EP4464962A2 - Procédé de production d'oxygène de très haute pureté et appareil de production d'oxygène de très haute pureté - Google Patents

Procédé de production d'oxygène de très haute pureté et appareil de production d'oxygène de très haute pureté Download PDF

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Publication number
EP4464962A2
EP4464962A2 EP24171695.0A EP24171695A EP4464962A2 EP 4464962 A2 EP4464962 A2 EP 4464962A2 EP 24171695 A EP24171695 A EP 24171695A EP 4464962 A2 EP4464962 A2 EP 4464962A2
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EP
European Patent Office
Prior art keywords
oxygen
rectification column
nitrogen
heat exchanger
feed
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.)
Pending
Application number
EP24171695.0A
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German (de)
English (en)
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EP4464962A3 (fr
Inventor
Kenji Hirose
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.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Publication date
Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP4464962A2 publication Critical patent/EP4464962A2/fr
Publication of EP4464962A3 publication Critical patent/EP4464962A3/fr
Pending legal-status Critical Current

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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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/0403—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of 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
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    • 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
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    • F25J3/04036—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of oxygen
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    • 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
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    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04363—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of oxygen
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    • 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
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
    • 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
    • F25J2205/86—Processes or apparatus using other separation and/or other processing means using electrical phenomena, e.g. Corona discharge, electrolysis or magnetic field
    • 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
    • F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of 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
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
    • 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
    • F25J2215/56—Ultra high purity oxygen, i.e. generally more than 99,9% 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/50—Separating low boiling, i.e. more volatile components from oxygen, e.g. N2, Ar
    • 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
    • F25J2240/12—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream 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
    • 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
    • F25J2240/20—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/10—Boiler-condenser with superposed stages
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/14—External refrigeration with work-producing gas expansion loop
    • 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
    • F25J2270/50—Quasi-closed internal or closed external oxygen refrigeration cycle
    • 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
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop

Definitions

  • the present invention relates to an ultra-high-purity oxygen production method and an ultra-high-purity oxygen production apparatus.
  • the present invention relates to the production of ultra-high-purity oxygen in which the impurity concentration is controlled to no greater than the ppb level.
  • a method employing a catalyst in conjunction with an adsorbent, and cryogenic separation in which oxygen is liquefied and separated by means of a rectification operation are known as methods for removing the impurities, but adsorption processes and removal by molecular sieve are especially difficult for argon impurities because argon is chemically inert and its molecules are very close in size to oxygen molecules, thus cryogenic separation is suitable.
  • Known methods for obtaining ultra-high-purity oxygen include a method in which liquefied oxygen supplied from an air separation unit ( JP 3929799 ) or oxygen gas ( JP 2021-55890 A ) is rectified, or a method in which an oxygen-containing liquid from which the high-boiling-point components have been removed is drawn from a rectification column for rectifying air, and argon is removed by an oxygen rectification column.
  • US 5049173 A describes a method for producing ultra-high-purity oxygen in a double-column rectification system
  • WO 2014/173496 A2 describes a method for producing ultra-high-purity oxygen in a single-column nitrogen rectification system.
  • by-product oxygen from generating hydrogen by electrolysis of water is sometimes used as a feed material for the production of ultra-high-purity oxygen.
  • the oxygen derived from water electrolysis does not contain high-boiling-point components derived from the atmosphere such as methane, but it does contain a certain amount of low-boiling-point components dissolved in the water.
  • Low-boiling-point impurities in the water may be reduced by means of bubbling, etc. which utilizes nitrogen gas or oxygen gas, but it would be desirable to control the process by means of cryogenic separation from the point of view of stably removing impurities to a high level.
  • CN114017993A describes a process for liquefying oxygen in the main heat exchanger of an air separation unit.
  • WO2023274574 relates to a process in which oxygen from an electrolyser is sent to an air separation unit without being mixed with any fluid from that unit.
  • Figure 2 shows an oxygen purification column, fed with a stream from an air separation column and a stream from an electrolyser.
