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EP3746576A1 - Procédé de recyclage de batteries au lithium - Google Patents

Procédé de recyclage de batteries au lithium

Info

Publication number
EP3746576A1
EP3746576A1 EP19703268.3A EP19703268A EP3746576A1 EP 3746576 A1 EP3746576 A1 EP 3746576A1 EP 19703268 A EP19703268 A EP 19703268A EP 3746576 A1 EP3746576 A1 EP 3746576A1
Authority
EP
European Patent Office
Prior art keywords
liquid
digestion
manganese
sulfuric acid
graphite
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
EP19703268.3A
Other languages
German (de)
English (en)
Inventor
Christian Hanisch
Tobias Elwert
Lisa Brückner
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.)
Duesenfeld GmbH
Original Assignee
Duesenfeld 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
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Application filed by Duesenfeld GmbH filed Critical Duesenfeld GmbH
Publication of EP3746576A1 publication Critical patent/EP3746576A1/fr
Pending legal-status Critical Current

Links

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
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/02—Roasting processes
    • C22B1/06—Sulfating roasting
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M10/00—Secondary cells; Manufacture thereof
    • H01M10/54—Reclaiming serviceable parts of waste accumulators
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/20—Graphite
    • C01B32/205—Preparation
    • 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
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/005—Preliminary treatment of scrap
    • 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
    • C22B15/00—Obtaining copper
    • C22B15/0063—Hydrometallurgy
    • 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
    • C22B21/00—Obtaining aluminium
    • C22B21/0015—Obtaining aluminium by wet processes
    • C22B21/0023—Obtaining aluminium by wet processes from waste materials
    • 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
    • C22B23/00—Obtaining nickel or cobalt
    • C22B23/04—Obtaining nickel or cobalt by wet processes
    • 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
    • C22B23/00—Obtaining nickel or cobalt
    • C22B23/04—Obtaining nickel or cobalt by wet processes
    • C22B23/0407—Leaching processes
    • 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
    • C22B23/00—Obtaining nickel or cobalt
    • C22B23/04—Obtaining nickel or cobalt by wet processes
    • C22B23/0453—Treatment or purification of solutions, e.g. obtained by leaching
    • 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
    • C22B26/00—Obtaining alkali, alkaline earth metals or magnesium
    • C22B26/10—Obtaining alkali metals
    • C22B26/12—Obtaining lithium
    • 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
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
    • C22B3/08—Sulfuric acid, other sulfurated acids or salts thereof
    • 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
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/26—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
    • 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
    • C22B47/00—Obtaining manganese
    • 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
    • C22B47/00—Obtaining manganese
    • C22B47/0018—Treating ocean floor nodules
    • C22B47/0045—Treating ocean floor nodules by wet processes
    • 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
    • C22B7/006—Wet processes
    • 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
    • C22B7/006—Wet processes
    • C22B7/007—Wet processes by acid leaching
    • 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 lithium batteries. According to a second aspect, the invention relates to a recovery plant for processing lithium batteries.
  • Lithium batteries are batteries in which the electrical energy is stored by an electrochemical reaction based on lithium. Lithium batteries are widely used. The recycling of lithium batteries is still causing problems. So far it has not been possible to recover the graphite contained in electrodes in such a quality that it can be reused in the production of lithium batteries. The recovery of lithium is also causing problems. The recovery of cobalt, nickel, manganese, which may be contained in lithium batteries, is also usually possible only in such a purity that it makes use in new lithium batteries economically impossible. Viewed holistically, the material recycling efficiency of known recycling processes with regard to the viewing level of the battery cell is less than 50% by weight.
  • a method for recovering vanadium from lithium metal polymer batteries is known.
  • the comminuted material is mixed with 30 percent dilute sulfuric acid.
  • the vanadium is then obtained as vanadium pentoxide.
  • Such a method can only be used sensibly if the vanadium content in the comminuted material is sufficiently high. But this is not the case, for example, in the frequently used lithium-ion batteries.
  • other metallic constituents for example cobalt, nickel and manganese, can only be extracted poorly.
  • the use of concentrated sulfuric acid is discouraged, among other reasons, for safety reasons.
  • the invention is based on the object to improve the recycling of lithium batteries.
  • the invention solves the problem by a method for recycling lithium batteries with the steps of (a) breaking up comminution material containing comminuted constituents of electrodes of lithium batteries with, in particular concentrated, sulfuric acid in a digestion Temperature of at least 100.degree. C., preferably at least 120.degree. C., more preferably at least 140.degree. C., so that exhaust gas and a digestion material are formed, (b) discharging the exhaust gas and (c) wet-chemical extraction of at least one metallic constituent of the digestion material - as, in particular at least one metallic constituent (preferably of two, three, four or more metallic constituents) selected from the list comprising cobalt, lithium, manganese, nickel and titanium.
  • the invention solves the problem by a recovery plant for processing lithium batteries, in particular used lithium batteries, with (a) a reactor for breaking up comminuted material, the comminuted components of electrodes of lithium Contains, with concentrated sulfuric acid at a digestion temperature of at least 50 ° C, (b) a sulfuric acid feed device for supplying sulfuric acid to the comminuted material and (c) a discharge device which is arranged to discharge lead from exhaust gas from the reactor.
  • the discharge device is in particular designed so that it is hydrogen fluoride-tight. In other words, hydrogen fluoride can not escape into the environment.
