EP4356052A1 - Procédé et installation permettant de fournir un produit à base d'air gazeux sous pression riche en oxygène - Google Patents

Procédé et installation permettant de fournir un produit à base d'air gazeux sous pression riche en oxygène

Info

Publication number
EP4356052A1
EP4356052A1 EP22729038.4A EP22729038A EP4356052A1 EP 4356052 A1 EP4356052 A1 EP 4356052A1 EP 22729038 A EP22729038 A EP 22729038A EP 4356052 A1 EP4356052 A1 EP 4356052A1
Authority
EP
European Patent Office
Prior art keywords
pressure
range
temperature
air
pressure range
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
EP22729038.4A
Other languages
German (de)
English (en)
Other versions
EP4356052B1 (fr
EP4356052C0 (fr
Inventor
Dimitri GOLUBEV
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP4356052A1 publication Critical patent/EP4356052A1/fr
Application granted granted Critical
Publication of EP4356052B1 publication Critical patent/EP4356052B1/fr
Publication of EP4356052C0 publication Critical patent/EP4356052C0/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

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
    • F25J3/04375—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
    • F25J3/04006—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
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—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
    • F25J3/04406—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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/04—Multiple expansion turbines in parallel
    • 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
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J2240/46—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 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F25J2270/06—Internal refrigeration with work-producing gas expansion loop with multiple gas expansion loops
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/12—Particular process parameters like pressure, temperature, ratios
    • 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
    • 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms

