Method and facility for recycling battery cells or parts thereof

Abstract

The invention relates to a method and a facility (20) for recycling rechargeable battery cells (Z) or parts thereof which have electrolyte, lithium, and films provided with coating material, namely cathode films with a coating made of a cathode material and anode films with a coating made of an anode material. According to the method, - the cells (Z) are mechanically pre-comminuted in a shredder stage, in particular in a liquid medium (W), and a shredder fraction (S1) is obtained, - the shredder fraction (S1) is then rinsed in a pre-separation stage using a mechanical separator (24), in particular a stirring element under the effect of mechanical energy and using a liquid medium (W), thereby individualizing the films and rinsing out constituents of the shredder fraction (S1), such as electrolyte, coating material, and lithium, wherein the constituents are accumulated in the liquid medium (W), and a separator fraction (S2) is obtained in the pre-separation stage, and - the separator fraction (S2) is then further prepared in at least one separation stage.

Description

[0001] Description

[0002] Process and plant for recycling battery cells or parts thereof

[0003] The invention relates to a method and a system for recycling battery cells or parts thereof. These cells or parts thereof comprise, among other things, electrolytes and coated foils, namely cathode foils with a coating of cathode material and anode foils with a coating of anode material. Depending on the battery type, the cells or parts thereof contain additional components: lithium in the case of lithium batteries, nickel (nickel hydroxide) and a metal hydride in the case of NiMH batteries.

[0004] With the increasing use of lithium batteries, especially in the automotive industry for electromobility, the recycling of such batteries is becoming more and more of a focus.

[0005] DE 10 2019 218 736 A1 describes a method for the material-selective disassembly of lithium-ion batteries. The components are placed in a container filled with a liquid and crushed and separated using an electrohydraulic effect. A pulsed current source generates a surge discharge within the liquid within an underwater spark gap between a ground electrode and a high-voltage electrode. This surge discharge separates the coating material of the foils, i.e., the anode material or the cathode material, at least in sections. In subsequent separation steps, the foils and the coating materials can then be recovered separately and reused. Battery cells generally consist of an anode, a cathode, a separator, an electrolyte, and a housing.The anode and cathode are typically each formed by a foil provided with a coating. On the anode side, this is typically a copper foil (anode foil) coated with graphite as the anode material. On the cathode side, this is typically an aluminum foil (cathode foil), which is typically coated with a coating, e.g., a lithium-nickel-cobalt-manganese mixed oxide (NMC) as the cathode material. Alternatively, a coating of LiCoO, NiCoO, LiFePO4, or other known coating materials is applied. The layer thickness of the foil coatings is typically in the range of approximately 50 μm.

[0006] The electrolyte used in a lithium-ion battery (LIB) often consists of a conductive salt and a mixture of highly volatile and less volatile solvents, some of which are also solid at room temperature. The conductive salt only accounts for a few percent of the electrolyte, for example, only one percent by volume. A conductive salt such as LiPF6 (lithium hexafluorophosphate) is used.

[0007] During the battery charging process, lithium ions migrate from the cathode through the separator film to the anode and are deposited there. During the discharging process, however, the lithium ions migrate from the anode to the cathode and are reintegrated into the cathode material. While the lithium ions are tightly bound in the cathode material, on the anode side they are bound with only weak forces and are largely free in the electrolyte.

[0008] When recycling batteries, a rough mechanical disassembly typically begins, which can be done manually. Batteries typically consist of several interconnected modules, each of which contains several of the cells described above. The cells are obtained during the mechanical pre-shredding process and are then fed into the actual recycling process. Based on this, the invention seeks to enable the most efficient recycling of batteries or battery cells, especially lithium-ion batteries (cells) or parts thereof, with the highest possible recovery rate for the various valuable materials contained in the cells.

[0009] The object is achieved according to the invention by a method and a system for recycling battery cells or parts thereof. The battery cells are, in particular, cells of a lithium-ion battery. The advantages and preferred embodiments listed below with regard to the method also apply analogously to the system, and vice versa.

[0010] Where batteries are mentioned here, this refers in particular to accumulator batteries.

[0011] The system has a shredding stage, preferably with a mechanical shredder, which ensures mechanical pre-shredding of the cells. This is, in particular, wet shredding using a liquid medium. A (wet) shredder fraction is available at the output of the shredding stage. Through mechanical pre-shredding, in particular shredding, the films are exposed and separated from the cell housing. Shredders are generally understood to mean devices that use mechanical comminution devices, such as grinders, shearing devices, cutting devices, hammers, etc., to achieve comminution. In a broader sense, this also includes rotor shears, guillotines, etc.

[0012] The films contained in the shredder fraction preferably have a size in the range of 0.3 cm to 10 cm. This size is particularly well suited for the downstream electro-hydraulic separation device.

[0013] Following the shredding stage, the system comprises a pre-separation stage with a mechanical separator, which is particularly designed as an agitator. The shredded fraction is rinsed, in particular together with the liquid medium, in this mechanical separator under the action of mechanical energy with the aid of a liquid medium, in particular the liquid medium from the shredding stage, which is hereinafter referred to as process water without restriction of generality. The mechanical action in combination with the rinsing with the process water achieves several advantages: Firstly, the films, which are still densely packed in the cell, are advantageously separated. This makes the surfaces of the films more accessible in the subsequent process steps, and the subsequent separation and recycling steps can therefore be carried out with less effort and more efficiently.

[0014] At the same time, studies have shown that – in addition to washing out the electrolyte – at least a portion of the anode material, particularly the graphite, is advantageously removed from the anode foils and absorbed by the process water. This also improves the efficiency of the subsequent recycling steps.

[0015] Finally, rinsing – in the case of lithium-ion batteries – also removes any unbound lithium or ions in the process water. At the end of the mechanical separator, a wet separator fraction is obtained. This contains the process water and its constituents, as well as the shredded foils, at least partially still coated with the coating material.

[0016] This separator fraction is then fed to at least one further separation stage and further processed there. Specifically, it is fed to an electro-hydraulic separation device, such as that used in the

[0017] DE 10 2019 218 736 A1. In this separation stage, the material is divided into one or more coarse fractions, which in particular contain film and housing parts, and into a fine fraction which contains process water with particles floating in it. The plant is designed at least for the recycling of cells or parts thereof. However, modules or complete batteries can also be fed to the plant for recycling. For this purpose, for example, at least one disassembly stage is installed upstream of the shredding stage, in which the modules or batteries are first disassembled and shredded. Alternatively, larger units, such as modules, can also be fed to the shredding stage and shredded there.

