colonne basse pression (7) à la source d'oxygène liquide (19). 11 - Installation according to any one of claims 7 to 9, characterized in that the means for keeping cold comprise a source (19) of liquid oxygen under the low pressure connected, at an intermediate point of the exchange line thermal (3), at the gaseous oxygen heating passages, and in that a purge line (26) connects the tank of the low pressure column (7) to the source of liquid oxygen (19). 12 - Installation suivant l'une quelconque des revendications 7 à 11, caractérisée en ce qu'elle comporte un groupe frigorifique (21) de prérefroidissement de l'air comprimé, monté entre le compresseur (1) et l'appareil d'épuration (2). 12 - Installation according to any one of claims 7 to 11, characterized in that it comprises a refrigeration unit (21) for precooling the compressed air, mounted between the compressor (1) and the purification device ( 2). 13 - Installation suivant l'une quelconque des revendications 7 à 12, caractérisée en ce que la double colonne (5) est isolée sous vide, notamment par une enveloppe sous vide (22) qui ne contient que la double colonne et des tronçons de conduite, le reste des parties froides de l'installation, à l'exception éventuellement des sources (17, 19) d'azote liquide et/ou d'oxygène liquide et des conduites (18, 20) qui en partent, étant isolées par une boîte froide (24) à la pression atmosphérique contenant un isolant solide, notamment particulaire. 13 - Installation according to any one of claims 7 to 12, characterized in that the double column (5) is vacuum insulated, in particular by a vacuum envelope (22) which contains only the double column and pipe sections , the rest of the cold parts of the installation, with the possible exception of the sources (17, 19) of liquid nitrogen and / or liquid oxygen and the pipes (18, 20) which leave therefrom, being isolated by a cold box (24) at atmospheric pressure containing a solid insulator, in particular a particulate.
EP93402665A 1992-12-30 1993-10-29 Process and apparatus for the production of gaseous oxygen under pressure Revoked EP0605262B1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9215925A FR2699992B1 (en) 1992-12-30 1992-12-30 Process and installation for producing gaseous oxygen under pressure.
FR9215925 1992-12-30

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EP0605262A1 true EP0605262A1 (en) 1994-07-06
EP0605262B1 EP0605262B1 (en) 2000-06-28

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US (1) US5408831A (en)
EP (1) EP0605262B1 (en)
JP (1) JPH06229668A (en)
CA (1) CA2112499A1 (en)
DE (1) DE69328922T2 (en)
FR (1) FR2699992B1 (en)

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DE19919587B4 (en) * 1998-04-30 2007-08-16 L'Air Liquide, S.A. pour l'Etude et l'Exploitation des Procédés Georges Claude Air distillation unit and cold box
EP1903290A4 (en) * 2005-06-23 2011-02-16 Air Water Inc Nitrogen generating device and apparatus for use therefor
WO2012004241A2 (en) 2010-07-05 2012-01-12 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Apparatus and process for the separation of air by cryogenic distillation
WO2013159868A3 (en) * 2012-04-27 2014-05-08 Linde Aktiengesellschaft Transportable package having a cold box, low-temperature air separation plant and method for producing a low-temperature air separation plant
WO2018114052A2 (en) 2016-12-23 2018-06-28 Linde Aktiengesellschaft Cryogenic air separation method, and air separation plant

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FR2972794B1 (en) 2011-03-18 2015-11-06 Air Liquide APPARATUS AND METHOD FOR AIR SEPARATION BY CRYOGENIC DISTILLATION
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WO2013159868A3 (en) * 2012-04-27 2014-05-08 Linde Aktiengesellschaft Transportable package having a cold box, low-temperature air separation plant and method for producing a low-temperature air separation plant
WO2018114052A2 (en) 2016-12-23 2018-06-28 Linde Aktiengesellschaft Cryogenic air separation method, and air separation plant

Also Published As

Publication number Publication date
US5408831A (en) 1995-04-25
JPH06229668A (en) 1994-08-19
FR2699992A1 (en) 1994-07-01
CA2112499A1 (en) 1994-07-01
DE69328922T2 (en) 2000-11-16
FR2699992B1 (en) 1995-02-10
DE69328922D1 (en) 2000-08-03
EP0605262B1 (en) 2000-06-28

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