  • An advantage of the invention is that upon digestion of the comminuted material with sulfuric acid, which is preferably concentrated sulfuric acid, fluorine, which may be present in the comminuted material, is completely expelled. Fluorine compounds can form hydrogen fluoride, which is highly problematic from a health and safety point of view. In addition, hydrogen fluoride is highly corrosive. By breaking up the shredded material with sulfuric acid, the fluorine is removed from the material to be crushed so that the subsequent process steps can be carried out with less safety precautions and less material wear. Some separation processes (eg membrane separation processes, bipolar membrane electrodialysis) can not be performed in liquids with high fluoride contents, but are made possible by this preparation. In addition, impurities can not be produced by fluorine-containing substances, so that the other constituents of the comminuted material can generally be recovered with a high degree of purity.
  • sulfuric acid which is preferably concentrated sulfuric acid
  • Another advantage is that the battery graphite can often be recovered in such high purity that it can be used for the Fiergna new electrodes.
  • the process can generally be carried out so that the lithium is recovered in a sufficiently high purity, so that it is suitable for the production of new lithium batteries.
  • Cobalt, nickel, manganese and / or titanium, if contained in the comminuted material, can often also be recovered in a high degree of purity which makes it possible to reuse them in a battery.
  • the method according to the invention can be designed in most cases in such a way that, in contrast to pyrometallurgical methods, it clearly has lower energy requirements.
  • the method does not comprise a pyrometallurgical process step.
  • a method for recycling lithium batteries is understood in particular to mean a method in which metallic components of the lithium batteries are recovered.
  • the method according to the invention is also a method for extracting metallic components from lithium batteries.
  • the metallic constituents are for example lithium and / or secondary group metals, in particular metals of the sixth, seventh and eighth subgroup.
  • the subgroup metals are preferably manganese, and / or cobalt and / or nickel. It is also beneficial if copper and / or titanium is recovered.
  • a lithium battery is understood in particular to be an accumulator in which the electrochemical reaction involves lithium and / or lithium ions and / or a lithium compound.
  • a battery contains at least galvanic elements.
  • the lithium batteries are at least partially lithium-ion batteries.
  • the comminuted material contains at least 40 percent by weight, in particular at least 60 percent by weight, of lithium-ion batteries.
  • Lithium-ion batteries contain liquid, fluorine-containing electrolytes that make the use of lithium batteries much more difficult.
  • the content of fluorine in the comminuted material is preferably less than 7 percent by weight, in particular less than 5 percent by weight.
  • the content of fluorine in the comminuted material is preferably at least 0.5% by weight, in particular at least 1% by weight.
  • a recovery system is understood to mean, in particular, a device by means of which 1, 2, 3 or more metallic constituents of lithium batteries are or will be separated from other components of the lithium battery, so that further processing is possible.
  • temperatures are specified in the following description, these always refer to the average temperature in the corresponding object.
  • digestion at a digestion temperature of at least 50 ° C. is understood in particular to mean that the temperature of the comminuted material mixed with the sulfuric acid is on average 50 ° C. That locally higher or lower temperatures can exist is irrelevant.
  • the corresponding method step is preferably carried out at room temperature and ambient pressure under ambient atmosphere.
  • digestion is meant in particular that no dilute sulfuric acid is used.
  • the concentration of sulfuric acid is above 90%, in particular 95%, particularly preferably 98%.
  • the digestion is carried out in particular so that fluorine is expelled as hydrogen fluoride.
  • the digestion is carried out in such a way that fluorine constituents in the comminuted material in the form of hydrogen fluoride pass into the exhaust gas.
  • there is so little water in the mixture of comminuted material and sulfuric acid that a concentration of water-soluble fluoride below 100 milligrams per kilogram of digestion material, in particular below 10 milligrams per kilogram of digestion material.
  • the concentration of sulfuric acid is so high that the above-mentioned concentration of water-soluble fluoride per kilogram of AufBankmaterial is achieved.
  • the concentration of sulfuric acid is preferably at least 95%, preferably at least 98%. Unlike the use of non-concentrated sulfuric acid, the use of concentrated sulfuric acid results in little fluoride being present in the digestion material.
  • digestion is no leaching, since a lye is always carried out with an aqueous liquid.
  • the digestion material is particularly firm. Unlike processes in which no concentrated sulfuric acid is used, the reaction products, in particular the metal sulfates, can not dissolve in water and remain as solids. Crushed material is understood in particular to mean a material which has resulted from comminution of lithium batteries or at least one component of lithium batteries, in particular of electrodes, and, if appropriate, subsequent processing, for example drying. Thus, after the comminution several separation steps for the separation of comminuted metallic foils, plastic foils or Zellhüll- and module components follow. It is favorable if the comminuted material contains not more than 10% by weight, preferably not more than 5% by weight, of plastics and / or metallic impurities.
  • the comminuted material may contain powdered constituents of electrodes of lithium batteries.
  • uncomminuted material in particular electrode material, instead of the comminuted material. It is favorable, however, if this electrode material is comminuted.
  • the comminuted material may be a material which has not been subjected to any pyrometallurgical treatment, in particular roasting or incineration.
  • the comminuted material was not subjected to pyrometallurgical treatment.
  • the removal of the exhaust gas is understood in particular to mean that the exhaust gas is led away from the location of the decomposition, at least for the most part. It is possible that the exhaust gas is sucked off.
  • the exhaust gas usually contains a fluorine compound, in particular hydrogen fluoride. It is possible, but not necessary, for the hydrogen fluoride to be removed from the exhaust gas, in particular by precipitates, preferably with a calcium compound. It is also possible that the exhaust gas is supplied to a chemical process.