[0018] The mechanical separator is preferably designed as a stirrer having an agitator. The stirrer generally comprises a container into which the shredded fraction is introduced. The agitator rotates within the container while simultaneously introducing the liquid medium, which is, for example, sprayed in. Alternatively or additionally, the container is at least partially filled with the process water, so that stirring takes place directly in the process water. The stirrer simply introduces mechanical energy, which leads to the desired separation of the anode material from the anode foils. This also assists in the leaching of the lithium. Finally, the mechanical movement of the agitator leads to the desired separation of the foils in a particularly efficient manner.

[0019] As an alternative to a stirrer with agitator, other combined rinsing and separation devices are also possible, for example a rotating drum can be provided and / or the process water is jetted onto the shredder fraction using high pressure through appropriate nozzles, so that the desired separation and rinsing is carried out by the jet pressure of the water.

[0020] Preferably, the mechanical separator is arranged directly below the shredder so that the shredder fraction can fall into the mechanical separator from above.

[0021] The residence time of the shredder fraction within the mechanical separator, and specifically also the stirring time, is typically in the range of several minutes, for example between 20 seconds and 5 minutes. In a preferred embodiment, the wet separator fraction is dewatered, whereby at least a portion of the liquid medium and the components it contains (particles and dissolved substances) are separated out. After dewatering, a dewatered separator fraction is therefore available for further treatment, specifically in the electro-hydraulic separation device. The particular advantage of this dewatering is that, among other things, the ions contained in the process water, e.g. lithium ions, are also removed, so that the proportion of these conductive elements is reduced for the subsequent process step.Studies have shown that the operation and efficiency of the downstream electrohydraulic separation device is impaired with increasing conductivity. Conductivity is generally determined by ions dissolved in the process water. In general, this upstream dewatering offers particular advantages for subsequent wet separation steps using electrical processes.

[0022] For dewatering, for example, a screening device is used through which the process water can pass and the dewatered separator fraction remains.

[0023] In a preferred embodiment, dewatering is carried out via a conveyor system, specifically a screw conveyor, which transports the separator fraction to the subsequent recycling stage. The conveyor system is particularly inclined so that the process water can flow downwards, counter to the conveying direction, and be collected there. This achieves particularly simple and efficient dewatering without the need for an additional dewatering device.

[0024] In a preferred embodiment, components contained in the separated process water (liquid medium) are recovered. In particular, lithium and / or anode material (graphite) are recovered from the separated process water. This is carried out in particular in a suitable treatment facility for the process water (liquid medium), which is preferably (re)fed as treated process water to the mechanical separator (e.g., agitator) and, in particular, to the shredder stage as the liquid medium. This already achieves a very simple and efficient (partial) recovery of lithium and / or graphite.

[0025] For treatment, a portion of the separated process water is fed to the treatment facility either continuously or periodically via a branch line. Alternatively, the entire separated process water is fed to the treatment facility continuously.

[0026] As already explained, the pre-shredding in the shredding stage preferably takes place in a liquid medium.

[0027] According to an alternative embodiment, only dry pre-shredding takes place without the addition of a liquid medium. The right to file a correspondingly amended claim 1 without a liquid medium in the shredding stage, in which the cells are shredded dry in the shredding stage, remains reserved.

[0028] In the preferred wet shredding process, the liquid medium is either sprayed into the pre-shredding system, specifically the shredder, or the shredder is filled with the liquid medium. This pre-shredding in a liquid medium, generally water or an aqueous solution, has the advantage that the released electrolyte components, such as free (lithium) ions, are immediately bound. This wet shredding process offers the following additional advantages over conventional, dry shredding processes:

[0029] - Due to the immersion of the cells or parts to be recycled in the process water, a protective gas atmosphere is initially neither required nor intended, as the process water effectively prevents fires in partially charged batteries. - This procedure ensures a dust-free shredding process.

[0030] - Furthermore, operation is preferably carried out at room temperature, whereas dry shredding processes usually require high temperatures of 80 °C or more to separate the electrolytes from the gas phase.

[0031] - Due to wet shredding, the electrolytes, the conductive salt they contain, and the (free) lithium ions are absorbed into the process water and / or dissolved in it during the shredding stage. In contrast, dry shredding processes only separate highly volatile gases, whereas the semi-volatile components of the electrolyte and the conductive salts dry out and are then carried through the recycling process with the so-called black mass, i.e., the separated solids. This leads to the latent risk of hydrofluoric acid (HF) formation.

[0032] - Another advantage of the wet process is that the electrolytes retain their chemical structure. They are preferably recycled and reused as needed.

[0033] - Another particular advantage is that lithium is absorbed by the process water at an early stage of the process and can therefore be extracted.

[0034] Finally, any residual electrical energy contained in the cell can be easily discharged within the process water. This means that, unlike conventional processes, prior battery discharge can be omitted and is preferably avoided. Furthermore, the heat absorbed by the process water can be used as process heat within the plant itself.

[0035] The comminution in the shredding stage in a liquid medium is considered an independent invention – regardless of the use of the mechanical separator, particularly in the form of an agitator – and the filing of a divisional application for this purpose remains reserved. The essential steps here are comminution in a liquid medium to obtain a wet shredder fraction, feeding the shredder fraction to a downstream recycling stage, specifically an electrohydraulic separation device, in particular without the interposition of the mechanical separator (agitator).

[0036] A combination of features analogous to claim 1, however, which does not fulfill the feature of the pre-separation stage, is therefore also considered to be independently inventive. All other advantages and preferred embodiments described here can be combined with this.

[0037] These advantages previously described in connection with wet shredding also apply in particular to the previously described wet pre-separation stage using the mechanical separator.

[0038] The liquid medium is generally preferably water. This is fed to the shredding stage, particularly continuously. The water is preferably discharged from the shredder together with the shredder fraction and fed to the mechanical separator as the wet shredder fraction.

[0039] When water is mentioned here, this means that at least largely pure water is fed into the process, specifically the shredding stage or the pre-separation stage. The water content is at least 98%, preferably at least 99%. The remainder can be, for example, ions, minerals, etc. contained in the water. Tap water, deionized or distilled (pure) water, for example, is used as water. The water fed in preferably has an at least largely neutral pH value, which is therefore preferably in the range between 6.5 and 7.5 and preferably 7.0 + / - 0.2. The process water fed in is therefore not an acid or an alkali.No acid or alkali is added to the water and - apart from the cells or parts thereof to be crushed - no additives are introduced to react with the water, for example to form an acid or alkali.