Definitions

  • the invention relates to a method for providing a pressurized, oxygen-rich, gaseous air product and a corresponding system according to the preambles of the independent patent claims.
  • air product is intended to refer to a fluid provided at least in part by the cryogenic decomposition of atmospheric air.
  • An air product according to the understanding on which this is based has one or more air gases contained in the atmospheric air in a different composition than in the atmospheric air.
  • an air product can exist or be provided in a gaseous, liquid or supercritical state and can be converted from one of these states of aggregation to another.
  • a liquid air product can be vaporized ("vaporized”) or supercritical (“pseudo-vaporized”) by heating to a certain pressure, depending on whether the pressure at the time of heating is below or above the critical pressure . If “vaporization” is mentioned below, this should also include a corresponding pseudo-vaporization.
  • Air separation plants have rectification column systems which are conventionally designed as two-column systems, in particular as classic Linde double-column systems, but can also be designed as three- or multi-column systems.
  • rectification columns for the production of nitrogen and/or oxygen in liquid and/or gaseous form
  • rectification columns can be provided to obtain other air components, in particular the noble gases krypton, xenon and / or argon.
  • the terms “rectification” and “distillation” and “column” and “column” or terms composed of these are used synonymously.
  • the rectification columns of the rectification column systems mentioned are operated at different pressures.
  • Known double column systems have a so-called high-pressure column (also referred to as a pressure column, medium-pressure column or lower column) and a so-called low-pressure column (also referred to as an upper column).
  • the high-pressure column is typically operated at a pressure of 4 to 7 bar, in particular about 5.3 bar.
  • the low-pressure column is operated at a pressure of typically 1 to 2 bar, in particular about 1.4 bar. In certain cases, higher pressures can also be used in both rectification columns.
  • the pressures given here in each case are absolute pressures at the top of the columns given in each case.
  • So-called main (air) compressor/boost compressor main air compressor/booster air compressor, MAC-BAC) method or so-called high air pressure (HAP) method can be used for air separation.
  • main compressor/boost processes are the more conventional processes
  • high air pressure processes have been increasingly used in recent times as alternatives to the main compressor/boost processes.
  • the present invention is used in connection with high-air pressure processes, so that the following explanations in this regard apply generally and also to the present invention. Due to the significantly lower costs - the main and booster compressors are, to a certain extent, integrated in one machine - and basically comparable efficiency, high-air pressure processes can represent an advantageous alternative to the main compressor/boost process.
  • Main compressor/post-compressor processes are characterized in that only part of the total amount of feed air fed to the rectification column system is compressed to a pressure which is significantly, ie by at least 3, 4, 5, 6, 7, 8, 9 or 10 bar above of the pressure at which the high-pressure column is operated. Another part of the amount of air used is only on this pressure or one Pressure, which differs from this by no more than 1 to 2 bar, is compressed and fed into the high-pressure column at this lower pressure, in particular without additional relaxation.
  • a main compressor/post-compressor process is shown, for example, by Häring (see above) in FIG. 2.3A.
  • a high-air pressure process on the other hand, the entire amount of feed air fed to the rectification column system is compressed to a pressure that is significantly, i.e. by at least 3, 4, 5, 6, 7, 8, 9 or 10 bar, and for example up to 14, 16 , 18 or 20 bar, is above the pressure at which the high-pressure column is operated.
  • High-air pressure processes are known, for example, from EP 2 980514 A1 and EP 2 963367 A1.
  • High-air pressure processes are typically used with so-called internal compression (IV, Internal Compression, IC).
  • internal compression at least one gaseous, pressurized air product, which is provided by the air separation plant, is formed by taking a cryogenic, liquid air product from the rectification column system, subjecting it to a pressure increase to a product pressure, and subjecting it to the product pressure by heating it to the gaseous or supercritical state is transferred.
  • gaseous pressurized nitrogen (GAN IV, GAN IC) and/or gaseous pressurized argon (GAR IV, GAR IC) can be produced by internal compression.
  • Internal compression offers a number of advantages over external compression, which is also possible as an alternative, and is explained, for example, by Häring (see above) in Section 2.2.5.2, "Internal Compression".
