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WO2015010793A2 - Procédé de recyclage d'ensembles membrane-électrodes d'une pile à combustible - Google Patents

Procédé de recyclage d'ensembles membrane-électrodes d'une pile à combustible Download PDF

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Publication number
WO2015010793A2
WO2015010793A2 PCT/EP2014/002032 EP2014002032W WO2015010793A2 WO 2015010793 A2 WO2015010793 A2 WO 2015010793A2 EP 2014002032 W EP2014002032 W EP 2014002032W WO 2015010793 A2 WO2015010793 A2 WO 2015010793A2
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WO
WIPO (PCT)
Prior art keywords
solvent
mea
pem
membrane
loaded
Prior art date
Application number
PCT/EP2014/002032
Other languages
German (de)
English (en)
Other versions
WO2015010793A3 (fr
Inventor
Markus Paepke
Original Assignee
Daimler Ag
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 Daimler Ag filed Critical Daimler Ag
Publication of WO2015010793A2 publication Critical patent/WO2015010793A2/fr
Publication of WO2015010793A3 publication Critical patent/WO2015010793A3/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B11/00—Obtaining noble metals
    • C22B11/02—Obtaining noble metals by dry processes
    • C22B11/021—Recovery of noble metals from waste materials
    • C22B11/025—Recovery of noble metals from waste materials from manufactured products, e.g. from printed circuit boards, from photographic films, paper, or baths
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/005—Separation by a physical processing technique only, e.g. by mechanical breaking
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/008—Disposal or recycling of fuel cells
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/10—Fuel cells with solid electrolytes
    • H01M8/1004—Fuel cells with solid electrolytes characterised by membrane-electrode assemblies [MEA]
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/10—Fuel cells with solid electrolytes
    • H01M8/1016—Fuel cells with solid electrolytes characterised by the electrolyte material
    • H01M8/1018—Polymeric electrolyte materials
    • H01M8/1039—Polymeric electrolyte materials halogenated, e.g. sulfonated polyvinylidene fluorides
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/10—Fuel cells with solid electrolytes
    • H01M2008/1095—Fuel cells with polymeric electrolytes
    • 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
    • Y02E60/50—Fuel cells
    • 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
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/50—Reuse, recycling or recovery technologies
    • Y02W30/84—Recycling of batteries or fuel cells

