EP4204603A1 - Récupération de chaleur lors de procédés d'électrolyse - Google Patents

Récupération de chaleur lors de procédés d'électrolyse

Info

Publication number
EP4204603A1
EP4204603A1 EP21737562.5A EP21737562A EP4204603A1 EP 4204603 A1 EP4204603 A1 EP 4204603A1 EP 21737562 A EP21737562 A EP 21737562A EP 4204603 A1 EP4204603 A1 EP 4204603A1
Authority
EP
European Patent Office
Prior art keywords
electrolysis
stream
heat
streams
temperature level
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
EP21737562.5A
Other languages
German (de)
English (en)
Inventor
Andreas Peschel
Benjamin HENTSCHEL
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 EP4204603A1 publication Critical patent/EP4204603A1/fr
Pending legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/02—Hydrogen or oxygen
    • C25B1/04—Hydrogen or oxygen by electrolysis of water
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/50—Processes
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B15/00—Operating or servicing cells
    • C25B15/02—Process control or regulation
    • C25B15/021—Process control or regulation of heating or cooling
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • C25B15/083—Separating products
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • C25B15/087—Recycling of electrolyte to electrochemical cell
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
    • C25B9/19—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/133—Renewable energy sources, e.g. sunlight

Definitions

  • the invention relates to a method for using waste heat in electrolysis processes and to a system for carrying out such a method.
  • Hydrogen is often obtained from hydrocarbons, for example by steam reforming, which is no longer politically desirable in many places in the context of combating climate change.
  • steam reforming In order to reduce carbon dioxide emissions, processes based on electrolysis, in particular of water, for hydrogen production are therefore increasingly being used industrially.
  • synthesis gas can be produced from carbon dioxide and water, which is conventionally produced via steam reforming of fossil hydrocarbons.
  • Electrolysis as a manufacturing process thus makes renewable sources accessible for these substances and can contribute to reducing the carbon dioxide content in the atmosphere.
  • carbon dioxide electrolysis can have net negative emissions of gases that contribute to global warming.
  • electrolysis in the form of alkaline electrolysis (AEL) or electrolysis on a proton exchange membrane (PEM) or anion exchange membrane (AEM), all of which can be used in the form of low-temperature electrolysis, typically with operating temperatures below 60 °C .
  • High-temperature electrolysis methods for example using solid oxide electrolysis cells (SOEC), are also used for the electrolysis of, for example, water and/or carbon dioxide.
  • SOEC solid oxide electrolysis cells
  • the low-temperature electrolysis processes mentioned in particular are suitable for efficiently using renewable electrical energy, which is often subject to strong fluctuations in supply, and at the same time balancing out these fluctuations in supply, which can also contribute to the stabilization of corresponding power grids.
  • Waste heat generated during electrolysis is often lost unused, which has a negative impact on the overall efficiency of the process. It is therefore desirable to provide an improved electrolysis concept in which waste heat is used as efficiently as possible.
  • a method for the electrolytic production of at least one hydrogen-containing product stream wherein a feed stream containing at least water is subjected to an electrolysis to obtain two withdrawal streams. Both extraction streams are subjected to a separation downstream of the electrolysis to obtain the at least one product stream and two water-containing liquid fractions. At least one of the two liquid fractions is at least partially returned to the electrolysis.
  • the input stream is heated upstream of the electrolysis by heat exchange against at least one of the two extraction streams.
  • the at least one extraction flow, from which heat is extracted by the heat exchange is subjected to additional cooling, the additional cooling taking place using at least one organic Rankine cycle or a Rankine cycle with an organic-chemical heat transport medium.
  • the electrolysis is operated at a higher temperature level than is usually the case, because the cooling effect is lower due to the preheating of the input. This brings with it a gain in efficiency when operating the electrolysis.
  • the higher temperature level of the electrolysis also has the effect that waste heat is generated at a higher temperature than usual.
  • an Organic Rankine Cycle can be used efficiently to utilize waste heat. With conventional systems, this does not make economic sense due to the lower operating temperatures of typically below 60 °C.
  • the Organic Rankine Cycle is based on the Clausius-Rankine thermodynamic cycle.
  • this process is identical to a conventional steam cycle, in which water is evaporated by heating, the energy is extracted by performing work, especially mechanical work, and the steam is released again is condensed in order to be returned to the starting point of the cycle process.