  • High-air pressure methods can be used in different configurations. These are often classified and differentiated according to the liquid performance of the plant, ie according to the quantity of air products provided in liquid form and removed from the plant in liquid form, or according to the ratio of internally compressed air products to liquid products. If the liquid output is not too high, a cold booster or cold compressor of the type explained below is used in high-air pressure processes, for example, in order to increase the efficiency of the process by converting the then excess refrigeration output into higher air pressure. Also known are high-air pressure processes with a so-called Lachmann or Einblaseturbine (English also Upper Column Expander) of the type also explained below. The expanded air in the Lachmann turbine is fed into the low-pressure column.
  • the Lachmann turbine can be provided as a further turbine unit in addition to a turbine unit, by means of which gaseous compressed air is expanded into the high-pressure column, ie a so-called Claude turbine.
  • the object of the invention is to increase the efficiency and competitiveness of high-air pressure processes, in particular for such typical gas systems.
  • the present invention proposes a method for providing one or more oxygen-rich, gaseous air products and a corresponding system with the respective features of the independent patent claims.
  • Refinements of the invention are the subject of the respective dependent patent claims and the following description.
  • an “amount of feed air” or “feed air” for short is understood here to mean the entire air fed (“used”) to the rectification column system of an air separation plant.
  • a main compressor/post-compressor process only part of this amount of feed air is compressed to a pressure in a range that is significantly above a pressure range in which the high-pressure column is operated.
  • a high-air pressure process as is the subject of the present invention, the entire amount of feed air is compressed to a pressure in such a high pressure range.
  • cryogenic liquid is understood here to mean a liquid medium whose boiling point is well below ambient temperature, for example at -50° C. or less, in particular at -100° C. or less.
  • cryogenic liquids are liquid air, liquid oxygen, liquid nitrogen, liquid argon or liquids that are rich in the compounds mentioned.
  • turbo compressors In air separation plants, multi-stage turbo compressors are used to compress the input air, which are referred to here as "main air compressors".
  • the mechanical structure of turbo compressors is known in principle to those skilled in the art.
  • the medium to be compressed is compressed by means of turbine blades, which are arranged on a turbine wheel or directly on a shaft.
  • a turbo compressor forms a structural unit which, however, can have several compressor stages in the case of a multi-stage turbo compressor.
  • a compressor stage generally includes a turbine wheel or a corresponding arrangement of turbine blades. All of these airends can be driven by a common shaft. However, it can also be provided that the compressor stages are driven in groups with different shafts, in which case the shafts can also be connected to one another via gears.
  • the main air compressor is also characterized in that it compresses the entire amount of air fed into the distillation column system and used for the production of air products, ie the entire amount of feed air.
  • a "post-compressor" can also be provided, in which, however, only part of the input air quantity compressed in the main air compressor is brought to an even higher pressure.
  • This can also be designed as a turbo compressor. Additional turbo compressors are typically provided for compressing partial amounts of air, which are also referred to as boosters, but compared to the main air compressor or the secondary compressor, typically only compression to a relatively small extent, in particular in relation to the compressed one air volume.
  • a booster can also be present in a high-air pressure process, but this then compresses a subset of the input air quantity, starting from a higher pressure.
  • a “cold compressor” or “cold booster” is to be understood here as a compressor or booster, the fluid at a temperature in a temperature range well below the ambient temperature of the air separation plant, in particular at a temperature of less than 0 °C, -50 °C or -100°C and in particular more than -150°C or -200°C.
  • Air can also be expanded at several points in air separation plants, for which purpose, among other things, expansion machines in the form of turboexpanders, also referred to here as “expansion turbines”, can be used.
  • Turboexpanders can also be coupled to and drive turbocompressors. If one or more turbo compressors are driven without externally supplied energy, i.e. only via one or more turbo expanders, the term “turbine booster” is also used for such an arrangement.
  • the turboexpander (the expansion turbine) and the turbocompressor (the booster) are mechanically coupled, with the coupling being able to take place at the same speed (e.g. via a common shaft) or at different speeds (e.g. via an intermediate gearbox).
  • a “turbine unit” is mentioned here, this should be understood to mean in particular an arrangement with at least one expansion turbine.
  • a "throttle flow” or “Joule-Thomson flow” is understood to mean an amount of air which, at least for the most part, is liquefied under pressure in the main heat exchanger of an air separation plant and is then fed, in particular via a throttle valve, in particular into the high-pressure column.
  • a Joule-Thomson turbine can also be used instead of a throttle valve.