Definitions

  • the invention relates to a method for recycling membrane-electrode assemblies of a fuel cell.
  • Fuel cells which are used as alternative energy sources for vehicles, each consist of a stacked arrangement of several hundred membrane electrode units (MEA).
  • MEA membrane electrode units
  • a typical "stack" for vehicle applications has about 5 to 8 kg of precious metal-containing material.
  • Palladium, iridium, etc. are used in membrane-electrode assemblies.
  • the platinum content of a stack delivering 50 kW is between 50 and 100 grams, depending on the specification.
  • MEA Membrane Electrode Units
  • CCM Catalyst Coated Membrane
  • EP 1 478 042 A1 discloses a process for the enrichment of
  • Precious metals from fluorine-containing fuel cell components known in which the heat treatment process in the presence of an inorganic additive, which binds the fluorine takes place.
  • this inorganic additive which is an oxide, carbonate, bicarbonate or hydroxide of an element of the first, second or third main group, is separated from the noble metal-containing material.
  • this larger amounts of fluorine-containing slags that need further treatment form are known in which the heat treatment process in the presence of an inorganic additive, which binds the fluorine takes place.
  • Electrolysis cell generates chlorine, by means of which the noble metals are oxidized and go into solution, so that the noble metals from the reaction solution and from the
  • Washing water with which the digested material was washed can be deposited electrolytically or by reduction. Due to the high level of chemicals required and the low recovery rates, this process approach is currently not economical.
  • Fuel cell components in which the fluorine-containing components separated by the treatment with water in a supercritical state of the noble metal-containing components.
  • the supercritical water in a temperature range of 350 to 450 ° C and a pressure range of 200 to 400 bar and in a 100 to 000-fold excess based on the mass of the fluorine-containing components.
  • the method places great demands on the
  • Membranes are dissolved in an aqueous solvent suspension, which in a Temperature is maintained between 190 and 290 ° C until a paste is formed. The paste is filtered and the components are separated from the filtrate to give a catalyst fraction and a membrane fraction. Again, there are economic and safety concerns.
  • the inventive method of recycling (recovering) the noble metals of membrane electrode assemblies of a fuel cell containing fluorine-containing noble metal-loaded proton exchange membrane material is subjected to ultrasound and presence of a solvent to separate the noble metal from the fluorine-containing membrane material and followed by filtration.
  • the proton exchange membrane is often referred to as polymer electrolyte membrane (PEM), or proton exchange membrane (PEM).
  • the catalyst-loaded PEM is often referred to as CCM (Catalyst Coated Membrane).
  • Catalyst layer on the PEM usually consists of noble metal mixtures comprising Pt, Pd, Rh, Ru, and Ir and a catalyst support material, in particular of carbon, carbon black, graphite and auxiliaries.
  • the proton exchange membrane material is crushed and transferred into a solvent-filled ultrasonic bath and subjected to ultrasound treatment, wherein the noble metal together with the catalyst support material passes into the solvent, or is detached from the membrane material. Then the freed of noble metal, fluorine-containing membrane material is separated from the now loaded with noble metal solvent and fed to the fluorine-containing membrane material for thermal or material recovery. Filtration of the loaded with the noble metal and catalyst support material solvent leads to a loaded with precious metal filter material, the after a certain filtration time of a conventional thermal process step, for example ash in an oven to
  • the precious metal recovery can be carried out advantageously in a conventional plant, since the fluorine-containing Polymer of the proton exchange membrane was previously discharged, so that here, unlike the thermal treatment of the proton exchange membrane itself no corrosive fluorine reaction products are formed. Therefore, the material of the
  • Furnace also less stressed and an additional flue gas cleaning to remove the fluorine products can be omitted. Further, with the
  • inventive method prevents the stripping of noble metal or platinum fluorides, so that the noble metal yield is increased.
  • the GDL can sometimes also contain precious metal, which diffused in particular during the use of MEA from the PEM ago. If necessary, the GDL can be processed in parallel, or in the same process together with the PEM.
  • snippets, flakes or flakes are produced which can easily be separated again from the solvent, for example via sieves, net baskets or grids.
  • the size of the snippets, flakes or flakes is in the range of 0, 1 mm 2 to 9 cm 2 , preferably in the range of 2 mm 2 to 900 mm 2
  • Both comminution, as well as the treatment in the ultrasonic bath are designed so that the PEM not , or is no longer comminuted to fine particles, which can produce suspensions or colloidal solutions. The same applies to the possibly parallel processed GDL.
  • the ultrasound treatment can take place under normal conditions; an ethanol (EtOH) -water mixture as a solvent is inexpensive.
  • EtOH ethanol
  • Aqueous ethanol is particularly suitable because it separates the catalyst coating well from the PEM, or GDL and the PEM does not dissolve or gel.
  • the solvent can be circulated to aid in acoustic cavitation-based solvent extraction, such as by slow stirring or, more effectively, by oscillation of the media carrier basket.
  • acoustic cavitation-based solvent extraction such as by slow stirring or, more effectively, by oscillation of the media carrier basket.
  • several Umnachlztechniken can be combined.
  • Circulation improves the movement of the membrane material in the ultrasonic bath, so that overlaps and folds are avoided.
  • the movement also ensures that the material being treated is kept in dead spaces or "sonic shadows.”
  • the ultrasonic bath can be cooled.
  • the filtered solvent can be recycled to the ultrasonic bath and reused for extraction.