  • another, in particular organochemical, working fluid is used which has a higher vapor pressure or lower boiling point than water.
  • the working temperatures can thus be drastically reduced, so that even waste heat at a relatively low temperature level can be used, for example, to generate electricity using turbines.
  • a suitable working fluid is selected for the ORC depending on the intended temperature range. These can be individual organochemical compounds or mixtures of different compounds.
  • condensation media can also be provided for the ORC.
  • cooling water e.g., river water or sea water
  • vaporizing natural gas e.g., vaporizing hydrogen
  • vaporizing hydrogen e.g., vaporizing hydrogen
  • this temperature difference is further used to preheat the feed stream that is fed to the electrolysis.
  • the electrolysis as already mentioned, can be operated more efficiently at a higher temperature; on the other hand, the withdrawal stream is advantageously cooled as a result, so that the water contained therein, for example, has a lower vapor pressure.
  • This has an advantageous effect on the operation of the downstream separation, since the gaseous components of the extraction stream formed in the electrolysis are separated more effectively from the water contained.
  • conventional drying steps downstream of the separation can be made more efficient or omitted entirely.
  • the heat exchange according to the invention drastically reduces the system volume to be heated for a system start and thus also the start-up time required for the start, since preferably only the electrolysis unit itself and the corresponding media ducts between the heat exchanger and electrolysis are operated at the increased electrolysis temperature level.
  • the separation and processing of the input stream preferably takes place at a separation temperature level which, in particular, can essentially correspond to a natural outside temperature or is advantageously set by the energy balance between the corresponding system parts and the environment. Heat losses from these parts of the plant therefore only have a marginal effect on the overall energy balance of the method according to the invention and are negligibly small compared to conventional methods and plants.
  • the separation temperature level is therefore preferably between 10.degree. C. and 60.degree. C., preferably between 25.degree. C. and 50.degree. C., in particular around 30.degree.
  • Electrolysis is preferred as low-temperature electrolysis at an electrolysis temperature level that is in a temperature range between 60 °C and 200 °C, preferably between 70 °C and 150 °C, particularly preferably between 80 °C and 110 °C, in particular at about 95 °C, lies, operated.
  • high-temperature electrolysis can also be used, for example using a solid oxide electrolysis cell (SOEC).
  • SOEC solid oxide electrolysis cell
  • the waste heat can occur and be used at a significantly higher electrolysis temperature level, which is preferably between 300° C. and 1000° C., particularly preferably between 500° C. and 900° C., in particular at 800° C., with the advantages already mentioned Increased efficiency in the area of waste heat utilization.
  • the waste heat can be used, for example, initially using a conventional steam turbine, with the remaining residual heat also being able to be used here if necessary for preheating the input.
  • the use of waste heat according to the invention by means of ORC can preferably take place downstream of the preheating of the insert. Whether recycling the water into the feed stream is also advantageous in these configurations depends on the specific feedstocks used and process conditions, since steam from external sources is often used in the context of high-temperature electrolysis.
  • part of the input stream is fed into the electrolysis, bypassing the heat exchange.
  • the electrolysis temperature level can be set more precisely and overheating of the electrolysis can be avoided.
  • waste heat that is additionally present can be extracted from the system at a suitable point and used, for example, to desalinate water contaminated with metal ions, for example to provide a cleaned fresh insert 1 .
  • This additional waste heat extraction can take place, for example, downstream of the ORC and/or upstream of the separation.
  • a further aspect of the invention proposes a system for carrying out the described method according to the invention.
  • Advantageous configurations of the system according to the invention are set up for carrying out the further developments of the method described above and below with reference to the accompanying drawings.
  • the advantages described for the various configurations of the method therefore apply analogously to the corresponding system and vice versa.
  • waste heat is also advantageous in connection with other electrolysis technologies, for example in order to increase the efficiency of a chloralkali electrolysis or other electrolysis methods.
  • FIG. 1 shows a conventional electrolysis system or a conventional electrolysis process in a highly simplified schematic representation.
  • FIG. 2 schematically shows an advantageous electrolysis system with a feed-effluent heat exchanger and cooling of a withdrawal stream.
  • FIG. 3 shows an advantageous embodiment of a system according to the invention in a schematic representation.