[0040] The use of normal water allows for a cost-effective, simple process.

[0041] Shredding and / or pre-separation in the pre-separation stage continue to preferably take place at ambient temperature. Neither active cooling by a cooling device nor active heating by a heating device is provided.

[0042] Preferably, a large amount of liquid medium, especially water, is used for the mechanical separator and especially also for the shredding stage. The weight fraction of water is preferably at least 10 times greater, more preferably at least 30 times greater, and especially at least 50 times greater than the weight fraction of the cells or cell parts. This large amount particularly effectively achieves the aforementioned advantages of wet treatment.

[0043] Shredding preferably takes place underwater, meaning the material to be shredded is completely immersed in a water bath. The same preferably applies to further treatment, especially stirring, in the pre-separation stage.

[0044] A total wet shredder fraction is removed from the shredding stage and preferably fed directly to the pre-separation stage and the mechanical separator without further treatment. The ratio of water to the shredded cell fractions is preferably the same as that specified above for the shredding stage. Therefore, process water is preferably constantly fed to the shredding stage and removed again in the same quantity together with the shredded fractions and fed to the pre-separation stage as the wet shredder fraction. As already explained above, due to the wet treatment, discharging the battery and thus the cells is not necessary and, in a preferred embodiment, is not even provided. This eliminates an otherwise required discharge step. Furthermore, depending on the state of charge, this makes it possible to recover a high proportion of lithium directly from the process water.

[0045] In order to easily recover the highest possible lithium content, a practical design provides for the batteries / cells to be brought to a defined state of charge before the battery and cells are shredded, i.e. in particular before the shredding stage. For this purpose, a battery charging process is provided in particular. The defined state of charge is, for example, at least 30%, at least 50%, at least 75% or at least 90% or 100% of a maximum state of charge. The higher the state of charge, the more free lithium ions are present and can be washed out with the process water. State of charge (SOC) is generally understood to mean the current capacity of a battery as a percentage in relation to its maximum capacity. The maximum capacity of a battery indicates the maximum amount of electrical charge that the battery can store. It is typically specified in ampere hours (Ah).

[0046] This measure for recovering lithium is considered to be an independent inventive aspect. The filing of a divisional application is reserved. The essential process steps for this are

[0047] - crushing, especially shredding in wet environments (in process water)

[0048] - -subsequent separation of the process water with subsequent recovery of the lithium.

[0049] In a preferred embodiment, this is done in particular with non-discharged batteries, and in particular—as described above—the setting of a defined state of charge is provided. All other process steps described in this application are combined with this concept individually or in combination in a preferred embodiment.

[0050] As already mentioned several times, the dewatered separator fraction—or, in a variant where the pre-separation stage is omitted, a dewatered shredder fraction—is fed into the aforementioned (first) electrohydraulic separation device in a (first) separation stage. This device generally comprises a bath filled with a liquid medium (process water), into which the dewatered separator fraction is introduced. The separation device is constructed in particular according to DE 10 2019 218 736 A1. It comprises a ground electrode and a high-voltage electrode, which are suitably controlled to generate regular pulse discharges. These not only shred the introduced fraction but also separate the coating material from the film. The process parameters (pulse duration of the pulse discharges, pulse energy, etc.) determine the desired separation.), the coating material can be selectively removed from either the anode foil or the cathode foil. Therefore, in the first separation stage, the corresponding coating material is typically only separated from one of the foil materials. As previously mentioned, this is preferably the anode material, specifically graphite. At the end of the first separation stage, a first separation fraction is obtained.

[0051] In a preferred embodiment, this first separation fraction, which is particularly a wet fraction, is separated into a coarse fraction and a fine fraction. The coarse fraction comprises coarse film particles, while the fine fraction comprises the separated coating material and other fine particles, such as film particles. These components of the fine fraction are particularly present in the process water. The two fractions (coarse fraction and fine fraction) are then further processed separately.

[0052] During this further processing, the two different film fractions of the coarse fraction obtained in the first separation stage are separated from each other. The film fraction that still retains its coating, specifically the cathode foil with the cathode material (e.g., NMC), is fed to a second separation device in a second separation stage. For this purpose, an electrohydraulic (second) separation device is used. This is fundamentally similar or identical to the first electrohydraulic separation device, with only the process parameters preferably being changed and adjusted such that the cathode material is separated from the cathode foil.

[0053] This separates the cathode material, specifically NMC, from the previously separated cathode foil fraction and preserves it in high purity. This material is subsequently recovered from the process water.

[0054] To separate the various components of the first separation fraction, dewatering is preferably provided, especially of the coarse fraction, followed by sorting into the two film fractions. Sorting can generally also be carried out wet without prior dewatering. A centrifuge is preferably used for dewatering the coarse fraction.

[0055] According to a useful development, portions of the fine fraction in the process water and / or the second separation fraction (i.e., anode particles (graphite) and / or cathode particles (NMC)) are fed to a further comminution stage and a (further) comminution device, which is formed, in particular, by an electrohydraulic separation device. A comminuted fine fraction is thereby obtained.

[0056] For example, the parts of the fine fraction or parts of the second separation fraction are fed back to the previous separation stage, in particular to the previous electro-hydraulic separation device. However, these parts are preferably fed to an additional, further comminution device, specifically to a further electro-hydraulic separation device. The parts are in particular the coarse parts of the respective fraction. In order to feed these parts separately from the finer parts to the (further) comminution device, it is preferable to first classify the respective fraction into different size classes, specifically into a coarse fine fraction, a fine fine fraction, and an ultrafine fraction, in order to then feed only the coarser parts, in particular the coarse fine fraction, to the (further) comminution stage and obtain the comminuted fine fraction.

[0057] This design is based on the consideration that the fine fraction of the first separation fraction after the first separation stage (after the first electrohydraulic separation device) or the second separation fraction after the second separation stage (after the second electrohydraulic separation device) still contains comparatively large portions (greater than 50 μm, particularly greater than 250 μm) of the comminuted particles (anode material / cathode material) to which other components are still partially adhering. This is, in particular, a binder, such as PVDF or CMC, which holds the individual particles of the anode / cathode material together. Alternatively or additionally, this is a so-called conductive carbon black, particularly a type of amorphous graphite, which is electrically conductive and ensures that the current is conducted through the coating to the respective foil in the cells. The proportion of the binder or conductive carbon black is, for example, between 2% and 5%.