  • wet-chemical extraction is meant, in particular, that a substance that is liquid at 1013 hPa and room temperature or liquid in the state in which it is added is added to the digestion material or a substance resulting from the digestion material, thereby at least one substance containing a metal or a metal itself is separated.
  • the sulfuric acid is preferably at least 90% pure, more preferably at least 95% pure. However, it is possible that a sulfuric acid with a lower concentration is supplied to the crushed material.
  • the digestion temperature is preferably at least the temperature which is necessary in order to evaporate so much water from the sulfuric acid that it has a concentration of at least 90%, in particular at least 95%. Percentages are generally based on percent by weight.
  • the digestion of the comminuted material preferably comprises the step of mixing the comminuted material with the sulfuric acid.
  • the mixing may include spraying with sulfuric acid and / or compulsory mixing, for example, extruding, kneading or stirring.
  • the digestion temperature is preferably lower than the boiling temperature of the sulfuric acid to prevent evaporation of the sulfuric acid.
  • the digestion temperature is therefore lower than 335 ° C.
  • the digestion temperature is less than a binder decomposition temperature of a binder with which the active material is attached to its carrier.
  • the digestion temperature may be greater than the binder decomposition temperature. This prevents the binder from contaminating the graphite.
  • the disruption can be carried out to avoid the oxidation of graphite-like the other process steps-under protective gas, for example nitrogen or argon. It is possible, but not necessary, for other process steps to be carried out under protective gas.
  • protective gas for example nitrogen or argon. It is possible, but not necessary, for other process steps to be carried out under protective gas.
  • the digestion can - like the other process steps - be carried out batchwise or continuously.
  • the digestion material contains at most 15% water, in particular less than 10% water, preferably less than 5% water. If there is little or no water, fluorine is expelled as hydrogen fluoride, leaving little or no fluorine compounds.
  • the digestion is preferably carried out until a hydrogen fluoride concentration in the exhaust gas is below 0.83 mg per cubic meter.
  • the hydrogen fluoride concentration is below the detection threshold.
  • the detection threshold relates in particular to an infrared spectrometric measurement. In this way it is ensured that in the subsequent process steps no hydrogen fluoride can be released in significant quantities.
  • digestion is carried out until a fluorine concentration CF of water-soluble fluoride in the digestion material is below 100 milligrams per kilogram of digestion material, preferably below 10 mg / kg and particularly preferably below the detection threshold.
  • the sulfuric acid is added at least stoichiometrically, preferably more than stoichiometrically, to the comminuted material.
  • Flierunter is understood in particular that so much sulfuric acid is added that all non-noble metals and copper are extractable in the comminuted material and extracted according to a preferred embodiment in a subsequent process step.
  • so much sulfuric acid is added that all non-noble metals and copper in the comminuted material go to at least 99 percent by weight in solution. It should be noted that even with superstoichiometric addition of sulfuric acid due to the finiteness of the reaction rate and the resulting chemical equilibrium metal residues may remain which have not reacted with the sulfuric acid.
  • the concentrated sulfuric acid is used with a weight ratio to the weight of the comminuted material of at most 40 to 1, in particular at most 20 to 1, preferably at most 10 to 1. In other words At most 40 kilograms of concentrated sulfuric acid are added per kilogram of comminuted material.
  • cathode material For example, it is favorable if at least 1.8 grams of H2SO4 are added per gram of cathode material, in particular at least 1.8 grams of H2SO4 per gram of electrode active material.
  • the cathode material is in particular UMO2, where M stands for a transition metal or aluminum.
  • the cathode is the electrode that is positively charged when discharged.
  • the method comprises the step of separating hydrogen fluoride from the exhaust gas, in particular the precipitation of hydrogen fluoride from the exhaust gas. This is done, for example, by means of a calcium compound, so that calcium fluoride is formed.
  • the method comprises the steps of leaching the digestion material and depositing graphite so that a raw liquid is obtained. It is favorable if the method comprises the step of separating the pulverulent constituents of metal foils, metal and plastic pieces, so that separate powder of electrode active material is formed.
  • the leaching is preferably carried out with an aqueous liquid, in particular with water.
  • a weight ratio of digestion material to the aqueous liquid is preferably 1: 2 to 1:20.
  • the leaching is carried out for at least 1 minute and preferably for a maximum of 10 hours.
  • the deposition is preferably a filtration. But it is also possible that the graphite is centrifuged or otherwise deposited. Through the digestion with sulfuric acid it is generally achieved that the concentration of metal, in particular of metal ions, in the graphite is so small that the graphite is suitable as electrode graphite for the production of new lithium batteries or other batteries. It is possible that the method comprises the steps of cleaning the deposited graphite, which may be done with, for example, water or a dilute mineral acid.
  • the cleaning is preferably carried out so intensively that only ⁇ 10 mg / kg metal ions remain in the wash water. It has been found that graphite can be so severely damaged in its crystal structure in known processes that use as electrode graphite is not possible. Because, according to a preferred embodiment of the method, no wet-chemical or thermal oxidation is carried out before the graphite is deposited, the graphite is so little damaged in its crystal structure that it can mostly be reused in batteries.
  • the pH is preferably between -0.7 and 4.
  • the leaching is preferably carried out at room temperature, but this is not necessary.
  • the method includes the step of depositing copper from the raw liquid to form decuperated raw liquid.
