PLANT AND TREATMENT PROCESS FOR EXHAUSTED AND / OR DISMISSED LEAD-ACID BATTERIES

Description

PLANT AND TREATMENT PROCESS FOR BATTERIES EXHAUSTED AND / OR DISMISSED LEAD-ACID * * * The present invention relates to a plant and a process of 5 treatment of exhausted and / or disused lead-acid batteries, in in particular for the purpose of recovering reusable materials as raw materials secondary and / or to dispose of non-reusable materials in an optimal manner, waste. Lead-acid batteries are still widely used today 10 also in view of their low cost, for example in industry automotive, in industrial handling machines, in agricultural machinery, to allow the starting of the heat engine and power all electrical appliances on board. At the end of their useful life, as in the case of production waste 15 or of accumulators not (or no longer) usable for other reasons, the accumulators lead-acid batteries are subjected to recycling processes to recover the constituent materials of the various components, in particular lead and the electrolyte in addition to other valuable materials, and to enable a optimised disposal of non-recoverable materials. 20 In this description and the attached claims: - unless otherwise specified, when referring to lead-acid batteries it is understood that these are such batteries exhausted and / or decommissioned and electrically substantially discharged; - the term “accumulator” is sometimes used as an abbreviation 25 of “lead-acid battery”; - the adjective “homogeneous” is used to indicate a material comprising a single chemical element or chemical compound or a plurality of chemical elements or chemical compounds having physical characteristics chemicals similar enough to be used as raw materials secondary, following any specific treatment, or possibly from dispose of as waste; - with the expression “heterogeneous material” or “heterogeneous fraction” we it is intended to indicate a non-homogeneous material or fraction; 5 - the verb “com pr end ere” is used in a non-exhaustive sense, so in subject of the verb, in addition to the element or list of elements its complement object, one or more other elements may also be included; - the expression “and / or” is sometimes replaced by the separator bar alone (“ / ”) between the two terms to be considered together or alternatively; 10 - the expressions “avalle” and “am ont e” are intended to refer to the management of the main flow of the material treated in the plant and by these we mean understand that between a device upstream or downstream respectively another one or more additional devices may be included, unless otherwise indicated; 15 - the terms “hydro-separator” and “hydro-separator” are used as synonyms; - the expression “a w a ” is intended to include acidic water, in particular acidified by acids from the battery electrolyte and / or water industrial; 20 - the expressions “upper threshold” and “lower threshold” are used for indicate two thresholds, one greater than the other and therefore respectively one “high threshold” and a “low threshold”, each of which can represent a maximum limit or a minimum limit, depending on the context. The main materials that make up lead-acid batteries 25 are: - contact components, including grids, which form the structure carrier of the electrodes of the individual cells of the accumulator, the poles for the connection to the user and jumpers or “p ont i-polo” ( “p osts” in English), which electrically interconnect the grids of adjacent cells; these 30 components are made of metallic lead alloyed with other elements, typically lead-calcium (Pb-Ca) for grids or lead-antimony (Pb- Sb) for poles and pole bridges; - the active mass covering the grids, typically lead oxide (PbO), lead dioxide (PbO ), pure lead (Pb); 5 - the electrolyte, typically a solution of sulfuric acid (H SO ) in 2 4 distilled water, which can be in liquid form in accumulators traditional, in gelled form in other types of accumulators, or in absorbed in a glass fibre felt in AGM batteries (acronym for Absorbent Glass Mat) which also acts as a separator between the electrodes; 10 - the separators (membranes) placed between the positive and negative grids of adjacent cells; these components are typically made of polyethylene terephthalate (PET) filled with silica and / or textile materials (gauntlet) and / or from fiberglass felt in the case of AGM batteries; - the container or casing of the cells and the relative lid; these 15 components are typically made of polypropylene (PP) or acrylonitrile- butadiene styrene (ABS); - fastening components, typically made of iron or ferrous material and / or ferromagnetic. Treatment of exhausted or discarded lead-acid batteries 20 generally includes their grinding and separation of the product ground into fractions as homogeneous as possible, if not even extraction of individual materials with the highest possible degree of purity. This aim, as already mentioned, to recover reusable materials as raw materials primary secondary and / or to dispose of non-recyclable materials in an optimal manner 25 reusable as waste. As for lead, this is typically recovered, for as regards the above contact components, such as metallic fractions (lead-based), possibly separated according to the size of the particles, as well as, as far as the active mass is concerned, in the form of 30 “pastel”, that is, a mixture containing lead and its derivatives, in particular oxides and sulphates, which can vary from a powdery form to a pasty form. Other