  • the present disclosure provides an ultra-high-purity oxygen production method and an ultra-high-purity oxygen production apparatus that enable ultra-high-purity oxygen to be obtained at a low cost by removing low-boiling-point components from by-product oxygen obtained for example from water electrolysis.
  • an ultra-high-purity oxygen production method utilizing an air separation unit comprising a main heat exchanger, a nitrogen rectification column, a nitrogen condenser, an oxygen rectification column, and an oxygen vaporizer, wherein the method comprises:
  • the method further comprises:
  • an ultra-high-purity oxygen production apparatus comprising: a main heat exchanger into which feed air and feed oxygen are introduced;
  • the apparatus comprises:
  • an ultra-high-purity oxygen production apparatus comprising: a main heat exchanger into which feed air and feed oxygen are introduced;
  • the apparatus may comprise: expansion means - for expanding at least part of the feed oxygen following cooling in the main heat exchanger to provide refrigeration for the apparatus.
  • the oxygen rectification column may be connected so as to be fed only by the feed oxygen.
  • the oxygen rectification column is connected so as to be fed only by feed oxygen coming from an electrolyser.
  • the apparatus may comprises an integrated apparatus including an electrolyser, means for sending water to the electrolyser, means for removing hydrogen from the electrolyser, means for removing an oxygen rich stream from the electrolyser, an ultra high purity oxygen production apparatus as described above and means for sending the oxygen rich stream from the electrolyser as the feed oxygen.
  • the ultra-high-purity oxygen production method according to the present disclosure may be applied in an air separation unit comprising: a main heat exchanger, a nitrogen rectification column (first (medium-pressure) rectification column), a nitrogen condenser, an oxygen rectification column, and an oxygen vaporizer.
  • the ultra-high-purity oxygen production method comprises a step in which feed oxygen comprising low-boiling-point components (e.g., nitrogen and argon) as impurities is introduced from a warm end of the main heat exchanger (1) and cooled, then introduced into the oxygen rectification column (5), and product ultra-high-purity oxygen from which the low-boiling-point components have been removed is drawn as a gas or a liquid from a lower portion of the oxygen rectification column (5) or from the oxygen vaporizer (6).
  • feed oxygen comprising low-boiling-point components (e.g., nitrogen and argon) as impurities is introduced from a warm end of the main heat exchanger (1) and cooled, then introduced into the oxygen rectification column (5), and product ultra-high-purity oxygen from which the low-boiling-point components have been removed is drawn as a gas or a liquid from a lower portion of the oxygen rectification column (5) or from the oxygen vaporizer (6).
  • the method may also comprise a step in which the feed oxygen which has been at least partially liquefied in the main heat exchanger is introduced into the oxygen rectification column.
  • the method may also comprise a step in which one or more of: a portion of feed air cooled in the main heat exchanger, a portion of the feed oxygen cooled in the main heat exchanger, and a liquid or gas drawn from the medium-pressure rectification column is utilized as a heating medium in the oxygen vaporizer, liquefied oxygen supplied from a bottom portion of the oxygen rectification column is vaporized, and a vapour stream thereof is supplied to the bottom portion of the oxygen rectification column.
  • An oxygen condenser may be provided above or in a top portion of the oxygen rectification column.
  • liquid or gas drawn from the medium-pressure rectification column (2) examples include oxygen-containing liquid, oxygen-containing gas, liquefied nitrogen, and nitrogen gas, etc.
  • the method may also comprise a step in which liquefied nitrogen or an oxygen-containing liquid supplied from the medium-pressure rectification column, or liquid nitrogen or liquefied air supplied from outside the air separation unit is utilized as a refrigerant in the oxygen condenser, and a low-boiling-point component-containing oxygen stream supplied from the oxygen rectification column is liquefied and supplied to a top portion of the oxygen rectification column as a reflux liquid.
  • the method may also comprise a step in which a portion of the feed oxygen drawn from partway through the main heat exchanger is expanded by an expansion turbine (92) and cooled, after which it is once again supplied to the main heat exchanger (1), so as to maintain a heat balance in the main heat exchanger.