  • the deposition of copper is the wet-chemical process taking place immediately after the leaching.
  • other metals are deposited before the deposition of copper.
  • it is a selective copper deposition.
  • a temperature at the deposition of the copper is preferably between 0 ° C and 100 ° C.
  • the deposition is preferably carried out for 1 minute to 720 minutes.
  • the deposition may be, for example, a cementation.
  • Cementation causes an electrochemical reaction of the copper ions to form elemental copper.
  • the cementation is carried out with a ferrous substrate.
  • the deposition includes a case.
  • the copper may be precipitated as copper sulfide.
  • the raw liquid is added to a precipitating substance. guided, for example, a sulfur-containing substance. This may be sodium hydrogen sulphide.
  • a precipitating substance guided, for example, a sulfur-containing substance. This may be sodium hydrogen sulphide.
  • copper sulfide precipitates, in particular CuS. It is favorable if the precipitating substance is added more than stoichiometrically, so that a concentration of copper ions in the decuperated crude liquid is preferably below 10 mg per liter, in particular preferably below 1 mg per liter.
  • the method comprises the step of oxidizing iron ions and precipitating iron.
  • Fe 2+ ions in the decuperated crude liquid are oxidized to Fe 3+ ions.
  • an oxidizing agent for example with an oxygen compound.
  • the oxygen compound may be, for example, hydrogen peroxide or ozone.
  • the precipitation of the iron is preferably carried out as a hydroxide. It is obtained by the precipitation of a pure liquid.
  • the precipitation of iron and / or aluminum and / or titanium is preferably carried out by adding NaOH, Na 2 CO 3, KOH, MgO or ammonium hydroxide.
  • pure fluid is intended merely to indicate that metals regarded as contaminants, such as iron, and optionally copper, aluminum and titanium, have been removed. In particular, the term pure fluid should make no statement about the concentration of other substances.
  • oxygen changes its oxidation number.
  • a compound which contains oxygen but does not change its oxidation number in the redox reaction can be used as oxidizing agent.
  • the oxidation is preferably carried out until the electrochemical potential is between 0.8 and 1.4 volts relative to the normal hydrogen electrode. In this area of tension the editors Fe 2+ ⁇ Fe 3+ + e ⁇ take place.
  • the pFI value in the oxidation is preferably at most 8.7.
  • the pFI value at failure is at most 8.7, preferably at most 7.8. In this way it is achieved that iron and / or aluminum and / or titanium are precipitated to a very large extent.
  • the process comprises a solvent extraction of cobalt. This is preferably done from the pure liquid. It is particularly advantageous to use a cobalt complexing agent, for example a complexing agent dissolved in a lipophilic liquid.
  • the lipophilic liquid may be, for example, a mineral oil, for example kerosene.
  • an organic phosphine acid for example Cyanex 272 (bis (2,4,4-trimethylpentyl) phosphinic acid).
  • the process comprises the subsequent step of solvent-extruding nickel. This is preferably done with a nickel complexing agent.
  • the complexing agent is preferably dissolved in a lipophilic liquid, for example in a mineral oil such as kerosene.
  • manganese is removed from this liquid in a subsequent extraction step, in particular by solvent extraction, preferably by means of a manganese complexing agent.
  • a manganese complexing agent for extracting nickel or cobalt, for example, Cyanex 301 (bis (2,4,4-trimethylpentyl) dithiophosphinic acid) is suitable, which can be used dissolved in kerosene.
  • Nickel for example, can be reextracted from the charged organic phase by means of hydrochloric acid or sulfuric acid and subsequently crystallized out as nickel chloride or nickel sulfate.
  • cobalt may also be reextracted from the loaded organic phase using hydrochloric acid and / or sulfuric acid and then crystallized out as cobalt chloride or cobalt sulfate.
  • manganese can be reextracted from the charged organic phase by means of hydrochloric acid and / or sulfuric acid, and then manganese chloride and / or manganese sulfate can be crystallized out.
  • manganese can be precipitated, for example as a carbonate
  • a target liquid is obtained.
  • lithium is precipitated from the target liquid. This can be done, for example, by adding a phosphate, for example sodium phosphate, or a carbonate, for example sodium carbonate.
  • the precipitation of the lithium is preferably carried out at pH 7 to 14.
  • lithium is preferably precipitated from the clean liquid (28). This case occurs when, for example, only lithium iron phosphate batteries are used to produce the crushing material.
  • the comminuted material preferably comprises powdered electrode material made from lithium-ion batteries. From the comminuted lithium-ion batteries, smaller electrode foils, separator foils, other foils, the cell cladding materials and components of the battery module periphery are separated, so that powdery electrode active material is formed.
  • the comminuted material is obtained by crushing batteries and subsequently inactivating the raw comminuted material thus obtained by drying. It is particularly favorable if the comminution takes place under inert gas atmosphere and / or vacuum. If the crushing is done under vacuum, a pressure is preferably at most 300 hPa. A temperature is preferably at most 100 ° C, preferably at most 80 ° C. In this way the formation of fluoro-organic substances is avoided. The fluorine remains in the comminuted material and, as described above, is expelled by digestion with sulfuric acid.
  • shredded metallic current collector foils, separator foils of the cell cladding constituents and of the module constituents are separated so that the comminuted material is obtained.
  • the batteries are pre-discharged and / or obtained by disassembling battery systems or battery modules.
  • the reactor is preferably a rotary kiln or a heated compulsory mixer. This ensures intimate mixing of sulfuric acid with the comminuted material.