  • the electrolysis system 100 shown in FIG. 1 comprises an electrolysis unit E and two separators S1, S2.
  • a feed stream 2 which is formed from a fresh feed 1 and from at least one liquid fraction separated in the separators S1, S2, is fed into the electrolysis unit E, for example with the aid of a pump.
  • Two bleed streams 3, 4 are removed from the electrolysis unit E and are each conducted separately into one of the two separators S1, S2.
  • feed stream 2 is a water-containing stream from which hydrogen and oxygen are at least partially generated in electrolysis unit E.
  • the oxygen is formed at the anode and drawn off together with the extraction stream 3 as anode stream 3 and fed into the separator S1.
  • the hydrogen is formed at the cathode and fed into separator S2 as cathode stream 4 .
  • the liquid components of the anode 3 or cathode stream 4 are separated as a liquid phase, while the oxygen 7 or hydrogen s are discharged as gaseous product streams 6, 7 from the system 100.
  • the liquid phase formed from the anode stream 3 is fed back into the feed stream 2, while the liquid phase 5 formed from the cathode stream is discarded and withdrawn from the system.
  • the input stream 2 is tempered upstream of the electrolysis unit E to a desired electrolysis temperature level.
  • a temperature control device is provided, which is arranged, for example, downstream of the pump mentioned and upstream of the electrolysis unit E.
  • the electrolysis temperature level is typically selected in such a way that, depending on the type of electrolysis unit E, there is a suitable reaction temperature. If the electrolysis unit E is equipped, for example, with a proton exchange membrane (PEM) or an anion exchange membrane (AEM) or is provided in the form of an alkaline electrolysis (AEL), it is particularly suitable for low-temperature electrolysis, so that the electrolysis temperature level is typically in the range between 30 °C and 80 °C is selected. In the case of an electrolysis unit E with a high-temperature electrolysis such as a SOEC (see above), on the other hand, temperatures in the range from 300° C. to 1000° C. are typically used. Accordingly, it can take a long time, for example, until a corresponding liquid phase separates out in the separators, or additional condensers are necessary.
  • PEM proton exchange membrane
  • AEM anion exchange membrane
  • AEL alkaline electrolysis
  • separators S1, S2 Further separation stages, such as separators, absorbers, dryers and other cleaning devices, can be connected downstream of the separators S1, S2, for example in order to be able to provide products from the product streams 6, 7 that meet the specifications.
  • a heat exchanger W according to the invention is provided in the system 200 shown in FIG.
  • the input stream 2 can be heated to the electrolysis temperature level while recovering waste heat from the electrolysis unit E from the extraction stream 3 .
  • a bypass or bypass 8 can lead part of the feed stream past the heat exchanger W, so that the electrolysis temperature can be adjusted, for example, via a volume ratio of the corresponding partial streams of the feed stream 2 . This can be done, for example, via a control loop or be controlled automatically or manually.
  • Further cooling of the bleed stream 3 is provided downstream of the heat exchanger W in order to cool the bleed stream to a separation temperature level.
  • This has the advantage that, at low temperatures, only a small amount of water present in the separator S1 the gas phase passes.
  • a product stream 7 that is preferably almost anhydrous, but at least has a low water content, can be removed from the separator S1.
  • an advantageous embodiment of an electrolysis system 300 is shown schematically in FIG. 3 .
  • the cooling of the bleed stream 3 includes an Organic Rankine Cycle (ORC) O in addition to the heat exchanger W, which is provided here, as well as in the system 200, in the form of a feed-effluent heat exchanger.
  • the ORC O uses waste heat from the electrolysis unit E for generating electric current, which, for example--if necessary after appropriate rectification and/or transformation--can in turn be fed into the electrodes of the electrolysis unit E. Any other use of the electricity generated in this way is of course also possible.
  • the ORC O is preferably arranged upstream of the heat exchanger W, since this is where the highest temperature is present in the extraction stream 3 and the ORC O can therefore be operated with a particularly favorable degree of efficiency.
  • another cooling device is also arranged downstream of the feed-effluent heat exchanger W, which finally cools the extraction stream 3 to the separation temperature level.
  • This additional cooling device can, for example, also be designed as a heat exchanger, with the waste heat removed here being able to be used, for example, for the desalination of seawater or waste water. This is particularly advantageous if water streams contaminated with salts are to be used as fresh feed 1 and must first be treated for this purpose.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Metallurgy (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Automation & Control Theory (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)