  • “Ultra-high-purity oxygen” means an oxygen concentration of 99.99999% or greater.
  • “Feed oxygen” may be by-product oxygen (high purity oxygen, oxygen concentration of around 99.99%) generated by means of water electrolysis.
  • An ultra-high-purity oxygen production apparatus may comprise:
  • the ultra-high-purity oxygen production apparatus may comprise:
  • An ultra-high-purity oxygen production apparatus may comprise:
  • the ultra-high-purity oxygen production apparatus may comprise:
  • the oxygen vaporizer of the ultra-high-purity oxygen production apparatus may utilize, as a heating medium, one or more of: a portion of the feed air cooled in the main heat exchanger, a portion of the feed oxygen cooled in the main heat exchanger, and an oxygen-containing liquid or liquefied nitrogen drawn from the medium-pressure rectification column.
  • the ultra-high-purity oxygen production apparatus may comprise:
  • the ultra-high-purity oxygen production apparatus A1 constitutes an air separation unit comprising: a main heat exchanger 1, a medium-pressure rectification column 2, a nitrogen condenser 3, a low-pressure rectification column 4, an expansion turbine 92, an oxygen rectification column 5, an oxygen vaporizer 6,and a sub-cooler 8.
  • Feed air and feed oxygen are introduced into the main heat exchanger 1 from a warm end thereof and drawn from a cold end thereof, while product nitrogen gas and waste gas are introduced from the cold end thereof and drawn from the warm end thereof. Predetermined impurities and moisture are removed from the feed air.
  • the feed oxygen is by-product oxygen from water electrolysis, and contains low-boiling-point components (e.g., nitrogen and argon) as impurities.
  • the oxygen concentration of the feed oxygen is around 99.99%.
  • the feed oxygen has previously been dried to remove water and may also be purified to removed other impurities, such as residual hydrogen.
  • the feed oxygen is at a pressure between 15 and 30 bars abs within the heat exchanger 1.
  • the oxygen is preferably liquefied first of all, then undergoing heat and substance exchange with a vapour stream containing oxygen inside a rectification column so that the low-boiling-point components are removed while oxygen is concentrated in the liquid phase, and, for this purpose, at least a portion of the feed oxygen is liquefied in the main heat exchanger 1 in this embodiment, after which the feed oxygen is fed to the oxygen rectification column 5.
  • the medium-pressure rectification column 2 comprises: a bottom portion 21 into which the feed air cooled in the main heat exchanger 1 is introduced, a rectification portion 22, and a column top 23.
  • a feed air pipeline L1 is a pipeline for introducing the feed air, via the main heat exchanger 1, into a gas phase in the bottom portion 21 of the medium-pressure rectification column 2, or into a lower portion of a purification portion 22.
  • a first oxygen rich liquid pipeline L21a is a pipeline for introducing, into an intermediate stage of a rectification portion 42 of the low-pressure rectification column 4, via the sub-cooler 8, an oxygen-rich liquid drawn from the bottom portion 21 of the medium-pressure rectification column 2.
  • the first oxygen-rich liquid pipeline L21a and a second oxygen-rich liquid pipeline L21b may branch from a main pipeline L21 for the oxygen-rich liquid.
  • a condensing pipeline L23 is a pipeline which delivers, to the nitrogen condenser 3, a nitrogen-rich gas drawn from the column top 23 of the medium-pressure rectification column 2, and which merges with a first circulation gas pipeline L231 leading out from the column top 23.
  • the first circulation gas pipeline L231 is a pipeline for introducing, into a column top 43 of the low-pressure rectification column 4, via the sub-cooler 8, a nitrogen-rich gas drawn from the column top 23 of the medium-pressure rectification column 2.
  • the nitrogen condenser 3 condenses a nitrogen-rich gas drawn from the column top 23 of the medium-pressure rectification column 2.