  • Liquid, gaseous or fluids in the supercritical state can be rich or poor in one or more components in the language used here, with “rich” for a content of at least 75%, 90%, 95%, 99%, 99.5% , 99.9% or 99.99% and “poor” can stand for a content of at most 25%, 10%, 5%, 1%, 0.1% or 0.01% on a mole, weight or volume basis .
  • the term “predominantly” may correspond to the definition of "rich” just given, but in particular denotes a content of more than 90%. If, for example, “nitrogen” or “oxygen” is mentioned here, it can be a pure gas, but it can also be a gas rich in nitrogen or oxygen.
  • pressures and temperatures in specific pressure and temperature ranges are discussed for the characterization of pressures and temperatures. This is intended to express the fact that pressures and temperatures do not have to be used in the form of exact pressure or temperature values in order to implement an inventive concept. However, such pressures and temperatures typically range within respective ranges, for example, ⁇ 1%, 5%, or 10% about an average. Different pressure or temperature ranges can represent disjunctive ranges or ranges that overlap one another. In particular, for example, the specification of pressure ranges includes unavoidable or expected pressure losses, for example due to line resistances and the like. The same applies to pressure areas. Unless otherwise stated, the pressures or pressure range limits given here in bar are absolute pressures.
  • liquid performance denotes the quantity of air products that are discharged from the plant or a corresponding process in liquid form, i.e. in which there is no evaporation or pseudo-evaporation.
  • Such products cannot therefore be used to cool feed streams into the plant or the process by means of a corresponding evaporation. Therefore, if smaller amounts of air products are carried out in liquid form from the plant or a corresponding process, but these are evaporated or pseudo-evaporated, there is, so to speak, an excess of cold.
  • a so-called cold booster can therefore be used, for example, in order to increase the process efficiency by converting such excess cold into higher air pressure.
  • the heat input from the cold booster "destroys" some of the excess cold, but in return the cold booster compresses part of the input air, so that, for example, the power of the main air compressor can be reduced accordingly.
  • the intake temperature of a cold booster is below the ambient temperature, so that the power consumption is reduced if the gas behavior is assumed to be ideal for the sake of simplicity.
  • the invention is used in a high-air pressure process in which, as mentioned, gaseous oxygen is to be produced without (significant) liquid production, and in which an injection turbine (Lachmann turbine) is used as a second turbine unit in addition to a first turbine unit, which, according to Art a Claude turbine air relaxed in the high-pressure column, is provided.
  • an injection turbine Loachmann turbine
  • the present invention solves the above problem in particular in that air is supplied to the Lachmann turbine at a significantly lower air inlet temperature than in known methods. This results in strong pre-liquefaction at the turbine outlet of the Lachmann turbine. Accordingly, there is a significant reduction in the air quantities to be liquefied in the main heat exchanger as throttle flow or throttle flows and, as a consequence, there is a noticeable increase in efficiency. The amount of heat to be transferred in the lower area of the main heat exchanger, i.e. at the point where the condensation of air flows takes place, is therefore lower and the performance of the cold compressor is reduced.
  • the present invention proposes a method for producing a pressurized, oxygen-rich, gaseous air product using an air separation plant which has a rectification column system with a high-pressure column and a low-pressure column and a main heat exchanger, a first turbine unit and a second turbine unit.
  • the high-pressure column is operated in a first pressure range of 4 to 7 bar, in particular approx. 5.3 bar, the low-pressure column is operated in a second pressure range of 1 to 2 bar, in particular approx. 1.4 bar, and at least one predominant A proportion of the total amount of feed air fed to the rectification column system, in particular the total amount of feed air as is customary in a high-air pressure process, is compressed to a pressure in a third pressure range which is more than 3 bar above the first pressure range.
  • a third pressure range which is more than 3 bar above the first pressure range.
  • a first portion of the feed air quantity compressed to the pressure in the third pressure range is supplied at the pressure in the third pressure range or at a pressure in a fourth pressure range above the third pressure range and at a temperature in a first temperature range to the first turbine unit using the first Turbine unit relaxed to a pressure in the first pressure range, and fed into the high-pressure column.
  • the main heat exchanger of the air separation plant in particular is used in the manner explained below to provide the first subset at the temperature in the first temperature range, and the pressure in the fourth pressure range is optionally achieved using a corresponding booster unit in the manner explained below .