  • the reactor receives, for example, a temperature control or regulation by means of which the temperature of the mixture of comminuted material and sulfuric acid is brought to the digestion temperature and held thereon. It is also possible that the digestion is discontinuous, for example in a chamber furnace.
  • the recovery plant comprises a leaching device for leaching the digestion material in an aqueous medium.
  • the recovery plant preferably has a fluorine separator for separating the hydrogen fluoride.
  • the hydrogen fluoride can be precipitated.
  • the hydrogen fluoride is derived in a reaction with another substance, for example an organic substance.
  • the recovery system is designed to be mobile. In other words, it is possible to move the recovery plant without having to disassemble it.
  • the recovery plant is arranged in a 20-foot container or a 40-foot container.
  • the reactor it is then possible, but not necessary, for the reactor to be designed to be mobile, and preferably for a further apparatus as defined in the claims, to be capable of handling a sulfuric acid feed device and a removal device, and preferably together in a 20-foot container or a 40-foot container are arranged.
  • the recovery plant comprises a graphite recovery device having a graphite deposition device, in particular a filter for depositing graphite, and disposed downstream of the reactor in a material flow direction.
  • a graphite recovery device having a graphite deposition device, in particular a filter for depositing graphite, and disposed downstream of the reactor in a material flow direction.
  • the graphite recovery device comprises a washout device for washing out adherent lye solution from the graphite.
  • This washout device is preferably designed to wash out the lye solution with an aqueous liquid.
  • the recovery plant comprises a fluorine detector for detecting fluorine compounds, in particular hydrogen fluoride.
  • the fluorine detector is preferably a hydrogen fluoride meter for measuring a hydrogen fluoride concentration in the exhaust gas.
  • the recovery system comprises a control unit which is connected to the fluorine detector and is designed to automatically actuate the reactor so that it holds the digestion temperature until the fluorine concentration, in particular the hydrogen fluoride concentration, In the exhaust gas has fallen below a predetermined limit.
  • the recovery plant comprises a precipitator separator for separating, in particular filtering, precipitated Cu or Cu compounds.
  • the recovery plant has a solvent extraction device for extracting cobalt, manganese and / or nickel, which is arranged downstream of the graphite recovery device in the material flow direction.
  • the recovery system preferably also has a Fe / Al / Ti precipitate separator for separating off, in particular filtering off, precipitated iron and / or aluminum and / or titanium compounds.
  • the Fe / Al / Ti precipitated material separator is preferably arranged downstream of the rotary kiln in the material flow direction and in front of an optionally present solvent extraction device.
  • the maximum temperature to which the comminuted material or the pulping material is exposed is preferably at most 1000 ° C., preferably at most 700 ° C., in particular less than 335 ° C.
  • the comminution material has preferably not been subjected to a decrepitation treatment.
  • a recovery plant preferably comprises a comminution unit for comminuting the lithium batteries so that shredded material is obtained.
  • the recovery system preferably also includes an inactivation device for inactivating the shredded material. It is favorable if the inactivation device comprises a drying device which is set up for drying the shredded material until an electrolyte content of the shredded material is so small that an electrochemical reaction is impossible.
  • the recovery plant has a vacuum system connected to the drying device for generating a vacuum in the drying device.
  • the vacuum device is designed to generate a vacuum of at least 300 hPa.
  • the vacuum system is designed such that a pressure of 300 hPa or less is achieved.
  • the vacuum system is preferably constructed so that the maximum achievable pressure is greater than 0.01 Pa, preferably greater than 1 Pa.
  • the recovery plant has a hard metal separating device for separating hard metal from the material to be crushed.
  • a device for separating fragments of peripheral components of the battery system, the battery cell and / or the current contacts of the lithium battery is understood by the hard metal separating device.
  • the hard metal separating device comprises a magnetic separation device and / or a classifier, in particular a cross-flow classifier and / or a zigzag classifier.
  • the recovery plant preferably comprises a light fraction separation device for separating a light fraction comprising, for example, the separator film and coating material.
  • the light fraction separation device preferably comprises a zigzag sifter and / or an air separator, it being favorable when the air in the light fraction separation device is recirculated. This reduces the dust exposure of the environment.
  • the air separator may be, for example, an air-steel wire.
  • the recovery system has a separating device, in particular a classifying device, for separating active material from the carrier, in particular by air jet sieves and / or by a second comminuting step, so that an active material fraction and a carrier fraction are formed.
  • the carrier fraction comprises in particular aluminum and copper foil.
  • the recovery plant it is possible, but not necessary, for the recovery plant to have a filling device for filling the comminuted material into a transport container. By means of this transport container, the comminuted material can be transported over a possibly longer distance, which is for example at least 1 km. Thereafter, the comminuted material can be guided out of the transport container into the reactor.
  • the recovery system has no filling device for filling the comminuted material into a transport container.
  • the comminuted material after comminution is preferably transported to the reactor by means of a continuous or discontinuous conveyor and introduced there into the reactor.
  • FIG. 2 shows a schematic view of a recovery plant according to the invention
  • FIG. 3 shows a flowchart for a method according to the invention for processing cobalt-, nickel- and manganese-free comminuting material
  • FIG. 4 shows the flow diagram of a method for processing cobalt- and nickel-free, manganese-containing comminution material
  • FIG. 5 shows a flow chart of a method according to the invention for manganese- and nickel-free, cobalt-containing comminution material.
  • FIG. 6 shows a flow chart for the processing of manganese-free, cobalt- and nickel-containing comminution material.