  • a first waste gas pipeline L31 is a pipeline for causing the gas, which is drawn from the gas phase the nitrogen condenser 3, to pass through a part of the main heat exchanger 1, the gas then being used in the expansion turbine 92, and once again passed through the main heat exchanger 1.
  • the low-pressure rectification column 4 has the column top 43 and the rectification portion 42 into which is introduced a nitrogen-rich gas condensed in the nitrogen condenser 3 and/or a nitrogen-rich gas drawn from the column top 23 of the medium-pressure rectification column 2, after said nitrogen-rich gas has been cooled in the sub-cooler 8.
  • a product nitrogen gas pipeline L43 is a pipeline for causing the nitrogen-rich gas drawn from the column top 43 of the low-pressure rectification column 4 to pass through the main heat exchanger 1, via the sub-cooler 8.
  • a gas drawn from a gas phase the nitrogen condenser 3 is introduced into the expansion turbine 92 after said gas has been passed through a part of the main heat exchanger 1. After being used in the expansion turbine 92, the gas is once again delivered to the main heat exchanger 1 from where it is drawn out as a waste gas.
  • the oxygen rectification column 5 has a column top 53 or a purification portion 52 into which the feed oxygen that has undergone heat exchange and liquefaction in the main heat exchanger 1 is introduced, following expansion in valve V.
  • a feed oxygen pipeline L10 is a pipeline for introducing the feed oxygen, via the main heat exchanger 1, into the column top 53 or the rectification portion 52 of the oxygen rectification column 5.
  • a second waste gas pipeline L53 is a pipeline for causing low-boiling-point component-containing oxygen gas, which is drawn from the column top 53 of the oxygen rectification column 5, to merge into the waste gas pipeline L31 downstream from the expansion turbine 92 and upstream from the main heat exchanger 1.
  • the oxygen vaporizer 6 is arranged below a bottom portion 51 of the oxygen rectification column 5 and vaporizes liquefied oxygen while using, as a heating medium, an oxygen-rich liquid drawn from the bottom portion 21 of the medium-pressure rectification column 2.
  • the second oxygen-rich liquid pipeline L21b is a pipeline for introducing the oxygen-rich liquid drawn from the bottom portion 21 of the medium-pressure rectification column 2 into the oxygen vaporizers, from where it is introduced into an intermediate stage of the rectification portion 42 of the low-pressure rectification column 4.
  • An ultra-high-purity oxygen extraction pipeline L61 is a pipeline for extracting ultra-high-purity oxygen (liquid) from a vaporized liquid portion 61 of the oxygen vaporizer 6.
  • the oxygen vaporizer 6 is arranged below the oxygen rectification column 5 in order to supply a vapour stream to the oxygen rectification column 5.
  • the oxygen vaporizer 6 vaporizes liquefied oxygen supplied from the bottom portion 51 of the oxygen rectification column 5 and supplies the vapour stream thereof to the bottom portion 51 of the oxygen rectification column 5.
  • a portion of the feed oxygen is utilized as a heating medium.
  • a portion of the feed air supplied from the main heat exchanger 1, or a portion of an oxygen-containing liquid or liquefied nitrogen supplied from the medium-pressure rectification column 2 may be utilized.
  • the gas which is used as the heating medium may be liquefied and used as a reflux liquid in the low-pressure rectification column 4, or as a refrigerant in the main heat exchanger 1 or the sub-cooler 8.
  • the liquid which is used as the heating medium is sub-cooled, and therefore vaporization loss during decompression is reduced.
  • the sub-cooler 8 performs heat exchange of: an oxygen-rich liquid drawn from the bottom portion 21 of the medium-pressure rectification column 2, a purified gas condensed in the nitrogen condenser 3 and/or a purified gas drawn from the column top 23 of the medium-pressure rectification column 2, and a nitrogen-rich gas drawn from the column top 43 of the low-pressure rectification column 4.