fractions that are separated in the treatment of accumulators Spent or discarded lead-acid batteries typically comprise a fraction 5 of electrolyte and one or more polymer fractions, possibly separated into lightweight plastics, which float in the liquid material being treated and heavy, sinking plastics. For both economic and environmental reasons, as well as for reasons of adaptation to some regulations, the quantity and quality of reusable materials that are 10 collected separately in the lead-acid battery recycling process acid should be maximized. The technical problem underlying the invention is to provide a plant, as well as a process, for the treatment of lead-acid batteries- exhausted / discarded acid more efficient in terms of quantity and quality of the 15 secondary raw materials that can be collected separately. The invention concerns, in one aspect, a treatment plant for exhausted and / or disused lead-acid batteries, including: a grinding device configured to receive a plurality of 20 exhausted and / or disused lead-acid batteries and emit a material heterogeneous ground, wherein said plurality of lead-acid accumulators includes Absorbent Glass Mat, AGM, and / or accumulator type batteries with textile separators, a plurality of separating devices, each separating device 25 being configured to receive a respective heterogeneous material of input and extract from it at least two respective output fractions, each output fraction being homogeneous or less heterogeneous than the heterogeneous input material, wherein said heterogeneous input material input is called ground heterogeneous material or is one of the fractions of 30 output of another of said separating devices, wherein at least one of said separating devices comprises a sieve, wherein said system comprises a pressurization device of water and an injector device configured to selectively feed a flow of pressurized water against an exit face of the screen. 5 The Applicant perceived that the “counter-current” washing of the screen (with respect to the flow of material being separated through the sieve) results the detachment of glass wool fibres and / or textile fibres from the separators ground from its mesh wall, fibers that otherwise would clog the screen, thus making it possible to process accumulators 10 lead-acid batteries of AGM type and / or with textile separators in one same system set up for the treatment of accumulators with plastic separators, even the simultaneous treatment of two of these, or of all three different types of accumulators and thus making their separate collection or an operation for their disposal is superfluous 15 separation before introduction into the plant. In this way, the continued operation of the device or devices is also made possible. various separators comprising a respective sieve, and therefore the operation continued operation of the entire system, without the need (or with a reduced need) for plant shutdown to clean the screen(s). 20 This plurality of exhausted and / or discarded lead-acid batteries can also include accumulators with plastic separators. The direction of injection of the pressurized water flow can be between a direction orthogonal to the exit face of the sieve and a direction tangential to the exit face of the sieve, called extreme directions 25 being understood as included in the possible injection directions. The pressure of the pressurized water is preferably greater than 100 bar. Pressurized water can be industrial water from the network and / or recirculated water in the system, preferably recirculated water 30 in the plant. Said at least one separating device comprising a sieve may be chosen from the group consisting of: a lead pastel separator; a lead pastel and metal fraction separator based on lead, derived from contact components; a plastic separator that 5 float in the material being separated; a plastic separator that they sink into the material being separated. The system may also include a power supply device at least one flocculant material at or near said at least one separating device including the sieve. 10 Said at least one flocculant material can be fed directly into the separator device including the sieve and / or into the flow of material immediately upstream of the separation device including the sieve and / or in a device upstream of the device separator including the sieve and / or in the material flow 15 immediately downstream of the separation device comprising the sieve and / or in a device downstream of the separator device comprising the I'm screening. The flocculant material allows the fibres to aggregate into floccules, which due to their greater weight they can sink and be collected, like 20 precipitate or sediment, in the same separator device comprising the sieve or in a device downstream of it. Said at least one flocculant material may comprise a material anionic flocculant and a cationic flocculant material. By providing two such flocculant materials, the advantage is obtained that with 25 the cationic flocculant ionizes the fibers (glass and / or textile); the fact that the fibers are ionized allowing the anionic flocculant material to be more effective in making them aggregate into flocs. Said at least one separating device comprising a sieve, or a second separator device downstream of said at least one device 30 separator comprising a sieve, may be a material separator lead-bearing, in which floccules formed by said flocculant material are collected in the output