  • the first turbine unit is in particular a typical Claude turbine as explained above, or the first turbine unit includes one.
  • a second partial amount of the feed air amount compressed to the pressure in the third pressure range is at the pressure in the third pressure range or at a pressure in a fifth pressure range above the third pressure range and at a Temperature in a second temperature range of the second turbine unit fed, expanded using the second turbine unit to a pressure in the second pressure range, and fed into the low pressure column.
  • the main heat exchanger of the air separation plant in particular is used in the manner explained below to provide the second subset at the temperature in the second temperature range, and the pressure in the fifth pressure range is optionally achieved using a corresponding booster unit in the manner explained below .
  • the second turbine unit is, in particular, a typical Lachmann turbine as explained above, or the second turbine unit includes one.
  • the invention comprises removing oxygen-rich liquid from the rectification column system to provide the gaseous, pressurized, oxygen-rich air product, in the liquid state with heating to a temperature in a third temperature range in the liquid state to a pressure in a sixth pressure range of 16 to 50 bar or 25 to 50 bar, in particular 40 to 50 bar, for example approx. 43 bar, is fed to the main heat exchanger, evaporated in this at the temperature in the third temperature range and discharged from the air separation plant.
  • the pressurized, oxygen-rich air product is thus provided as an internal compression product.
  • the third temperature range i.e. the temperature range in which the temperature lies at which the oxygen-rich liquid is vaporized in the main heat exchanger after pressurization in the liquid state, is according to the invention both above the first temperature range and above the second temperature range.
  • the second temperature range is selected in such a way that a two-phase mixture with a liquid fraction of 5 to 15%, in particular 8 to 13%, forms at the outlet of the second turbine unit, with these percentages in particular representing a mole fraction of the liquid fraction, based on an amount of substance of the entire two-phase mixture.
  • the temperature in the first temperature range and the temperature in the second temperature range do not differ from one another by more than 10 K.
  • the air separation plant is operated in such a way that a proportion of less than 5%, in particular less than 2%, of all air products removed from the air separation plant are removed from the air separation plant in non-evaporated and liquid state.
  • air product which not only includes essentially pure products such as oxygen or nitrogen, but also impure streams (so-called waste gas), reference is made to the above explanations.
  • the proportion is less than 10%, in particular less than 5% or less than 2%.
  • the "substantially pure" products include in particular nitrogen, oxygen and argon, or fluids each rich in the respective component mentioned.
  • the first and the second temperature range are each 110 to 140 K, in particular 120 to 135 K.
  • the third temperature range is in particular more than 10 K and up to 40 K above the first temperature range and the second temperature range.
  • the first subset of the feed air quantity compressed to the pressure in the third pressure range is advantageously provided at the pressure in the fourth pressure range and brought to the pressure in the fourth pressure range using a booster unit.
  • the booster unit used here can be used in particular to drive the first turbine unit.
  • the first partial quantity of the feed air quantity compressed to the pressure in the third pressure range can be in a first Cooling step in the main heat exchanger before it is brought to the pressure in the fourth pressure range using the booster unit, and the first subset of the feed air quantity compressed to the pressure in the third pressure range can be cooled in a second cooling step in the main heat exchanger after it was brought to the pressure in the fourth pressure range using the booster unit, wherein the second cooling step comprises cooling to the already mentioned temperature in the first temperature range.
  • a third partial quantity of the feed air quantity compressed to the pressure in the third pressure range can be subjected to the first cooling step, in particular together with the first partial quantity of the feed air quantity compressed to the pressure in the third pressure range, and brought to the pressure in the fourth pressure range using the booster unit, wherein the third subset of the feed air quantity further compressed to the pressure in the third pressure range and then to the pressure in the fourth pressure range is liquefied at the pressure in the fourth pressure range in the main heat exchanger, then expanded, and fed into the high-pressure column.
  • the first subset is taken from the main heat exchanger in particular at an extraction point corresponding to the temperature in the first temperature range, whereas the third subset is routed through the main heat exchanger to the cold end. In this way, the third subset forms a choke flow.
  • the second subset of the feed air quantity compressed to the pressure in the third pressure range can be provided in particular at the pressure in the fifth pressure range and brought to the pressure in the fourth pressure range using a further booster unit.