  • the description of the ultra-high-purity oxygen production apparatus A2 will focus on features which are different from those of the ultra-high-purity oxygen production apparatus A1 of embodiment 1, and features which are the same will not be described, or will be described in simple terms. Reference symbols which are the same denote the same functions.
  • the ultra-high-purity oxygen production apparatus A2 comprises an oxygen condenser 7 for condensing a low-boiling-point component-containing oxygen gas drawn from the column top 53 of the oxygen rectification column 5.
  • the second oxygen-rich liquid pipeline L21b is a pipeline for introducing the oxygen-rich liquid drawn from the bottom portion 21 of the medium-pressure rectification column 2 into the oxygen vaporizer 6, where heat is released from the oxygen-rich liquid and it is then introduced into a cold heat liquid portion 71 of the oxygen condenser 7.
  • a second circulation gas pipeline L71 is a pipeline for introducing, into the intermediate stage of the rectification portion 42 of the low-pressure rectification column 4, an oxygen-rich liquid drawn from the cold heat liquid portion 71 of the oxygen condenser 7.
  • a third circulation gas pipeline L73 is a pipeline for introducing, into the intermediate stage of the rectification portion 42 of the low-pressure rectification column 4, a gas drawn from a column top 73 of the oxygen condenser 7.
  • the oxygen condenser 7 is arranged above the oxygen rectification column 5 in order to improve a recovery rate of ultra-high-purity oxygen. This makes it possible to increase the amount of ultra-high-purity oxygen that can be recovered from the feed oxygen which is supplied, while maintaining the purity of the ultra-high-purity oxygen.
  • An oxygen-containing liquid or liquefied nitrogen supplied from the medium-pressure rectification column 2 or the low-pressure rectification column 4, or liquefied feed air condensed in the oxygen vaporizer 6 may be utilized as a refrigerant in the oxygen condenser 7. Furthermore, liquefied nitrogen or liquefied air may also be supplied from the outside.
  • the description of the ultra-high-purity oxygen production apparatus A3 will focus on features which are different from those of the ultra-high-purity oxygen production apparatus A2 of embodiment 2, and features which are the same will not be described, or will be described in simple terms. Reference symbols which are the same denote the same functions.
  • the ultra-high-purity oxygen production apparatus A3 comprises a branch feed oxygen pipeline L11.
  • the branch feed oxygen pipeline L11 branches the feed oxygen from partway through the main heat exchanger 1 in a feed oxygen pipeline L10, and merges into the first waste gas pipeline L31 before connection to the expansion turbine 92.
  • a portion of the feed high-pressure oxygen is drawn from partway through the main heat exchanger 1, and expanded by the expansion turbine 92 and cooled, after which it is once again supplied to the main heat exchanger 1, so as to maintain a heat balance in the main heat exchanger 1.
  • This enables the cold heat required for liquefying the feed oxygen to be supplied to the main heat exchanger 1. If there is any surplus feed oxygen, the cold heat thereof may be utilized to contribute to maintaining a cold heat balance in the air separation unit or the nitrogen generating apparatus.
  • the ultra-high-purity oxygen production apparatus B1 comprises: a main heat exchanger 1, a nitrogen rectification column 2, a first nitrogen condenser 3, a second nitrogen condenser 30, an expansion turbine 92, a compressor 91, an oxygen rectification column 5, and an oxygen vaporizer 6.
  • a main heat exchanger 1 a nitrogen rectification column 2
  • a first nitrogen condenser 3 a second nitrogen condenser 30
  • an expansion turbine 92 a compressor 91
  • an oxygen rectification column 5 an oxygen vaporizer 6.
  • the difference with embodiments 1-3 lies in the single-column nitrogen rectification column, with two nitrogen condensers and a compressor for recycling gas being provided. The features which are different will mainly be described.
  • the nitrogen rectification column 2 comprises: a bottom portion 21 into which the feed air cooled in the main heat exchanger 1 is introduced, a rectification portion 22, and a column top 23.
  • the first nitrogen condenser 3 condenses a nitrogen-rich gas drawn from the column top 23 of the nitrogen rectification column 2.