  • FIG. 7 shows a comminution unit of a recovery plant according to the invention.
  • FIG. 1 shows a flow chart of a method according to the invention.
  • comminuted material for example in the form of comminuted Elektrodengentmateri- as provided. This can be done for example by means of a method which is described in DE 10 2015 207 843 A1.
  • batteries it is possible for batteries to be first comminuted so that raw comminuted material is obtained.
  • the raw comminuted material is deactivated by drying, so that inactivated raw comminuted material is obtained.
  • the inactivation is preferably a drying. Drying takes place, for example, under an inert gas atmosphere or under a vacuum. It is favorable if a pressure is at most 300 hPa and a temperature during drying is at most 80 ° C. Thus, comminuted material 10 is obtained, which can no longer react to a significant extent electrochemically, since the low-boiler content of the electrolyte is too low.
  • the electrode active material is separated from the raw comminuted material according to a preferred embodiment of the method.
  • This is preferably a combination of mechanical stress, magnetic separation, non-ferrous metal separation, screening and density separation. It is advantageous to use a Heilstrahlsiebung, so is obtained by finer separation grain sizes a purer Siebgut.
  • This comminuted material 10 is mixed with sulfuric acid 12.
  • the mixing may be, for example, a stirring by means of a stirrer. However, it is also possible that the mixing is a mere admit. This is possible in particular when the comminuted material 10 is located in a reactor in the form of a rotary kiln. It is also possible that the comminuted material and the sulfuric acid are mixed together in a reaction vessel, preferably made of steel. The mixed comminution material thus obtained is then fed to a reactor, in particular a rotary kiln.
  • the sulfuric acid 12 is preferably at least 95% pure.
  • the digestion produces waste gas 14, which in particular contains hydrogen fluoride HF.
  • the digestion takes place until, in a discontinuous comparison experiment in a container without continuous addition of material in the exhaust gas 14, a content of a fluorine compound, in particular a hydrogen fluoride content, is below a predetermined threshold of, for example, 0.83 mg per cubic meter. This is checked by means of a fluorine detector 15, which continuously measures a fluorine concentration.
  • the digestion is carried out in a batch process, the digestion is carried out so long that the content of a fluorine compound, in particular a hydrogen fluoride content, is below a predetermined threshold of, for example, 0.83 mg per cubic meter.
  • digestion is carried out until a fluorine concentration CF of water-soluble fluoride in the digestion material is below 100 milligrams per kilogram of digestion material, preferably below 10 mg / kg and particularly preferably below the detection threshold.
  • the residence time of the comminuted material 10 and the sulfuric acid 12 is selected so that the digestion material has a fluorine concentration CF of water-soluble fluoride which does not exceed the stated values.
  • digestion material 16 is formed which, to a good approximation, can be considered fluorine-free.
  • the digestion material 16 is mixed with water 18 and thereby leached.
  • the leaching can be done in the same container in which the digestion of the crushed material was, but this is not necessary. It is also possible for example that the digestion material is filled into a container which preferably already contains water.
  • the leaching takes place at a pH of -0.7 to 4 and preferably without active heat supply or removal.
  • the graphite deposition device 22 is a filter having a pore size of at most 15 micrometers, preferably at most 10 micrometers. It is favorable if the pore size is at least 0.5 micrometers.
  • the graphite 20 can be purified in a subsequent process step, for example with water, an alcohol, an organic solvent or a mineral acid, so that electrode graphite is obtained.
  • Electrode graphite is such graphite that is suitable for the production of electrodes, in particular for lithium batteries. There is thus obtained a raw liquid 24.
  • metallic copper Cu is obtained, for example by cementation.
  • metallic iron is brought into contact with the raw liquid 24 so that iron ions go into solution and copper precipitates out metallic.
  • the copper is deposited as copper sulfide. This is done for example by precipitation by addition of sodium hydrogen sulfide NaHS. By depositing the copper, decuperated raw liquid 26 is obtained. This has a pH value in the interval from 0 to 4, for example pH 1.
  • the Fe 2+ ions in the decuperated crude liquid 26 are subsequently oxidized to Fe 3+ ions. In the present case this is done by adding hydrogen peroxide H2O2. However, another oxidizing agent may be used.
  • the pH of the decuperated crude liquid is below 4.3 before oxidation. This step is preferably carried out without active heat supply or removal.
  • iron, aluminum and optionally titanium are precipitated in the form of a hydroxide.
  • the pH is increased to a value between 4.3 and 8.7. This is done by adding sodium hydroxide and subsequent deposition, in particular filtering or centrifuging, of the resulting precipitate. It is thus obtained a pure liquid 28 in addition to the deposited hydroxides.
  • nickel and cobalt are extracted by means of solvent extraction. This is done in the present case using Cyanex 301, which is dissolved in an organic solvent, usually kerosene.
  • FIG 1 shows that two solvent extraction steps are nested.
  • Cobalt and nickel are first extracted by means of Cyanex 301, which is dissolved in kerosene.
  • acid especially hydrochloric or sulfuric acid, a solution 30 containing nickel and cobalt is obtained. These are crystallized separately after further separation using Cyanex 272.
  • manganese for example manganese
  • it basically means the metals in elemental form as well as compounds containing this metal, generally including the metal ions.
  • the statement that manganese, cobalt and nickel are extracted also means that manganese, cobalt and nickel ions and compounds, especially ions, containing manganese, cobalt and nickel are removed.