  • the further booster unit can in particular drive the second turbine unit, which is therefore designed to be “self-boosted”.
  • the second turbine unit can in particular be designed with oil or generator braking, as is known per se.
  • a fourth partial quantity of the feed air quantity compressed to the pressure in the third pressure range can be cooled in the main heat exchanger together with the second partial quantity of the feed air quantity compressed to the pressure in the third pressure range, the second partial quantity being at one of the temperatures in the second temperature range corresponding point can be carried out from the main heat exchanger, but the fourth subset can be further cooled and liquefied.
  • the fourth subset can be taken from the cold side of the main heat exchanger and fed into the high-pressure column as a further throttle flow.
  • the two-phase mixture which forms at the outlet of the second turbine unit is advantageously fed to a phase separation in a suitable phase separator and then fed into the low-pressure column in separate phases, i.e. in the form of a gas stream and a liquid stream.
  • the two-phase mixture forming at the outlet of the second turbine unit is fed into the low-pressure column in two phases.
  • a pump can be dispensed with, as liquid droplets are entrained due to the relatively high flow rate.
  • the present invention further relates to an air separation plant for providing a pressurized oxygen-rich gaseous air product.
  • an air separation plant for providing a pressurized oxygen-rich gaseous air product.
  • FIGS 1 to 5 illustrate air separation plants according to preferred embodiments of the invention.
  • FIGS 6 and 7 show temperature-enthalpy diagrams.
  • FIG. 1 shows an air separation plant, designated 100, according to a preferred embodiment of the invention.
  • the air separation plant 100 has a rectification column system 10 with a high-pressure column 11 and a low-pressure column 12, which are connected in a known manner.
  • Air separation plants of the type shown are often described elsewhere, for example by Häring (see above) and there in particular in Section 2.2.5, "Cryogenic Rectification".
  • An air separation plant for the use of the present invention can be designed in the most varied of ways.
  • the high-pressure column 11 is operated in a first pressure range
  • the low-pressure column 12 is operated in a second pressure range
  • at least a predominant proportion of a total amount of feed air fed to the rectification column system 10, here in the form of a compressed air stream a is pressurized to a pressure in a third pressure range compressed, which is significantly above the first pressure range.
  • feed air is sucked in by means of a main air compressor 1, compressed to the pressure in the third pressure range, cooled in a direct contact cooler, also not designated separately, and freed of water and carbon dioxide in particular in a pre-cleaning unit 2.
  • the feed air provided in this way as the mentioned compressed air stream a at the pressure in the third pressure region is then divided into two partial streams b and c divided, both of which are fed to a main heat exchanger 3 on the hot side and cooled therein. It will be by picking up
  • Intermediate temperature levels and the cold side of the main heat exchanger 3 each formed further substreams, which represent subsets of the feed air of the compressed air flow a, referred to here as “first" to “fourth” subsets, and are indicated with a1 to a4.
  • the first partial quantity of the total input air quantity of compressed air flow a compressed to the pressure in the third pressure range is at a pressure in a fourth pressure range above the third pressure range and at a temperature in a first temperature range in the form of partial flow a1 of a first Supplied to turbine unit 5, expanded to a pressure in the first pressure range using the first turbine unit 5, and fed into the high-pressure column 11.
  • the first partial quantity i.e. the partial flow a1 is brought to the pressure in the fourth pressure range as part of the partial flow b using a booster unit 4, the booster unit 4 being driven by that of the first turbine unit 5.
  • the first partial quantity, i.e. the partial flow a1 is cooled in the main heat exchanger 3 in a first cooling step before it is brought to the pressure in the fourth pressure range using the booster unit 4, and the first partial quantity, i.e. the material flow a1 is cooled in a second cooling step in the main heat exchanger 3 after being pressurized in the fourth pressure range using the booster unit 4 .
  • the second cooling step includes cooling to the temperature in the mentioned first temperature range.
  • the second partial quantity of the feed air quantity of compressed air flow a compressed to the pressure in the third pressure range is, on the other hand, part of partial flow c at the pressure in the third pressure range and at a temperature in a second temperature range in the form of partial flow a2 of a second Supplied to the turbine unit 6, which is coupled to a generator G in the embodiment illustrated here, expanded to a pressure in the second pressure range using the second turbine unit 6, and then fed into the low-pressure column 12.