fraction including lead-bearing material. The Applicant acknowledged that the presence of silica in the glass fibres AGM type battery separators bring advantages in the process 5 metallurgical treatment of lead-bearing material as it promotes the slagging. The Applicant also acknowledged that the presence of fibres textile accumulator separators with textile material bring advantages in the metallurgical process of treating lead-bearing material as provides a non-polluting energy contribution. The forecast, in 10 combination, of the backwashing of the sieves and the addition of at least one flocculant material, in particular a cationic flocculant and one anionic, therefore has the additional advantage of enriching an output fraction lead-bearing with fibres useful for its subsequent treatment, fibres which, Instead, if the sieve were washed off-line, they would be dispersed 15 in the rinse water. In particular, when said at least one flocculant material comprises a cationic flocculant and an anionic flocculant, the cationic flocculant material can be fed into a device upstream of the separator device including the sieve and / or in the flow of 20 material immediately upstream of the separation device including the sieve and / or directly into the separating device including the sieve; the anionic flocculant material may be fed directly into the separator device comprising the sieve and / or in the material flow immediately downstream of the separator device 25 including the sieve and / or in a device downstream of the separator device including the screening. The invention concerns, in one aspect, a process for the treatment of exhausted and / or disused lead-acid batteries, including: grind a plurality of exhausted lead-acid batteries and / or decommissioned, to emit a ground heterogeneous material, in which said plurality of lead-acid accumulators includes accumulators of type AGM and / or accumulators with textile separators, 5 separating said ground heterogeneous material into a plurality of fractions of output, each output fraction being homogeneous or less heterogeneous of ground heterogeneous material, wherein said separating comprises at least a screening of a stream of material through a sieve, and selectively feed a flow of pressurized water against a 10 exit face of the sieve. The invention concerns, in one aspect, a treatment plant for exhausted and / or disused lead-acid batteries, including: a grinding device configured to receive a plurality of 15 exhausted and / or disused lead-acid batteries and emit a material heterogeneous ground, a plurality of separating devices, each separating device being configured to receive a respective heterogeneous material of input and extract from it at least two respective output fractions, 20 each output fraction being homogeneous or less heterogeneous than the heterogeneous input material, wherein said heterogeneous input material input is called ground heterogeneous material or is one of the fractions of output of another of the said separating devices, wherein said system comprises a pressurization device of 25 air and at least one diffuser configured to diffuse compressed air generated by the air pressurization device on at least one of said output fractions of at least one of said separating devices. The Applicant perceived that, through the diffusion of compressed air on the flows of material that is gradually separated from the ground material 30 exhausted / disused accumulators (specifically the fractions that represent secondary raw material or possibly waste), is advantageously possible, even using liquid phase separation techniques, to reduce significantly the residual humidity of this material, avoiding possible contamination by acidic water. Furthermore, this measure makes it possible 5 faster, therefore cheaper and more sustainable, the subsequent treatment metallurgical furnace (in particular, with regard to the fractions lead-based metals derived from contact components and the pastel of lead). Said at least one of said separating devices may be chosen in the 10 group consisting of: a plastic separator; a separator of a lead-based metallic fraction derived from contact components; a lead pastel separator. The system may also include a conveyor device of the type auger downstream of said at least one of said separating devices and the means 15 to spread compressed air may include at least one diffuser in correspondence of the screw type conveyor device. In this case, said at least one separator device can be chosen in the group consisting of a plastic separator device and a elutriation device. 20 The plastic separator device can be chosen in the group consisting of a sink-float device, a hydrodynamic separator and a I'm screening. Alternatively, the diffuser may be provided inside the said at least a separating device. 25 In this case, said at least one separating device can be chosen in the group consisting of a pastel separator device and a device separator of lead pastel and a lead-based metallic fraction derived from contact components. The pastel separator device can be a filter press. The device for separating lead pastel and a metal fraction lead-based derived from contact components can be a screening multi-stage rotary. 