Abstract

L'invention concerne un procédé de fabrication électrolytique au moins d'un flux de produit contenant un hydrogène, un flux de départ (1, 2) contenant au moins de l'eau étant soumis à une électrolyse (E), ce qui permet d'obtenir deux flux de prélèvement (3, 4). En aval de l'électrolyse (E), les deux flux de prélèvement (3, 4) sont soumis à une séparation (S1, S2) qui permet d'obtenir l'au moins un flux de produit (6, 7) ainsi que deux fractions liquides (2, 5) contenant de l'eau. Au moins une des deux fractions liquides (2, 5) est renvoyée au moins partiellement à l'électrolyse (E). En amont de l'électrolyse (E), le flux de départ (1, 2) est chauffé par échange de chaleur avec au moins un des deux flux de prélèvement (3, 4). L'au moins un flux de prélèvement (3) duquel de la chaleur est extraite par échange de chaleur, est soumis à un refroidissement supplémentaire, le refroidissement supplémentaire s'effectuant par recours à un cycle de Rankine à fluide organique ou un cycle de Rankine à l'aide d'un fluide caloporteur chimico-organique (O). Ainsi l'électrolyse (E) est conduite à un niveau de température supérieur à l'accoutumée, car le préchauffage de départ entraîne un effet de refroidissement plus faible. On obtient ainsi un gain d'efficacité lors du fonctionnement de l'électrolyse (E). Le niveau de température supérieur de l'électrolyse (E) a également pour effet que la chaleur dissipée s'avère habituelle dans le cas d'une température supérieure. Ainsi l'utilisation d'un cycle de Rankine à fluide organique aux fins de récupération de la chaleur dissipée s'avère efficace. L'invention propose également une installation (300) correspondante destinée à la mise en œuvre du procédé.
EP21737562.5A 2020-08-27 2021-06-23 Récupération de chaleur lors de procédés d'électrolyse Pending EP4204603A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102020005242.8A DE102020005242A1 (de) 2020-08-27 2020-08-27 Wärmerückgewinnung bei Elektrolyseprozessen
PCT/EP2021/025226 WO2022042876A1 (fr) 2020-08-27 2021-06-23 Récupération de chaleur lors de procédés d'électrolyse

Publications (1)

Publication Number Publication Date
EP4204603A1 true EP4204603A1 (fr) 2023-07-05

Family

ID=76796917

Family Applications (1)

Application Number Title Priority Date Filing Date
EP21737562.5A Pending EP4204603A1 (fr) 2020-08-27 2021-06-23 Récupération de chaleur lors de procédés d'électrolyse

Country Status (10)

Country Link
US (1) US20230332302A1 (fr)
EP (1) EP4204603A1 (fr)
JP (1) JP2023540467A (fr)
KR (1) KR20230056684A (fr)
CN (1) CN115943230A (fr)
AU (1) AU2021331003A1 (fr)
BR (1) BR112023003224A2 (fr)
CL (1) CL2023000518A1 (fr)
DE (1) DE102020005242A1 (fr)
WO (1) WO2022042876A1 (fr)

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP4269658A1 (fr) * 2022-04-28 2023-11-01 Linde GmbH Procédé permettant de faire fonctionner une installation d'électrolyse en ce qui concerne la gestion de l'eau et installation d'électrolyse
CN218175136U (zh) * 2022-07-28 2022-12-30 考克利尔竞立(苏州)氢能科技有限公司 一种废热回收存储利用系统
WO2024110053A1 (fr) * 2022-11-25 2024-05-30 Thomas Noll Procédé de synthèse de vecteurs énergétiques gazeux ou liquides à partir d'une installation de conversion d'énergie thermique océanique
DE102023201421A1 (de) 2023-02-20 2024-08-22 Robert Bosch Gesellschaft mit beschränkter Haftung Verfahren zum Betreiben einer Elektrolyseanlage, Elektrolyseanlage
DE102023202387A1 (de) * 2023-03-16 2024-09-19 Robert Bosch Gesellschaft mit beschränkter Haftung Systemanordnung und Verwendung einer solchen Systemanordnung zur Elektrolyse von Wasser

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7188478B2 (en) * 2004-09-13 2007-03-13 General Electric Company Power generation system and method of operating same
DE102010035229A1 (de) * 2010-08-24 2012-03-01 Linde Ag Verfahren und Vorrichtung zur Erzeugung von Wasserstoff
EP2623640B1 (fr) * 2012-02-02 2019-01-09 Siemens Aktiengesellschaft Procédé de fonctionnement d'un électrolyseur
JP2016141868A (ja) * 2015-02-04 2016-08-08 三菱重工環境・化学エンジニアリング株式会社 排熱回収装置、発電システム、及び排熱回収方法

Also Published As

Publication number Publication date
DE102020005242A1 (de) 2022-03-03
CN115943230A (zh) 2023-04-07
CL2023000518A1 (es) 2023-10-20
AU2021331003A1 (en) 2023-03-23
BR112023003224A2 (pt) 2023-03-28
WO2022042876A1 (fr) 2022-03-03
US20230332302A1 (en) 2023-10-19
KR20230056684A (ko) 2023-04-27
JP2023540467A (ja) 2023-09-25

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