[0058] The comminuted fine fraction then preferably has a homogeneous particle size, generally preferably less than 50 pm, and in particular less than 40 pm or less than 30 pm. Further comminution removes the undesirable adhering components (binder and conductive carbon black), and the particles of the coating material (anode material, graphite, cathode material, NMC) are obtained in a largely pure form.

[0059] In a preferred embodiment, one or more of the fractions selected from the fine fraction of the first separation stage, the second separation stage, the resulting classified fractions, or the comminuted fine fraction are fed to a subsequent separation stage. Specifically, the fine fraction, or one or more of the resulting classified fractions or the resulting comminuted fraction(s), are fed to the further separation stage. In this stage, different particle types, in particular particles of the anode material and particles of the cathode material, are separated from one another.

[0060] This is based on the consideration and realisation that, especially in the first separation stage, the fine fraction obtained is not sufficiently pure, i.e. the fine fraction contains not only particles of one coating material (typically the anode material, graphite) but also particles of the other coating material (typically cathode material, NMC). The further separation stage therefore further separates the two coating materials from each other.

[0061] Further separation is preferably carried out using a centrifuge or a so-called flotation process.

[0062] It is particularly advantageous if, before this further separation, the fractions have been treated with the (further) comminution device and the comminuted fine fraction has been produced, which is then fed to the further separation stage.

[0063] By means of the further comminution device, the particles are generally crushed to a size as uniform as possible, which simplifies the subsequent separation of the cathode and anode particles.

[0064] As already mentioned, a further (third) electro-hydraulic separating device is preferably used as the (further) comminution device, as already described above.

[0065] Such an electrohydraulic separation device uses shock waves to crush the introduced material and is capable of homogenizing the particle size distribution or separating different (interconnected) particle types from one another. Depending on the treatment duration and / or pulse energy, different fraction sizes result. The preferred post-treatment described here therefore deliberately utilizes this crushing function to achieve the most uniform particle size distribution possible. The thus prepared, homogenized, and crushed fine fraction is then preferentially dewatered, and the different components (particle types) are separated and separated from one another.

[0066] These aspects, on the one hand the downstream comminution by means of the (further) comminution device and on the other hand the downstream further separation stage and in particular their combination, are again considered as independent inventive aspects and the filing of divisional applications on this subject remains reserved. The essential steps for the further comminution stage are

[0067] - feeding the fine fraction obtained from a separation stage to a comminution device, in particular to a further, preferably electro-hydraulic separation and comminution device for producing a comminuted fine fraction,

[0068] - preferably subsequent dewatering and separation of different types of particles in a further separation stage, in particular with the aid of a centrifuge or in a flotation or sedimentation process.

[0069] The essential steps for the next separation stage are:

[0070] - feeding the fine fraction obtained from a separation stage (especially from the first separation stage) to a further separation stage, in particular after dewatering, wherein the further separation stage is formed in particular by a centrifuge or a flotation process,

[0071] - Preferably, the fine fraction obtained from the separation stage is pre-classified into several classified fine fractions, with several and / or each of the classified fine fractions being fed to the further separation stage. In a preferred embodiment, the system has several circuits for the liquid medium, which can also be combined with one another, at least in part.

[0072] Specifically, a first circuit is provided, in which at least the shredder and / or the mechanical separator (stirrer) are integrated. A portion of the graphite, and in particular a portion of the lithium, is contained in the process water of the first circuit and is recovered from it.

[0073] The second circuit includes in particular the first separation stage with the electro-hydraulic first separation device and the third circuit includes the second separation stage with the second electro-hydraulic separation device.

[0074] The last two circuits are preferably coupled to each other, in particular in that the process water from the third circuit is fed to the second circuit and used there and that the process water is purified after passing through the second circuit.

[0075] An embodiment of the invention is explained in more detail below with reference to the figures, which show, in simplified representations:

[0076] FIG 1 shows a partial view of a plant for recycling accumulator cells in the area of ​​a shredder and a stirrer, which are integrated into a first process water circuit,

[0077] FIG 2 shows a partial view of the system in the area of ​​a first electro-hydraulic separating device, which is integrated into a second process water circuit and

[0078] FIG 3 a partial view of the system in the area of ​​a second electro-hydraulic separating device, which is integrated into a third process water circuit

[0079] Figures 1-3 each depict parts of a coherent system 20. Figure 1 shows a first section in which the cells Z to be recycled, in particular lithium cells of a lithium-ion battery, are subjected to pre-shredding and pre-separation.

[0080] In this first subsection, the plant has a shredder 22, a stirrer 24 and a conveyor device 26 as essential components. A liquid medium, referred to here as process water W, is guided in a first circuit K1. Several pumps, valves and collecting or collecting containers 28 are arranged in this circuit K1. Furthermore, FIG. 1 shows a treatment device 30 as a type of black box for treating the process water W and in particular for recovering components of the cells Z. In particular, lithium and / or graphite are recovered by means of this treatment device 30. This device is generally coupled in after screening and / or filtering stages. The screening or filtering stages preferably filter out all particles larger than, for example, 5 pm, before the treatment then takes place with the device.In this process, the remaining microparticles are removed, as well as substances dissolved in the process water, especially (lithium) ions.

[0081] A wet shredder fraction S1 leaves the shredder 22 together with the process water W, which is fed to the agitator 24 and then leaves it as a wet separator fraction S2.

[0082] This is transported by means of the conveyor device 26 in the direction of the second section, which is shown in FIG 2. During transport via the conveyor device 26, which is designed in particular as an inclined conveyor screw, the separator fraction S2 is dewatered.

[0083] This dewatered separator fraction S2 is fed to a first electrohydraulic separation device 32. In this second section of the system 20, graphite G is separated from the shredded anode foils (copper foils CU). The second section of the system 20, downstream of the first electrohydraulic separation device 32, has several components for drying / dewatering, sorting, and classifying the different fractions. The first separation device 32 is a bath filled with process water W, into which the separator fraction S2 is introduced. In this bath, the separator fraction S2 is treated with high pulse energy using shock waves, with the process parameters being set such that the graphite G is separated from the copper foil.The thereby crushed and treated separator fraction S2 leaves the first separation device 32 as a first separation fraction T1, specifically it is pumped out of the bath together with the process water W and fed to a centrifuge 34.