  • the pH of the target liquid 32 may be between -0.7 and 10.5.
  • the manganese is removed from the manganese-containing target liquid 32 by means of solvent extraction. This can be done for example by means of D2EHPA, which is dissolved in kerosene.
  • the manganese is removed by precipitation, which can be done for example by adding sodium hydroxide.
  • the precipitation can be carried out by adding sodium carbonate.
  • Removing the manganese produces a target liquid 34.
  • This liquid contains lithium ions as an important constituent.
  • the lithium is removed from the target Liquid 34 precipitated. This is done for example by means of sodium carbonate.
  • a favorable temperature is at most 30 Kelvin below the boiling point of the target liquid 34 and preferably above 50 ° C.
  • the lithium carbonate is washed by means of water at 50-100 ° C, preferably 80-100 ° C, and / or ethanol.
  • the lithium may be precipitated as lithium phosphate, to which, for example, sodium phosphate may be added.
  • the concentration can be carried out, for example, by reverse osmosis and / or evaporation.
  • FIG. 2 shows a schematic view of a recovery system 36 according to the invention for processing lithium batteries, in the present case in the form of comminuted material 10, which is produced from lithium batteries.
  • the recovery plant 36 comprises in the present case a reactor 40 in the form of a rotary kiln, in which the comminuted material 10 is digested with sulfuric acid 12.
  • the comminuted material 10 and the sulfuric acid 12 were previously mixed together in a mixer 42.
  • the mixer 42 is advantageous, but dispensable.
  • the sulfuric acid 12 is supplied by means of a sulfuric acid feed device 43, which can be, for example, a metering device comprising a sulfuric acid container and a controllable valve. However, it is also possible that the sulfuric acid 12 is poured from a container.
  • the recovery plant 36 comprises a discharge device 44 in the form of an exhaust pipe, which may be connected to a vacuum generator, so that the exhaust gas 14 is sucked out of the reactor 40.
  • the removal device 44 may have a scrubber for washing off hydrogen fluoride.
  • the exhaust gas 14 in this scrubber is associated with a calcium compound, for example, with an aqueous solution containing calcium ions, so that hydrogen fluoride in the exhaust gas 14 is washed out.
  • the exhaust gas 14 is supplied by means of the discharge device 44 to a reactor, which reacts the hydrogen fluoride, for example, with an organic substance.
  • the fluorine concentration CF is detected by the fluorine detector 15.
  • a leaching device 46 is arranged, in which the digestion material 16, for example by means of water, is leached.
  • a graphite recovery device 48 is arranged which in the present case has only the graphite separation device 22 in the form of a filter.
  • An optional leaching device for washing out adhering lye solution from the graphite is not shown. It is also possible first to fill the graphite in a transport container and to carry out the washing out of adhering clay solution after transport to another location.
  • the copper extractor 50 comprises a container 52 for cementing the copper after the addition of iron, in particular in the form of iron sheet or iron shavings, and a precipitator separator 54 for separating selected copper compounds.
  • the Dijkgut-From separator 54 may be, for example, a filter.
  • the pore size of the filter is preferably less than 50 micrometers and at least 1 micrometer.
  • the precipitate separator is designed to deposit copper sulfide, and the container 52 serves to react the raw liquid 24 with NaFIS so that copper sulfide precipitates.
  • a Fe / Al / Ti precipitated material separator 56 is arranged, in which an oxidizing agent 58 is added to the decuperated raw liquid 26. This can be done in a first container 60.1.
  • the solution obtained is then transferred to a second container 60.2, for example pumped.
  • a hydroxide is added, in particular an alkali metal hydroxide. For example, sodium hydroxide is supplied.
  • aluminum, iron and possibly titanium are precipitated out as hydroxides or as hydrogenated oxide.
  • the precipitate is removed by means of a particle separator 62 downstream in the material flow direction.
  • the particle separator 62 is formed, for example, by a filter which may have a pore size of at most 15 micrometers.
  • the resulting pure liquid 28 is fed to a solvent extraction device 64 which includes a Co / Ni solvent extraction device 66.
  • This comprises a large number of reaction vessels 38.1, 38.2,..., which are connected to one another as shown in FIG.
  • the structure of a solvent extraction apparatus is known from the prior art and therefore will not be explained in detail. Thereby, the manganese-containing target liquid 32 is obtained.
  • the target liquid 32 is supplied to a manganese solvent extraction device 70, which generates target liquid 34.
  • the manganese-containing target liquid 32 is fed to a second precipitation reactor 72, in which the manganese is precipitated as manganese hydroxide after addition of a hydroxide, in particular an alkali hydroxide such as, for example, sodium hydroxide.
  • the manganese-containing target liquid 32 is fed to a precipitation reactor 74.
  • a carbonate in particular after addition of sodium carbonate, precipitated or precipitated as manganese carbonate.
  • the lithium is precipitated in respective containers as carbonate by addition of sodium carbonate or as phosphate by addition of sodium phosphate. It is possible for the recovery plant 36 to include a concentrator 74 for removing water from the target liquid 34 to facilitate precipitation.
  • FIG. 3 shows a flow chart for a method according to the invention for processing cobalt-, nickel- and manganese-free comminution material and / or electrode material. It can be seen that the method corresponds to the method according to FIG. 1, the steps relating to the extraction of cobalt, nickel and manganese being omitted.
  • FIG. 4 shows a flow chart for the processing of manganese-containing, cobalt- and nickel-free comminution material and / or electrode material.
  • For the extraction of manganese only the variant with the solvent extraction is shown.