  • the second temperature range is selected in such a way that a two-phase mixture forms at the outlet of the second turbine unit 6 with the liquid fraction specified several times above.
  • the two-phase mixture forming at the outlet of the second turbine unit 6 is fed to a phase separation in a phase separator 7 and then fed into the low-pressure column 12 in separate phases in the form of a liquid stream a2l and a gas stream a2g.
  • the third partial quantity of the feed air quantity of the compressed air flow a compressed to the pressure in the third pressure range is subjected to the first cooling step in the form of the mentioned partial flow a3 together with the first partial quantity, i.e. the partial flow a1 and thus as part of the partial flow b, and is also used the booster unit 4 to the pressure in the fourth pressure range, with the third subset, i.e. the partial flow a3, but liquefied at the pressure in the fourth pressure range in the main heat exchanger 3, expanded, and fed into the high-pressure column 11.
  • the fourth partial quantity of the feed air quantity of the compressed air flow a compressed to the pressure in the third pressure range is fed in the form of the mentioned partial flow a4 together with the second partial quantity, i.e. the partial flow a2, and thus as part of the partial flow c, to the main heat exchanger 3, but not on taken from the temperature in the second temperature range, but also liquefied in the main heat exchanger, then expanded and fed into the high-pressure column 11 .
  • the partial streams a3 and a4 used as throttle streams are combined to form a total stream k before they are fed into the high-pressure column 11 .
  • oxygen-rich liquid is removed from the rectification column system 10, more precisely a bottom of the low-pressure column 11, in the form of a stream I, in the liquid state with heating to a temperature in a third temperature range by means of an internal compression pump 8 to a pressure in brought to a sixth pressure range, at the temperature in the third temperature range evaporated in the main heat exchanger 3 and discharged from the air separation unit 100.
  • the air separation plant 200 according to FIG. 2 differs from the air separation plant 100 according to FIG.
  • the air separation plant 300 according to Figure 3 differs from the air separation plants 100 and 200 according to Figures 1 and 2 essentially by the provision of the pressurized, oxygen-rich air product in the form of two fractions or partial flows 11 and I2, which are formed from the partial flow I and in the main heat exchanger 3 are vaporized at different pressures.
  • the air separation plant 400 according to FIG. 4 differs from the air separation plants 100 to 300 according to FIGS fifth pressure range is provided and is brought to the pressure in the fifth pressure range using a further booster unit 41, which is driven in particular by the turbine 6 (that is to say is “self-boosted”).
  • the further booster unit 41 is formed by a warm booster for air, i.e. by a booster with an inlet temperature above 273 K.
  • the air separation plant 500 according to FIG. 5 differs from the air separation plants 100 to 400 according to FIGS. 1 to 4 essentially in that an argon discharge column 51 of a known type is used, as described for example in EP 3067649 A1. From the argon discharge column 51, an argon-enriched, gaseous stream s withdrawn and heated in the main heat exchanger 3. The argon discharge column 51 is fed from the low-pressure column 12 and bottom liquid (in each case without a separate designation) is returned to the low-pressure column 12 after it has been depleted of argon. To cool a top condenser of the argon discharge column 51, bottom liquid from the high-pressure column 11 is used, which is fed into the low-pressure column 12 after partial evaporation
  • argon discharge column is used here to refer to a separating column for argon-oxygen separation which is not used to obtain a pure argon product but to discharge argon from the air to be separated in the pressure column and low-pressure column. Its circuit differs only slightly from that of a classic crude argon column, although it contains significantly fewer theoretical plates, namely less than 40, in particular between 35 and 15. Like a crude argon column, the bottom area of an argon discharge column is connected to an intermediate point of the low-pressure column and the argon discharge column is a top condenser is cooled, on the evaporation side of which expanded bottom liquid from the high-pressure column is introduced; an argon discharge column does not have a bottom evaporator.
  • FIGs 6 and 7 are temperature-enthalpy diagrams of the main heat exchanger 3 of an air separation plant according to an embodiment of the invention, for example an air separation plant 100 to 500 according to Figures 1 to 5, with a temperature on the vertical axis in K compared to an enthalpy sum in kW are plotted on the horizontal axis and the diagram according to FIG. 7 corresponds to an enlarged representation of the diagram according to FIG.
  • the temperature points Ta1 and Ta2 each correspond to the extraction temperature levels of the partial flows a1 and a2.
  • the air separation plants according to FIGS. 1 to 5 can, of course, also be adapted to obtain low-pressure nitrogen product (LPGAN) as a by-product of air separation. This can be done by using a corresponding separating section in the low-pressure column 12 .
  • LPGAN low-pressure nitrogen product