  • the proton exchange membranes PEM Prior to the ultrasound-induced solvent extraction, the proton exchange membranes PEM can be isolated from the membrane-electrode assemblies. Alternatively, the MEA may also be fractionated and the separation omitted.
  • the MEA is framed with a silicone gasket, it should be removed in a first step. This can be done manually but also partially or fully automated, done by cutting or punching. Remains the component of the membrane-electrode assembly, which is arranged between two gas diffusion layers and having the proton exchange membrane. This MEA is comminuted to a preferred areal dimension between 15 x 15 mm 2 to 30 x 30 mm 2 . The MEA particles are then Schnipsei-shaped. For shredding a cutting or punching tool should be used. High-speed units should not be used as this could lead to erosion of the carbon carrier and the PGMs. Prior separation of the GDLs from the PEM is not mandatory. The material produced can then be fed to the separation of the carbon support together with precious metals of the ultrasonic treatment.
  • the filtering system used may, to prevent premature clogging of the filter and, on the other hand, also detect the nano-sized noble metal particles, have at least two series-connected filter stages, the filter material having decreasing pore size in the direction of flow. It also makes sense to choose a filter material that is solvent resistant and non-halogenated. Polypropylene is a suitable filter material.
  • the precious metal in the solvent is in the filter material
  • the filter mass is ashed, wherein the carbon and optionally. Auxiliaries are burned.
  • the remaining noble metal which is a mixture of different elements, such as Pt, Rh, Ir or Ru, is thus concentrated to the extent that a fractionation and recovery of each element economically worthwhile. Since the noble metal-containing material is now present in a modified matrix, no conclusions can be drawn on the original material by the recycler who performs the recovery. The remaining after removal of the seal component can be crushed by means of cutting or punching tools in Schnipseln. The use of
  • the separation of a carbon support covered by the proton exchange membrane or a soot particle layer from the fluorine-containing membrane material takes place at the same time.
  • the soot particles also pass into the solvent and are deposited together with the precious metals on the filter material, so that already optically a control of
  • the extraction step is preferably carried out several times, in particular in a cascaded arrangement of extraction stations.
  • the PEM, or GDL snippets can be collected in each extraction station in grid or net baskets and transferred to the subsequent station.
  • the filter over which the solvent is passed to separate the catalyst material be separated as soon as the intended filter occupancy is reached.
  • the solvent especially aqueous ethanol, separates the layers of MEA.
  • the GDL and PEM detach from each other.
  • Solvent an aqueous ethanol solution with 75 to 85 vol.% EtOH, preferably 20% water and 80% EtOH. Higher ethanol concentrations lead to no improvement, while lower ethanol concentrations significantly worse
  • FIG. 2 is an exploded perspective view of a membrane-electrode assembly
  • Fig. 3 is a side sectional view through an ultrasonic bath.
  • the device according to the invention relates to the enrichment of noble metals from fluorine-containing fuel cell components by ultrasound-induced
  • the ultrasound-induced extraction with 80% ethanol as solvent allows the fluorine-containing material of the proton exchange membrane to be excluded prior to the thermal process.
  • the noble metals are enriched in the filter, which is not made of fluorine-containing material but, for example, of polypropylene, so that the subsequent recovery of the noble metals in a conventional thermal process is safe, since no corrosive reaction products are formed. An elaborate flue gas cleaning and reduced furnace life can be avoided. Furthermore, the noble metal losses caused by stripping of platinum fluorides are minimized, the recovery rate is optimized.
  • the inventive method is outlined in Fig. 1 for recovering the noble metals from the membrane electrode assemblies of fuel cells.
  • the method can be subdivided essentially into the four process blocks P1 to P4.
  • process step P1 the membrane-electrode assemblies MEA are separated into their individual components, the proton exchange membranes PEM, the gas diffusion layers GDL and the seals D.
  • Fig. 2 shows a membrane-electrode unit MEA with its individual components shown, the two outer gas diffusion layers GDL, the intervening proton exchange membrane PEM, on which the noble metal is applied, and a peripheral seal D include.
  • the gas diffusion layers GDL consist of a carbon fiber braid, which is hydrophobicized with a layer of polytetrafluoroethylene.
  • the gas diffusion layers GDL are porous, brittle and brittle.
  • On the surface of the perfluorosulfonic acid polymer (PFSA) of the proton exchange membrane PEM there is a catalytic soot layer, associated with the polymer, of dense carbon black particles coated with noble metal particles.
  • the proton exchange membrane PEM is elastic and deformable.
  • the seal D is provided to separate the anode side of the cathode side gas and liquid-tight. Nafion ® is often used as PFSA.
  • the seal (silicone) D is separated (if present).
  • the separation of the GDLs from the PEM before the ultrasonic bath treatment is not absolutely necessary.
  • the size is preferably in the range of 225 mm 2 to 900 mm 2 .
  • the material is further treated in process step 2, while the seals D are a material or thermal recovery supplied.
  • Process step P2 leads to the recovery of PFSA, which is recycled in such a way that it can be recycled, after the
  • Soot particle layer including the noble metal was released from the PFSA surface.
  • the comminuted MEA (comprising PEM and GDL) according to the invention a treatment in the ultrasonic bath z. B. subjected to 45 kHz.
  • the ultrasonic frequency is preferably in the range from 20 to 10 kHz. Too high an ultrasonic frequency, or ultrasound energy is disadvantageous for the process, as this stable suspensions or colloids formed and the PEM or GDL would be further crushed. This would degrade the separation of the catalyst material by filtering and the separation of the PEM or GDL by sieves, grids or baskets.