  • the second nitrogen condenser 30 condenses the nitrogen-rich gas drawn from the column top 23 of the nitrogen rectification column 2.
  • a gas drawn from a gas phase in the first nitrogen condenser 3 is introduced into the expansion turbine 92 after said gas has been passed through a part of the main heat exchanger 1.
  • the compressor 91 is connected to the expansion turbine 92 and compresses a gas drawn from a gas phase in the second nitrogen condenser 30.
  • the oxygen vaporizer 6 is arranged below a bottom portion 51 of the oxygen rectification column 5 and vaporizes liquefied oxygen while using, as a heating medium, an oxygen-rich liquid drawn from the bottom portion 21 of the nitrogen rectification column 2.
  • a feed air pipeline L1 is a pipeline for introducing the feed air, via the main heat exchanger 1, into a gas phase in the bottom portion 21 of the nitrogen rectification column 2, or into a lower portion of a purification portion 22.
  • a first oxygen-rich liquid pipeline L21a is a pipeline for introducing, into a cold heat liquid portion (not depicted) of the second nitrogen condenser 30, the oxygen-rich liquid drawn from the bottom portion 21 of the nitrogen rectification column 2.
  • a first condensing pipeline L231 delivers a nitrogen-rich gas drawn from the column top 23 of the nitrogen rectification column 2 to the first nitrogen condenser 3 and returns same to the column top 23.
  • a second condensing pipeline L232 delivers the nitrogen-rich gas drawn from the column top 23 of the nitrogen rectification column 2 to the second nitrogen condenser 30 and returns same to the column top 23.
  • a product nitrogen gas pipeline L23 causes the nitrogen-rich gas drawn from the column top 23 of the nitrogen rectification column 2 to pass through the main heat exchanger 1, from where it is drawn as product nitrogen gas.
  • a first waste gas pipeline L31 is a pipeline for causing the gas, which is drawn from the gas phase 31 in the column top of the first nitrogen condenser 3, to pass through a part of the main heat exchanger 1, the gas then being used in the expansion turbine 92, and once again passed through the main heat exchanger 1.
  • a recycled gas pipeline L301 is a pipeline for causing a gas drawn from a gas phase 301 in the column top of the second nitrogen condenser 30 to be compressed in the compressor 91, then passed through a part of the main heat exchanger 1, from where it is introduced into a lower portion of the rectification portion 22 of the nitrogen rectification column 2.
  • a feed oxygen pipeline L10 is a pipeline for introducing the feed oxygen, via the main heat exchanger 1, into the column top 53 of the oxygen rectification column 5.
  • a second waste gas pipeline L53 is a pipeline for causing low-boiling-point component-containing oxygen gas, which is drawn from the column top 53 of the oxygen rectification column 5, to merge into the waste gas pipeline L31.
  • a second oxygen-rich liquid pipeline L21b is a pipeline for introducing the oxygen-rich liquid drawn from the bottom portion 21 of the nitrogen rectification column 2 into the oxygen vaporizer 6, from where it is introduced into the cold heat liquid portion (not depicted) of the second nitrogen condenser 30.
  • An ultra-high-purity oxygen extraction pipeline L61 is a pipeline for extracting ultra-high-purity oxygen (liquid) from a vaporized liquid portion 61 of the oxygen vaporizer 6.
  • Embodiment 5 has the same basic configuration as embodiment 4. The difference lies in the feed oxygen pipeline L10 and the oxygen-containing liquid pipeline L22.
  • the feed oxygen pipeline L10 is a pipeline for introducing the feed oxygen, via the main heat exchanger 1, into an intermediate stage of the rectification portion 52 of the oxygen rectification column 5.
  • the oxygen-containing liquid pipeline L22 is a pipeline for introducing, into the column top 53 of the oxygen rectification column 5, an oxygen-containing liquid drawn from an intermediate stage (a position above the feed air introduction pipeline L1) of the rectification portion 22 of the nitrogen rectification column 2.