[0084] In the centrifuge 34, dewatering and separation of a coarse fraction C from a fine fraction F takes place. For example, the coarse fraction C contains particles with a diameter greater than or equal to 0.5 cm or greater than or equal to 1 cm. Accordingly, the fine fraction F contains particles smaller than or equal to 0.5 cm or smaller than 1 cm.

[0085] The fine fraction F is subsequently classified and finally dried. For this purpose, the fine fraction F is fed together with the process water W in the exemplary embodiment to a screening device 36. In this screening device, the process water W is separated and a coarse fine fraction F1 and a fine fine fraction F2 are sorted out and classified. The coarse fine fraction F1 comprises, for example, pieces of film with a size of greater than 250 pm and the fine fine fraction comprises graphite or pieces of film with a size in the range of, for example, 50-250 pm. Even smaller components are fed as the finest fraction F3 with the process water W to a filter device 38. From this, the finest fraction F3 is finally obtained, which in particular comprises graphite G with a particle diameter of, for example, less than 50 pm.

[0086] The process water W is conducted in a second circuit K2 in the area of ​​this second section of plant 20.

[0087] The separated coarse fraction C is fed to the third sub-section, as shown in FIG 3. This sub-section is used in particular to obtain NMC, i.e. the cathode material. For this purpose, a second separation device 40 is provided in particular, in which the NMC is separated from the cathode foil (aluminum foil). First, the coarse fraction C is dried in a drying device 42 and then, for example, the various foil fractions are separated from one another in an air classifier 44, namely on the one hand a copper fraction CU, which contains copper foils, and on the other hand an aluminum fraction, which contains the aluminum foils AL that are still coated with the cathode material (NMC). The copper fraction CU also contains the separator foils.

[0088] The aluminum fraction AL is fed to the second electro-hydraulic separation device 40, in which the process parameters are now set such that the cathode material, in particular NMC, is separated from the aluminum foils. Depending on the cell type and cathode coating, other materials are also used and separated accordingly, such as NCA, LFP. The crushed and treated aluminum fraction AL leaves the second separation device 40 as the second separation fraction T2 together with the process water W and is fed to a further filter device 38. In this, the process water W is again separated together with an ultra-fine fraction F3 and a coarse fine fraction F1 and a fine fine fraction F2 are separated. The coarse fine fraction F1 in turn contains particles with a diameter of, for example, greater than 250 pm and the fine fine fraction F2 contains particles with a diameter of between 50 and 250 pm.The fine fraction F2 typically consists of at least highly enriched NMC. The ultrafine fraction F3 also consists of at least highly enriched NMC. This, in turn, is fed with the process water W to a filter device 38, where the ultrafine fraction F3 (NMC) is separated.

[0089] In FIG. 2, at least one further treatment stage, particularly for the coarse fine fraction F1, is indicated by dashed lines following the screening device 36. In a preferred embodiment, this coarse fine fraction F1 is fed to a further comminution stage of a further comminution device, in particular a third electrohydraulic separating device 50. In this device, the particles of the coarse fine fraction F1 are further comminutioned and homogenized. At the same time, any remaining binder components or conductive soot are also separated. A comminuted fine fraction ZF is obtained.

[0090] In addition, another of the classified fine fractions F2, F3, in particular the fine fine fraction F2, can be fed to such a further comminution stage.

[0091] Preferably, this further comminution device is followed by a further separation stage, for example, in the form of another centrifuge 52. In this stage, different particle types, in particular the cathode material, are separated from those of the anode material. After the first separation device 32, NMC fractions of, for example, 10% to 20% are still present in the graphite fraction. This further separation stage therefore achieves improved purity.

[0092] Such an additional separation stage is preferably also provided for one or more or all of the further classified fine fractions F2, F3. These do not necessarily need to be preceded by an additional comminution stage.

[0093] The further comminution stage is alternatively arranged, for example, downstream of the first separating device 32, in particular at a position after separation of the fine fraction F, which is crushed (i.e. before classification) and from which the crushed fine fraction ZF is then obtained.

[0094] Such a further comminution stage is arranged in addition or alternatively to the treatment of the second separation fraction T2 downstream of the second separation device 40, either directly for the treatment of the second separation fraction or - preferably - for the treatment of one or more of the classified fine fractions F1, F2, F3, specifically for the treatment (only) of the coarse fine fraction F1 and possibly also for the treatment of the fine fine fraction F2. Since the second separation fraction T2 is generally already largely pure, a further separation stage is preferably dispensed with here.

[0095] The process water is pumped in a third circuit K3 and thus continuously through the various components of the third section. In the exemplary embodiment, the third circuit K3 is coupled to the second circuit K2. For this purpose, the process water W accumulating in the filter device 38 is fed to the second circuit K2.

[0096] In a manner not shown in detail here, used process water W is fed into a wastewater treatment plant.

[0097] In Annex 20 described here, the following aspects are particularly worth highlighting:

[0098] - Through wet shredding, particularly in combination with wet stirring of the cells Z in the shredder 22 and the stirrer 24, the electrolytes, lithium ions and also a portion of the graphite are separated early on with the process water W and are extracted from the process water W in a simple and efficient manner using the treatment device 30. This means that lithium and graphite with a high degree of purity are already extracted at this point.

[0099] - Preferably, the charge level of the batteries and thus of the cells Z is adjusted in a defined manner (not shown in detail here). In particular, the batteries / cells Z are deliberately electrically charged before shredding. This increases the "free" lithium ion content, so that as much lithium as possible is washed out with the process water W and recovered.

[0100] It should also be emphasized that the use of stirrer 24 already separates a portion of the graphite and recovers it at this point. Furthermore, stirrer 24 separates the otherwise densely packed foils, which is advantageous for subsequent treatment in the electrohydraulic separators 32, 40. Overall, this improves the separation efficiency with regard to separating the coating material from the respective foil in the separators 32, 40, thereby improving the recovery rate. In the system described here, this is typically greater than 90% for NMC.

[0101] - Furthermore, the dewatering of the wet separator fraction S2 before it is fed to the first separation device 32 is noteworthy. This reduces the proportion of free lithium ions in the process water W, which has a positive effect on the operation of the first separation device 32.

[0102] The entire recycling process with the individual process steps (hereinafter A.., B.., C.., D.., E.., W...) as well as the mode of operation, functions and alternatives to the individual components are also outlined in the following detailed, bullet-point description:

[0103] A1 Zerlequnq (vehicle) batteries

[0104] Vehicle batteries are disassembled (manually, semi-automatically or automatically), the modules are removed and the remaining components (housing, cables, electronics) are sorted and recycled separately as material streams.