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Oxygen, Ozone, And Oxides In General (AREA)

Abstract

L'invention concerne un procédé à pression atmosphérique élevée pour la production d'un produit à base d'air gazeux sous pression riche en oxygène. Une première quantité partielle de la quantité d'air d'alimentation est fournie à une température dans une première plage de températures jusqu'à une première unité de turbine (5), décomprimée au moyen de celle-ci, et introduite dans une colonne à haute pression (111). Une seconde quantité partielle de la quantité d'air d'alimentation est fournie à une température dans une deuxième plage de températures jusqu'à une seconde unité de turbine (6), décomprimée au moyen de celle-ci, et introduite dans une colonne à basse pression (12). Le produit à base d'air sous pression riche en oxygène est fourni sous la forme d'un produit de compression interne à 16 à 50 bars, l'évaporation étant effectuée à partir d'une température dans une troisième plage de températures. La troisième plage de températures se situe au-dessus des première et deuxième plages de températures, la deuxième plage de températures étant sélectionnée de sorte qu'un mélange à deux phases avec une proportion liquide de 5 à 15 % se forme au niveau de la sortie de la seconde unité de turbine (6), la température dans la première plage de températures et la température dans la deuxième étant différentes l'une de l'autre de pas plus de 10 K, et une partie inférieure à 5 % de tous les produits d'air éliminés de l'installation de séparation d'air (100) est éliminée de l'installation de séparation d'air dans un état non évaporé et liquide. La première unité de turbine est freinée par un compresseur froid (4), la seconde par un générateur (G) ou un surpresseur chaud. L'invention se rapporte également à une installation de séparation d'air (100).
EP22729038.4A 2021-06-17 2022-05-17 Procédé et installation de fourniture d'un produit gazeux dérivé de l'air, sous pression et riche en oxygène Active EP4356052B1 (fr)

Applications Claiming Priority (2)

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EP21020325 2021-06-17
PCT/EP2022/025230 WO2022263013A1 (fr) 2021-06-17 2022-05-17 Procédé et installation permettant de fournir un produit à base d'air gazeux sous pression riche en oxygène

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EP4356052A1 true EP4356052A1 (fr) 2024-04-24
EP4356052B1 EP4356052B1 (fr) 2025-08-06
EP4356052C0 EP4356052C0 (fr) 2025-08-06

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US (1) US20240384928A1 (fr)
EP (1) EP4356052B1 (fr)
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Publication number Priority date Publication date Assignee Title
JP3306516B2 (ja) * 1992-02-14 2002-07-24 日本酸素株式会社 空気液化分離装置用精留塔
FR2895068B1 (fr) * 2005-12-15 2014-01-31 Air Liquide Procede de separation d'air par distillation cryogenique
EP2634517B1 (fr) * 2012-02-29 2018-04-04 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé et appareil pour la séparation d'air par distillation cryogénique
US20130255313A1 (en) * 2012-03-29 2013-10-03 Bao Ha Process for the separation of air by cryogenic distillation
EP2963367A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procédé et dispositif cryogéniques de séparation d'air avec consommation d'énergie variable
EP2980514A1 (fr) 2014-07-31 2016-02-03 Linde Aktiengesellschaft Procédé de séparation cryogénique de l'air et installation de séparation d'air
EP3067649A1 (fr) 2015-03-13 2016-09-14 Linde Aktiengesellschaft Système de colonnes de distillation et procédé de production d'oxygène par séparation cryogénique de l'air
EP3133361B1 (fr) * 2015-08-20 2018-06-13 Linde Aktiengesellschaft Systeme de colonnes de distillation et installation de production d'oxygene par separation cryogenique de l'air
EP3394536A1 (fr) * 2015-12-23 2018-10-31 Linde Aktiengesellschaft Procédé et dispositif de production d'azote pur et d'oxygène pur par séparation cryogénique d'air
EP3696486A1 (fr) * 2019-02-13 2020-08-19 Linde GmbH Procédé et installation de fourniture d'un ou d'une pluralité de produits dérivés de l'air gazeux, riches en oxygène

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CN117501057A (zh) 2024-02-02
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US20240384928A1 (en) 2024-11-21
TW202300843A (zh) 2023-01-01
EP4356052C0 (fr) 2025-08-06

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