  • the alternatives for removing the manganese shown in FIGS. 1 and 2 are also possible for the method according to FIG. 4 and represent preferred embodiments.
  • Figure 5 shows the flow diagram of a process for processing manganese and nickel-free, cobalt-containing electrode and / or comminution material.
  • FIG. 6 shows a flow chart of a method according to the invention for cobalt- and nickel-containing, manganese-free electrode and / or comminuting material.
  • FIG. 7 shows a second embodiment of a recovery system 36 according to the invention, wherein the components arranged behind the leaching device 46 in the material flow direction have been omitted for the sake of clarity. It can be seen that the recovery plant 36 has a shredding unit 118 and an inactivation device 126.
  • the inactivation device 126 is designed as a drying device.
  • lithium batteries 110.1, 110.2,... are discharged in a discharge unit 112.
  • disassembly station 114 disassembly of the lithium batteries 110 follows, if necessary, because otherwise the battery systems can not be carried into the shredding unit 118 for geometric or gravimetric reasons.
  • the battery systems are opened if necessary and disassembled so far that the modules and or stacks can be removed individually.
  • the individual lithium battery cells can be separated from the control electronics.
  • the shredding unit 118 may include a rotary shear having at least one rotor and at least one stator.
  • the shredding unit 118 can also comprise a cutting mill with one or more rotors.
  • the comminution unit 118 comminutes the lithium batteries 110.i under protective gas 120, which is taken, for example, from a protective gas cylinder 122. Alternatively or additionally, liquid nitrogen from a liquid nitrogen source 119 may be added.
  • the protective gas may be, for example, nitrogen, a noble gas, carbon dioxide, nitrous oxide or another, preferably non-toxic gas.
  • shredded material 124 is produced, which is fed to an inactivation device in the form of a drying device 126.
  • a lock 128 Disposed between the comminution unit 118 and the drying device 126 is a lock 128 which is gastight so far that the drying device 126 is separated from the comminution unit 118 in a gas-tight manner to a good approximation.
  • the drying device 126 is connected to a vacuum system 129, which has a vacuum pump 130 and generates a vacuum.
  • a pressure pi26 of pi26 100 ⁇ 60 hPa, preferably 50 hPa.
  • the vacuum pump is a compressor that sucks and compresses gas 131 existing in the dryer 126.
  • the vacuum system 129 may have a jet pump, in which a jet medium in the form of a liquid is passed through at least one Venturi nozzle at high speed.
  • the blasting medium is preferably alkaline and has a pFI value of at least pH 13 and is, for example, a 10% potassium hydroxide solution.
  • the vacuum system 129 includes a gas cleaning device 132, which is arranged between the drying device 126 and the vacuum pump 130 and in the present case a capacitor 134 and / or an activated carbon filter 136 summarizes.
  • the condenser is operated at a temperature of, for example, -10 ° C., so that carbonic acid dimethyl ester and ethyl carbonate of carbonic acid can condense and be discharged into a condensate container 138. In addition, any existing water is frozen out.
  • a control valve 140 is configured to open when the pressure p26 becomes too high and to close when the pressure pi26 becomes too small, that is, to fall below a predetermined threshold.
  • the drying material is moved in the drying device 126. This can happen, for example, by stirring with a stirrer 141, such as an anchor stirrer or a rod stirrer, with rods, for example, mounted perpendicular to the stirrer shaft. Alternatively by a moving drying container.
  • the drying of the shredded material 124 produces inactivated comminuted material 10, which is supplied to the mixer 42.
  • the inactivated comminuted material 10 is filled into a transport container 146 under vacuum and / or under protective gas.
  • the transport container 146 is preferably gas-tight. It is possible, but not necessary, for the transport container 146 to be filled with inert gas before being transported away, so that it is under normal pressure. Alternatively, it is also possible that the transport container is closed and transported under vacuum. It is possible that, as an alternative to the transport container, a vacuum-welded film, for example an aluminum composite film, is selected.
  • Protective gas 120 is supplied from the vacuum pump 130 to the comminution unit 118 via a purge line 148. If the vacuum pump 130, as in the present case, which represents a preferred embodiment, also functions as a compressor, the protective gas 120 can be drawn onto a compressed gas cylinder 150. Alternatively or additionally, the protective gas 120 may be released into the environment, optionally after additional purification.

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Abstract

L'invention concerne un procédé de recyclage de batteries au lithium qui comprend les étapes suivantes : (a) désagréger le produit de broyage (10) qui contient des constituants broyés d'électrodes de batteries au lithium avec de l'acide sulfurique (12) concentré, à une température de désagrégation (TA) d'au moins 100°C, en particulier d'au moins 140°C, de sorte à produire des gaz brûlés (14) et un matériau de désagrégation (6), (b) évacuer les gaz brûlés (14) et (c) extraire par procédé chimique par voie humide au moins un constituant métallique du matériau de désagrégation (16).
EP19703268.3A 2018-01-30 2019-01-29 Procédé de recyclage de batteries au lithium Pending EP3746576A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE102018102026.0A DE102018102026A1 (de) 2018-01-30 2018-01-30 Verfahren zum Verwerten von Lithium-Batterien
EP18170117.8A EP3517641B2 (fr) 2018-01-30 2018-04-30 Procédé de valorisation de batteries au lithium
PCT/EP2019/052122 WO2019149698A1 (fr) 2018-01-30 2019-01-29 Procédé de recyclage de batteries au lithium

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