[0105] A2 Classifying the battery modules

[0106] Battery modules are measured and classified (suitable for second-life applications vs. recycling). Modules to be recycled are further pre-sorted (e.g., by type, chemical composition, and residual charge, if applicable).

[0107] A3 Set the charge level of the battery modules

[0108] According to one variant, modules are largely or completely discharged using a discharge device. The electricity is fed back into the grid or used for the recycling plant. Alternatively, entire vehicle batteries can be discharged without prior disassembly of the modules.

[0109] For this process, however, the charge level is ignored, as the process allows for the recycling of charged batteries, or a defined charge level is set (e.g., the highest possible charge through charging instead of the usual discharging) in order to extract as much lithium as possible. A4 Dismantling / pre-shredding of battery modules manually / semi-automatically / automatically

[0110] The battery modules are disassembled with the goal of separating the individual components (especially the cells, housing parts, and electronic components) with as little mixing as possible. Pure disassembly (removal) steps can be used (e.g., unscrewing, prying open) as well as separation processes (sawing, cutting). The components (including cells) can remain intact or be damaged; the goal is to avoid mixing. Any existing adhesives, conductive pastes, or similar materials can be dissolved using suitable solvents.

[0111] Alternatively, the battery modules can also be shredded in a liquid medium or shredded with very high pulse energy using an electro-hydraulic separation device (e.g. according to DE10 2019 218 736 A1).

[0112] B1 Pre-shredding of battery cells Z in liquid medium (essential aspect)

[0113] Shredding in shredder 22:

[0114] The cells Z are roughly shredded or cut into strips. This exposes the battery foils (anode, cathode) and separates them from the casing, while also washing out the electrolytes, which are largely absorbed into the water.

[0115] Advantages over dry shredding processes:

[0116] (1) No expensive protective gas atmosphere is necessary, since any residual energy present is discharged in the water ==> can be used in industrial plants as process heat for later steps.

[0117] (2) Operation at room temperature (instead of 80°C or more) = energy efficient

[0118] (3) All electrolytes and also conducting salt are safely dissolved in the water (vs. dry process: only the highly volatile gases are well separated, conducting salts and semi-volatile components dry out and are mixed with the black mass; which results in a permanent risk of hydrofluoric acid (HF) formation.

[0119] (4) The electrolytes retain their chemical structure and can later be recycled themselves.

[0120] (5) Fully or partially charged cells can also be treated in this way Discharge step can be omitted

[0121] (6) Lithium is already dissolved in the water at this point and can be recovered. In other processes, lithium remains in the black mass and can only be recovered much later in the process or is lost (in pyrolytic processes).

[0122] (5) + (6) The lithium content in the process water can be adjusted by flow rate and charge state (charged cell Most of the lithium is present as a free ion in the graphite and dissolves in water; discharged cell: most of the lithium is chemically bound in the NMC and remains in the later black mass. This makes it possible to recycle the lithium in advance by charging it beforehand. As an alternative to the traditional shredder, a rotary shear or a guillotine can also be used:

[0123] Cutting or breaking the shell into several large pieces. The goal is to obtain the largest possible fractions in order to ensure the best possible sorting of the shell parts and to lose as little black mass as possible during this step.

[0124] As a further alternative to the classic shredder, the cells are opened automatically by precisely cutting them on one or more predefined sides.

[0125] B2: Pre-sorting of battery cell pieces (optional)

[0126] After pre-shredding in step B1, the material stream consists of the following components:

[0127] (1) Cathode foils made of aluminum with mostly still adhering cathode active mass (e.g. NMC, LFP, etc.)

[0128] (2) Anode foils made of copper with fully or partially adhering anode active mass (usually graphite mixture)

[0129] (3) Separator film

[0130] (4) Housing parts

[0131] (5) Fine fraction (mainly graphite, with smaller amounts of cathode active mass and foil particles)

[0132] In this step, first, the resulting fine fraction is removed and sorted / classified (e.g., by screening, sink-float sorting, centrifugation, magnetic and / or eddy current separation). This occurs in steps D1 and D3. Second, the coarse casing components are removed (e.g., by sink-float sorting, magnetic and / or eddy current separation). The advantage of only coarse shredding in B1 (compared to much finer shredding in other shredding processes): a higher percentage of casing components can be removed.

[0133] C1 Pretreatment of battery cells (electrolyte, anode stripping)

[0134] The shredded or pre-cut cell materials are rinsed or stirred in water for some time (stirrer 24, essential aspect).

[0135] Goals are:

[0136] (1) the separation of the films (still densely packed in the cell, by separating the surfaces of the films are more accessible in the subsequent steps)

[0137] (2) Dissolving / rinsing the electrolyte

[0138] (3) Removal of graphite from the anode foils

[0139] (4) Dissolving / rinsing the lithium

[0140] Advantages 1 to 3 and 5 and 6 from B1 also apply here. Steps B1, B2, and C1 are connected by a common first process water circuit K1. This has the highest concentration of electrolytes and, if applicable, also graphite and dissolved lithium. After step C1, partial dewatering takes place through the conveyor system 26, a screw conveyor with integrated sieve. As a result, the process water W in the following step C2 contains significantly less electrolyte and is also less conductive (since easily soluble components such as lithium ions and, if applicable, unbound heavy metals) are already absorbed in the first circuit. Furthermore, the higher concentration of lithium and electrolytes in this first circuit is advantageous for filtering them out.

[0141] C2 with high

[0142] Steps C2 and D1 to D6 are connected by a shared second process water circuit K2. Advantages 1 to 3 and 5 and 6 from B1 also apply here. However, due to process steps B1 and C1, the concentration of electrolytes, graphite, and lithium in this second circuit K2 is lower. Advantages: The process water W can be circulated for longer periods without intermediate purification; the water circuit represents a second purification stage, so the residual concentration is negligibly low.

[0143] D1 Drainage coarse fraction G

[0144] The coarse fraction C from step C2 (a mixture of mainly cathode foils, anode foils, and separator foils) is conveyed out of the first separation device 32 continuously or discontinuously (and possibly already separated from the fine fraction, but this is not mandatory). Currently, conveying is carried out by means of a conveyor belt, but other methods (e.g., screw conveyor, rinsing with process water) are also possible. The coarse fraction C is pre-dewatered in the centrifuge 34 (various types of centrifuges are possible, both discontinuous and continuous).