  • the feed oxygen is introduced into the intermediate stage of the oxygen rectification column 5, and the oxygen-containing liquid from the intermediate stage of the nitrogen rectification column 2 is supplied to the column top 53 of the oxygen rectification column 5.
  • the oxygen-containing liquid is drawn from a stage of the nitrogen rectification column above the stage where the feed air is supplied, so that the oxygen-containing liquid does not contain any high-boiling point impurities derived from the atmosphere.
  • oxygen originating from the nitrogen rectification column can be purified into high-purity oxygen while at the same time a liquid for condensing the feed oxygen can be supplied to the oxygen rectification column, making it possible to produce high-purity oxygen while the operating rate of a water electrolysis apparatus and a nitrogen generating apparatus is optimized for high-purity oxygen demand.
  • the liquid nitrogen (nitrogen gas condensed in the condenser 3) drawn out through the pipe L231 and the oxygen-containing liquid (oxygen-rich liquid) drawn out through the pipe L21a were each cooled in the sub-cooler 8, after which the liquid nitrogen (nitrogen gas condensed in the condenser 3) was supplied to the top portion 43 of the low-pressure rectification column 4 operated at 2.5 barA.
  • the oxygen-containing liquid (oxygen-rich liquid) was supplied to the intermediate portion of the low-pressure rectification column 4.
  • the liquid nitrogen and the oxygen-containing liquid were rectified while undergoing heat and substance exchange with the vapour stream supplied from the nitrogen condenser 3, and nitrogen gas was drawn from the top portion 43 of the low-pressure rectification column 4 at 730 Nm 3 /h, and a waste gas was drawn from the bottom portion 31 at 270 Nm 3 /h.
  • Nitrogen gas drawn out through the pipe L43 was warmed in the sub-cooler 8 and then further warmed in the main heat exchanger 1, being drawn from the warm end of the main heat exchanger 1 at a temperature of 17.5°C and a pressure of 2.3 barA.
  • the waste gas drawn out through the pipe L31 was warmed to -120°C in the main heat exchanger 1 then expanded by the expansion turbine 92 and cooled, after which the waste gas was once again supplied to the main heat exchanger 1, and drawn from the warm end of the main heat exchanger 1 at a temperature of 17.5°C, and a pressure of 1.15 barA.
  • the feed oxygen containing 1 ppm of argon as impurity was introduced into the main heat exchanger 1 at a flow rate of 30 Nm 3 /h, a temperature of 20°C, and a pressure of 10 barA, cooled to -153.5°C and liquefied.
  • the oxygen-containing liquid (oxygen-rich liquid) was supplied at 310 Nm 3 /h from the bottom portion 21 of the medium-pressure rectification column 2 as a heating medium for the oxygen vaporizers, and cooled, then supplied to the intermediate portion of the rectification portion 42 of the low-pressure rectification column 4.
  • Ultra-high-purity oxygen liquid in which the content of low-boiling-point components (argon impurity) had been reduced to 10 ppb was obtained at 7.3 Nm 3 /h from the vaporized liquid portion 61 of the oxygen vaporizer 6 or the column bottom portion of the oxygen rectification column 5.