  • the optimum solvent is ethanol and water in the ratio 4: 1 proved. Other solvents such as isopropanol and cyclohexane did not lead to the desired extraction result. While a higher water content in relation to ethanol one drastic deterioration of the extraction behavior leads to a
  • the extraction or ultrasonic treatment is carried out without heating or heating.
  • preference is given to a
  • a treatment time of only approx. 3 min is sufficient.
  • the extraction can be assisted by additional circulation of the solvent, for example by stirring or oscillation of the material carrier basket. Since a temperature rise caused by the ultrasonic effect of the
  • Solvent may affect the extraction process, cooling may optionally be provided.
  • cooling may optionally be provided.
  • soot particle film together with the noble metal loading is almost completely detached from the PFSA surface.
  • two fractions are obtained: the solvent laden with precious metal and carbon and the now non-precious PFSA and GDL material, which is now discharged and recycled.
  • Fig. 3 shows schematically the ultrasonic bath 1 in which the comminuted particles of the MEA (comprising PEM and GDL) in the solvent LM are subjected to the ultrasonic treatment.
  • the material particles PEM can easily with the help of a basket 2 with a
  • Mesh size are applied to the ultrasonic bath 1, which allows the particles PEM during the treatment in the basket 2 remain, even if they due to changes in their material properties during the extraction process their
  • Change grain size for example, enlarge.
  • the basket meshes should be smaller than 6 mm in order to avoid a rinsing of the particles through the mesh.
  • the swelling of the PEM the GDL dissolves so that the PEM floats freely in the medium and can be treated with the entire surface with the solvent LM and the ultrasonic waves.
  • the solution performance can be favored by a material circulation and so the
  • Fig. 3 shows nozzles 3 at the bottom of the ultrasonic bath 1, with which the material by a supplied liquid flow is set in motion and a circulation U is brought about. This avoids material through dead spaces and
  • the noble metal-loaded solvent LM is supplied to the filtration in the process step P3 (FIG. 1). Prior to material recycling, the PFSA and GDL material present in the basket 2 can still be rinsed, for example with water.
  • the noble metal loaded solvent LM is now transferred to a filtration system to separate the solvent from the noble metals.
  • the filter material retains the noble metals (and soot particles) and is fed to a conventional thermal recovery stage in the last process step P4. Therefore, filter materials are preferred which do not cause critical reaction products or emissions in the thermal treatment and are resistant to the solvent LM.
  • a fluorine-free plastic filter for example
  • Pore size (s) must be taken into account that the precious metal particles partially in
  • Suitable filter forms include filter cartridges inserted in a filter housing.
  • the noble metal-loaded filter material is removed after a certain period of use, but at the latest after the construction of a certain overpressure in front of the filter, and P4, the 4th process step 4, fed.
  • the filtered solvent LM can be returned to the ultrasonic bath of the process step P2 and thus used again.
  • step P4 the noble metal-loaded filter material and optionally the gas diffusion layers GDL are supplied to a conventional noble metal recovery, which can essentially correspond to the noble metal recovery from auto-exhaust catalysts.
  • the noble metals are concentrated in a blast furnace process, optionally with the use of various additives.
  • the precious metals enriched collector metal can be supplied to a hydrometallurgical treatment in which the metal alloy is dissolved and the noble metals are recovered by electrolysis.
  • the starting material selected was a membrane electrode assembly (MEA) made of PEM fuel cells with an area of approximately 100 ⁇ 600 mm 2 .
  • the MEA consisted of the components GDL, PEM, and silicone gasket.
  • the silicone gasket was removed. This was done manually, but can also be partially or fully automated, done by cutting or punching.
  • the MEAs were crushed to a surface area of 15 x 15 mm 2 to 30 x 30 mm 2 .
  • the MEA particles were Schnipei-shaped. Here, a cutting or punching tool was used. Fast-rotating units were not used, as this could lead to erosion of the carbon carrier, including the PGMs. A prior separation of the GDLs from the PEM was not necessary. - Ultrasonic bath treatment:
  • the prepared material was placed in a stainless steel basket.
  • Basket was chosen so that the material particles could not leave the basket.
  • Mesh size was chosen 6 x 6 mm 2 .
  • the material was with the basket in the with
  • Ultrasonic bath supplied for extraction constantly unloaded, fresh solvent.
  • the temperature of the solvent was adjusted to 20 ° C by means of a flow cooler located behind the last filter.
  • the extraction was terminated when the PEM appeared colorless or transparent. After extraction, the PEM from Nafion and the GDLs remained in the basket.
  • the basket with the Nafion and GDLs was removed from the ultrasonic bath and transferred to a water bath to quench the reaction. After rinsing, the material was recycled.
  • Car exhaust catalysts is applied are supplied.
  • the solvent was further processed. For this purpose, it was cleaned by another filter made of polypropylene with a porosity of 100 nm of other, invisible, PGM residues. This filter was also replaced by saturation, dried and fed to a PGM recovery process.
  • the purified ethanol solution was then distilled and used to make a "fresh" 80% ethanol solution.
  • the process used recovered more than 98% by weight of the precious metals in the MEA. In the MEA only traces of precious metals could be detected.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Manufacturing & Machinery (AREA)
  • Sustainable Development (AREA)
  • Mechanical Engineering (AREA)
  • Organic Chemistry (AREA)
  • Metallurgy (AREA)
  • Materials Engineering (AREA)
  • Sustainable Energy (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Inert Electrodes (AREA)