[0145] D2 Drying coarse fraction C

[0146] The coarse fraction C is dried in drying device 42. The degree of drying is adjustable and is selected according to the subsequent sorting process. Heat drying, air drying, or other methods (stationary or continuous) are possible. Dewatering D1 and drying D2 are advantageous in the case of dry sorting D3. They can be omitted in the case of wet sorting.

[0147] D3 Sorting coarse fraction (wet or dry)

[0148] Air separation (dry or largely dry, air separation 44). The coarse fraction C is sorted into various fractions (cathode foil, anode foil, separator, casing residues, other) in single- or multi-stage processes. If necessary, subfractions are formed (e.g., different size classes). Intermediate steps may be necessary, e.g., pelletizing of foils, e.g., using an impact mill or similar. Alternatives to air separation are optical sorting (dry or largely dry), magnetic separation, eddy current separation (dry or largely dry), wet sorting processes (sink-float separation, flotation), and magnetic separation or eddy current separation in water.

[0149] D4 Pre-sorting / Pre-dewatering fines from pre-treatment

[0150] The fine particles F of step C2 are discharged continuously or discontinuously by means of the process water W and classified, e.g. by means of a sieve with one or more stages.

[0151] We perform wet screening, but wet separation tables, dry screening (if drying is performed beforehand), centrifugation, hydrocyclones, or similar processes are also possible. These screening stages also serve as pre-dewatering. Combinations of magnetic and / or eddy current separation in a wet medium are also possible, as are sedimentation processes. This results in one or more different fractions of varying grain size and composition.

[0152] D5 Dewatering / Filtration of fines from pretreatment

[0153] The various fractions from step D4 are thickened and further dewatered using filter devices 38 (e.g., vacuum, inclined filter, chamber filter press, or other). Filter cakes are formed for each fraction, the consistency of which can vary with regard to residual moisture (i.e., the filter cake consists of / contains largely the active material of the anode (graphite)).

[0154] D6 Drying / Further treatment of fines

[0155] The various fractions from step D5 are dried. The degree of drying is adjustable and selected according to the customer's requirements. Heat drying, air drying, or other methods are used (stationary or continuous). If necessary, presses or other processes are used to compact and package the material.

[0156] E1 Post-treatment of the cathode foils (cathode stripping)

[0157] The “cathode foils” fraction from step D3 is fed to another shock wave system (2nd separation device 40, with low pulse energy), in which the active material (e.g. NMC, LFP, NCO,..) is separated from the electrode carrier (generally aluminum foil).

[0158] Steps E1 and F1 to F6 are connected by a common process water circuit. Advantages 1, 2, and 6 from B1 also apply here (3, 4, and 5 are no longer relevant because electrolytes and charge were removed in the previous steps). If process steps B, C, and D, or parts of them, are performed beforehand, the concentration of electrolytes, graphite, and lithium in this third water circuit is very low. Advantage: The process water can be circulated for a longer period without intermediate purification.

[0159] E2 Sorting After step E1, the materials are discharged into one or more circuits and separated into different fractions. The goal is, on the one hand, to maximize the concentration of the cathode active material (NMC) in one or more fractions, and, on the other hand, to maximize the concentration of the carrier film (typically aluminum) in other fractions. Wet sieve sorting is preferred, supplemented by centrifugation if necessary. Alternatives include dry sieve sorting, sink-float sorting, flotation, and magnetic sorting (possibly for LFP).

[0160] E3 Pre-dewatering / removal of impurities

[0161] Using centrifuges or other technologies (sedimentation, sink-float process, flotation), any additional impurities are removed from the fractions and pre-dewatering is carried out in the same or subsequent steps.

[0162] To remove impurities, additional (chemical, mechanical) auxiliary agents may be added (e.g., precipitants, caustic soda, or catalytic agents). These substances may also be added in a previous step or at the beginning of the overall wet process (B1).

[0163] E4 Drainage

[0164] The various fractions from step D4 are thickened and further dewatered using filter units (e.g., vacuum, inclined filter, chamber filter press, or other). Filter cakes are produced for each fraction, the consistency of which may vary with regard to residual moisture. If necessary, presses or other processes are used to compact and package the material.

[0165] E5 Drying / Further treatment

[0166] The various fractions from step D5 are dried. The degree of drying is adjustable and selected according to the customer's requirements. Heat drying, air drying, or other methods are used (stationary or continuous). If necessary, presses or other processes are used to compact and package the material.

[0167] W1 Process water post-treatment

[0168] Cycles

[0169] Process water W is the medium used in many of the aforementioned process steps. It is reused in separate and / or coupled circuits. Preferably, process water W from the second separation device 40 (steps (F1, F2...)) is subsequently used in the first separation device 32 (steps (C2, D...)), and preferably subsequently used in the pre-shredding stage (B1, B2) in order to ensure the water can be used for as long as possible.

[0170] A portion of the process water is removed from one or more circuits (continuously or discontinuously) in order to extract and recover the dissolved or suspended valuable substances.

[0171] W2 Process Water Treatment Process water from one or more of the aforementioned circuits K1, K2, and K3 is treated in a multi-stage process. The objectives are:

[0172] (1) To make the process water usable again, and / or

[0173] (2) To make the process water suitable for discharge

[0174] (3) Recover valuable materials

[0175] The cleaning is carried out with regard to suspended and dissolved substances, in particular:

[0176] (1) Metals and heavy metals (e.g. Li, AI, Cu, Ni, Co, Mn, Fe, etc.)

[0177] (2) Other substances (e.g. P, F)

[0178] (3) Organic components (electrolytes, electrolyte salts)

[0179] Possible methods:

[0180] Fine and ultra-fine filtration (ultrafiltration, reverse osmosis, high-performance disc filters, etc.)

[0181] Activated carbon filter

[0182] Other filter materials, e.g. blotting paper, glass fibre fleece, fabrics

[0183] Electrical or electrochemical processes

[0184] Mechanical processes

[0185] Chemical processes (flocculation and precipitation)

[0186] Vacuum evaporation

[0187] Adsorption materials of ceramic origin

[0188] W3 Lithium recovery

[0189] Lithium is recovered from the remaining process water W.