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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)
EP24171695.0A 2023-04-24 2024-04-22 Procédé de production d'oxygène de très haute pureté et appareil de production d'oxygène de très haute pureté Pending EP4464962A3 (fr)

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JP2023070607A JP7355980B1 (ja) 2023-04-24 2023-04-24 超高純度酸素製造方法及び超高純度酸素製造装置
FR2400965A FR3150578B3 (fr) 2023-04-24 2024-01-31 Procédé et appareil de séparation d’air par distillation cryogénique
FR2401265 2024-02-09

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JP (1) JP7355980B1 (fr)
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JP7505702B1 (ja) 2023-12-06 2024-06-25 レール・リキード－ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード 高純度酸素製造方法及び高純度酸素を製造する空気分離装置
WO2025202876A1 (fr) * 2024-03-28 2025-10-02 Fabrum Ip Holdings Limited Système et procédé de cryo-séparation améliorés

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5049173A (en) 1990-03-06 1991-09-17 Air Products And Chemicals, Inc. Production of ultra-high purity oxygen from cryogenic air separation plants
JP3929799B2 (ja) 2002-03-11 2007-06-13 日本エア・リキード株式会社 超高純度酸素の製造方法及び製造装置
WO2014173496A2 (fr) 2013-04-25 2014-10-30 Linde Aktiengesellschaft Procédé permettant d'obtenir un produit air dans une installation de séparation de l'air à stockage temporaire et installation de séparation de l'air
JP2021055890A (ja) 2019-09-30 2021-04-08 レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード 高純度酸素製造装置
CN114017993A (zh) 2022-01-06 2022-02-08 杭州制氧机集团股份有限公司 一种利用绿电电解水制氢副产氧气的装置及方法
WO2023274574A1 (fr) 2021-07-02 2023-01-05 Linde Gmbh Procédé et installation permettant de fournir un produit à base d'azote, un produit à base d'oxygène et un produit à base d'hydrogène

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5590543A (en) * 1995-08-29 1997-01-07 Air Products And Chemicals, Inc. Production of ultra-high purity oxygen from cryogenic air separation plants
JP3203181B2 (ja) * 1996-05-14 2001-08-27 日本エア・リキード株式会社 窒素製造装置に付随する酸素製造方法
US6196021B1 (en) * 1999-03-23 2001-03-06 Robert Wissolik Industrial gas pipeline letdown liquefaction system
JP4960277B2 (ja) * 2008-02-26 2012-06-27 エア・ウォーター株式会社 超高純度酸素の製造方法
EP3739714A1 (fr) * 2019-05-16 2020-11-18 Linde GmbH Procédé de fonctionnement d'une installation industrielle et installation industrielle correspondante
CN210512327U (zh) * 2019-08-13 2020-05-12 安徽加力气体有限公司 高纯液氧生产装置
CN113061905B (zh) * 2021-03-23 2024-12-27 中国海洋石油集团有限公司 一种基于lng接收站的氢气制取和液化装置系统及方法
CN117355487A (zh) * 2021-06-01 2024-01-05 林德有限责任公司 用于生产氨的方法和设备
CN216048690U (zh) * 2021-09-26 2022-03-15 开封市鑫联空分设备有限公司 一种含氢氧气的提纯液化系统
CN115406182B (zh) * 2022-09-22 2025-11-14 盈德气体工程(浙江)有限公司 一种氧气回收空分装置

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5049173A (en) 1990-03-06 1991-09-17 Air Products And Chemicals, Inc. Production of ultra-high purity oxygen from cryogenic air separation plants
JP3929799B2 (ja) 2002-03-11 2007-06-13 日本エア・リキード株式会社 超高純度酸素の製造方法及び製造装置
WO2014173496A2 (fr) 2013-04-25 2014-10-30 Linde Aktiengesellschaft Procédé permettant d'obtenir un produit air dans une installation de séparation de l'air à stockage temporaire et installation de séparation de l'air
JP2021055890A (ja) 2019-09-30 2021-04-08 レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード 高純度酸素製造装置
WO2023274574A1 (fr) 2021-07-02 2023-01-05 Linde Gmbh Procédé et installation permettant de fournir un produit à base d'azote, un produit à base d'oxygène et un produit à base d'hydrogène
CN114017993A (zh) 2022-01-06 2022-02-08 杭州制氧机集团股份有限公司 一种利用绿电电解水制氢副产氧气的装置及方法

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EP4464962A3 (fr) 2025-03-12
JP7355980B1 (ja) 2023-10-04
US20240353173A1 (en) 2024-10-24
CN118836642A (zh) 2024-10-25
KR20240156942A (ko) 2024-10-31
FR3150578B3 (fr) 2025-07-11
FR3150578A3 (fr) 2025-01-03
TW202442936A (zh) 2024-11-01

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