Abstract

L'invention concerne un procédé de recyclage d'ensembles membrane-électrodes (MEA) d'une pile à combustible comprenant un matériau de membrane échangeuse de protons (PEM) et des couches de diffusion de gaz (GDL), le PEM contenant un polymère d'acide perfluorosulfonique (PFSA) et un métal noble, sous l'effet d'ultrasons et en présence d'un solvant pour séparer par filtration le métal noble du matériau de membrane contenant du fluor, le procédé comprenant les étapes suivantes : - décomposition du MEA chargé avec un métal noble, en copeaux, flocons ou lamelles, - transfert du MEA décomposé, chargé avec un métal noble, dans un bain à ultrasons rempli d'un solvant (LM) d'éthanol aqueux, - exposition du matériau de membrane du MEA à un traitement par ultrasons dans le solvant (LM), le métal noble passant dans le solvant (LM), - séparation du matériau de membrane contenant du fluor (PFSA) du solvant chargé de métal noble (LM), et amenée du matériau de membrane contenant du fluor (PFSA) à un recyclage thermique ou un recyclage des matériaux, - filtration du solvant (LM) chargé avec le métal noble et obtention d'un matériau de filtration chargé de métal noble, - récupération du métal noble dans le matériau de filtration chargé, par un procédé thermique classique.
PCT/EP2014/002032 2013-07-26 2014-07-25 Procédé de recyclage d'ensembles membrane-électrodes d'une pile à combustible WO2015010793A2 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
DE102013012421 2013-07-26
DE102013012421.2 2013-07-26
DE201310013455 DE102013013455A1 (de) 2013-07-26 2013-08-10 Verfahren zum Recycling von Membran-Elektroden-Einheiten einer Brennstoffzelle
DE102013013455.2 2013-08-10

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Publication Number Publication Date
WO2015010793A2 true WO2015010793A2 (fr) 2015-01-29
WO2015010793A3 WO2015010793A3 (fr) 2015-05-07

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WO2018138427A1 (fr) 2017-01-24 2018-08-02 Commissariat A L'energie Atomique Et Aux Energies Alternatives Procede de recuperation du platine et du cobalt contenus dans une pile a combustible
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GB201505311D0 (en) * 2015-03-27 2015-05-13 Johnson Matthey Fuel Cells Ltd Process
EP4239088A1 (fr) * 2022-03-02 2023-09-06 Heraeus Deutschland GmbH & Co. KG Procédé de concassage des membranes électrolytiques polymères revêtues de catalyseur
DE102023103386A1 (de) 2023-02-13 2024-08-14 Schaeffler Technologies AG & Co. KG Recyclingvorrichtung und Verfahren zum Recyclen von Bestandteilen eines elektrochemischen Systems

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US20050211630A1 (en) 2004-03-26 2005-09-29 Ion Power, Inc. Recycling of used perfluorosulfonic acid membranes
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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2018138427A1 (fr) 2017-01-24 2018-08-02 Commissariat A L'energie Atomique Et Aux Energies Alternatives Procede de recuperation du platine et du cobalt contenus dans une pile a combustible
EP3957759A1 (fr) * 2020-08-05 2022-02-23 Robert Bosch GmbH Procédé d'extraction du platine et/ou du ruthénium

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