[0190] Advantages of the procedure:

[0191] 1 .The charge state determines how much lithium ends up in the process water W (charged Most of the lithium is present as an ion, i.e. it is dissolved out of graphite and electrolyte; uncharged most of the lithium is bound in the NMC, less is dissolved out)

[0192] 2. Concentration far higher than in natural Li deposits

[0193] Methods:

[0194] Possibly ultrafiltration, reverse osmosis

[0195] Precipitation

[0196] Electrochemical

[0197] W4 Exhaust air purification and material recovery - wet & dry

[0198] The atmosphere above the wet and dry process steps is preferably removed continuously or discontinuously and subjected to measurement and cleaning.

[0199] Goals are:

[0200] (1) Comply with and monitor emissions requirements

[0201] (2) Methods for recovering valuable materials:

[0202] sedimentation

[0203] Activated carbon filtration

[0204] Electrochemical - Chemical

[0205] List of reference symbols

[0206] 20 Appendix

[0207] 22 shredders

[0208] 24 stirrers

[0209] 26 Conveyor system

[0210] 28 collection containers

[0211] 30 processing facility

[0212] 32 first electro-hydraulic separating device

[0213] 34 Centrifuge

[0214] 36 screening device

[0215] 38 Filter device

[0216] 40 second separating device

[0217] 42 Drying device

[0218] 44 wind sifters

[0219] 50 third electro-hydraulic separator

[0220] 52 additional centrifuges

[0221] Z cells

[0222] W Process water

[0223] K1 first circuit

[0224] K2 second circuit

[0225] K3 third circuit

[0226] G Graphit

[0227] 51 Shredder Faction

[0228] 52 Separator fraction

[0229] T1 first separation fraction

[0230] T2 second separation fraction

[0231] C coarse fraction

[0232] F Fine fraction

[0233] F1 coarse fine fraction

[0234] F2 fine fine fraction

[0235] F3 Fine fraction

[0236] ZF crushed fine fraction

[0237] CU copper fraction

[0238] AL aluminum fraction

Claims

Claims Method for recycling battery cells (Z) or parts thereof, which contain electrolytes, in particular lithium, and foils provided with coating material, namely cathode foils with a coating of cathode material and anode foils with a coating of an anode material, wherein - the cells (Z) are mechanically pre-shredded in a shredding stage in liquid medium (W) and a wet shredder fraction (S1 ) is obtained, - the wet shredder fraction (S1) is then rinsed in a pre-separation stage using a mechanical separator (24), in particular a stirrer, under the influence of mechanical energy and using the liquid medium (W), thereby singulating the films and rinsing out components of the shredder fraction (S1), such as electrolyte, coating material and lithium, whereby these components accumulate in the liquid medium (W), and a separator fraction (S2) is obtained in the pre-separation stage. - the separator fraction (S2) is subsequently further processed in at least one separation stage. A method according to the preceding claim, wherein the separator is designed as a stirrer (24) with an agitator in which the shredder fraction (S1) is stirred. A method according to any of the preceding claims, wherein the wet separator fraction (S2) is dewatered, and for this purpose a portion of the liquid medium (W) with the components contained therein is separated, and a dewatered separator fraction (S2) is obtained. A method according to the preceding claim, wherein, for the purpose of dewatering the wet separator fraction (S2), it is conveyed via a conveying device (26) a process according to one of the two preceding claims, wherein components contained in the separated liquid medium (W) are recovered, in particular lithium and the anode material. A process according to one of the preceding claims, wherein the liquid medium is water. A process according to one of the preceding claims, wherein the weight fraction of the liquid medium is at least 10 times, and preferably at least 30 times, or 50 times greater than the weight fraction of cells or parts of cells fed to the shredder stage. A process according to one of the preceding claims, wherein the cells (Z) are not discharged before the shredder stage.A method according to any one of the preceding claims, wherein the cells (Z) are brought to a defined state of charge before the shredding stage, the defined state of charge corresponding to at least 30%, at least 50%, at least 75%, or at least 90% of the maximum state of charge. A method according to any one of the preceding claims, wherein the dewatered separator fraction (S2) is fed to a first electrohydraulic separation device in the separation stage, and at least one of the coatings is removed from the films on which it is applied, in particular the anode material from the anode films, and a first separation fraction (T1) is obtained. A method according to the preceding claim, wherein the first separation fraction (T1) is separated into a coarse fraction (C) containing coarse film fragments and a fine fraction (F) containing the removed coating material, and the two fractions are processed separately. A method according to the preceding claim, wherein anode foils and cathode foils are separated from each other in the coarse fraction (C), and the foil fraction from which the coating material was not separated in the first separation stage is fed to a second separation stage in which the coating material is separated from the foils of this foil fraction, wherein, in particular, a second electrohydraulic separation device (40) is used for this purpose, and a second separation fraction (T2) is obtained. A method according to one of the two preceding claims, wherein at least parts of the fine fraction (F) and / or the second separation fraction (T2) are fed to a further comminution stage, in particular to a preferably further electrohydraulic separation device (50), and a comminution of the fine fraction (ZF) is obtained.A method according to any one of claims 10 to 12, wherein the fine fraction (F) and / or the second separation fraction (T2) is classified into different fine fractions (F1, F2, F3), and at least one of these classified fine fractions (F1, F2, F3) is fed to the further comminution stage to obtain the comminuted fine fraction (ZF). A method according to any one of claims 10 to 13, wherein one of the fractions selected from the fine fraction (F), separation fraction (T2), comminuted fine fraction (ZF), or classified fine fraction (F1, F2, F3) is fed to a further separation stage in which different types of contained particles are separated from one another. A method according to any one of the preceding claims, wherein several separate or interconnected circuits (K1, K2, K3) are provided for liquid medium (W), wherein at least lithium and / or graphite is recovered from the liquid medium (W). A method according to one of the preceding claims, wherein the liquid medium (W) is recycled in a first circuit (K1) via the shredder stage and via a pre-separation stage and back again. A method according to the preceding claim, wherein at least a portion of the liquid medium is fed to a processing unit (30) in which lithium and / or graphite is separated. A system (20) for recycling battery cells (Z) or parts thereof, which comprise an electrolyte, lithium, and films provided with coating material, namely cathode films with a coating of cathode material and anode films with a coating of anode material, wherein - a shredding stage is provided for the mechanical pre-shredding of the cells (Z) in order to obtain a shredder fraction (S1 ), - a pre-separation stage with a separator is provided below, in particular a stirrer (24), for rinsing and separating components of the shredder fraction (S1), such as electrolyte, coating material, and for singulating the films, - a first separation material with in particular a first electrohydraulic separation device (32) is provided in which the separator fraction (S2) obtained in the pre-separation stage is further processed.

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