5 The invention concerns, in one aspect, a process for the treatment of exhausted and / or disused lead-acid batteries, including: grind a plurality of exhausted lead-acid batteries and / or decommissioned, to emit a ground heterogeneous material, separate said ground heterogeneous material into a plurality of fractions 10 output, each output fraction being homogeneous or less heterogeneous of the ground heterogeneous material, and spread compressed air on at least one of said outlet fractions. The invention concerns, in one aspect, a treatment plant for 15 exhausted and / or discarded lead-acid batteries, including: a grinding device configured to receive a plurality of exhausted and / or disused lead-acid batteries and emit a material heterogeneous ground, a plurality of separating devices, each separating device 20 being configured to receive a respective heterogeneous material of input and extract from it at least two respective output fractions, each output fraction being homogeneous or less heterogeneous than the heterogeneous input material, wherein said heterogeneous input material input is called ground heterogeneous material or is one of the fractions of 25 output of another of said separating devices, wherein a first of said separator devices is configured to extract pastel as one of said respective output fractions, wherein a second of said separating devices is arranged upstream of said first of said separator devices and comprises a settler and 30 an elutriator configured to receive the output fraction as input sedimented in the sedimenter and to extract a metallic fraction from it lead-based as one of said output fractions of said second of called separating devices. The first separator device can be immediately downstream of the 5 second separator device and receive as heterogeneous material of input a fraction of the output of the second separator device, but this it is not strictly necessary. The Applicant perceived that the combination of a downstream elutriator of a sedimentation tank, placed upstream of a paste separator, 10 advantageously achieves the extraction of the lead metal residue or lead alloy, derived from battery contact components, which It has not been separated by previous separating devices. This results in particular possibility to separate very fine particles, very valuable as free from sulphates and other impurities present in the active mass, particles 15 which are usually not extracted separately, but rather flow together in pastel which, due to the aforementioned sulphates and impurities, is a material having a lower metallurgical yield and therefore less valuable. The lead-based metallic fraction can be derived from contact components of lead / acid batteries. 20 The particle size of the lead-based metal fraction may be lower than a pre-set lower threshold. The pre-set lower threshold can be between 0.5 and 4 mm, preferably between 1 and 3 mm, even more preferably 2 mm. One third of said plurality of separating devices may be configured 25 to extract, as one of said respective output fractions, a second lead-based metallic fraction, in which particles of the second fraction lead-based metal have a size greater than one dimension of particles of said lead-based metallic fraction. The second lead-based metallic fraction can be derived from 30 lead acid battery contact components. The said third of said plurality of separating devices may be located upstream of said second of said separating devices. The particle size of the second metal-based fraction lead may be higher than a predetermined upper threshold, greater than 5 one or respectively of the pre-set lower threshold of the size of particles of said lead-based metallic fraction. It is understood that in practice, the second metal-based fraction lead may also include a negligible amount of lead particles dimensions smaller than the pre-set upper threshold. 10 The preset upper threshold can be between 6 and 16 mm, preferably between 8 and 12 mm, even more preferably 10 mm. In case such upper threshold is foreseen, a quarter of said plurality of separator devices can be configured to extract, such as one of said respective output fractions, a third metallic fraction based 15 lead, in which particles of the third lead-based metallic fraction have a size between the pre-set lower threshold and the threshold higher than predetermined. It is understood that in practice, the third metal-based fraction lead may also include a negligible amount of lead particles 20 dimensions below the pre-set lower threshold. The third lead-based metallic fraction can be derived from contact components of lead / acid batteries. The said fourth (388) of said plurality of separating devices may be located upstream of said second of said separating devices. 25 Foreseeing the fourth separator upstream of the above combination of the sedimentation tank and the elutriation tank, a purity is achieved and therefore a very high quality of separated very fine lead powders from the el utria tor e. Said plurality of separating devices may further comprise at least 30 one of: a separator of plastics floating in the liquid material that is treated; a separator of plastics that sink into the liquid material which is treated; an electrolyte separator; a further electrolyte separator pastel. 5 The invention concerns, in one aspect, a process for the treatment of exhausted and / or disused lead-acid batteries, including: grind a plurality of exhausted lead-acid batteries and / or decommissioned, to emit a ground heterogeneous material, separate said ground heterogeneous material into a plurality of fractions 10 output, each output fraction being homogeneous or less heterogeneous of the ground heterogeneous material, wherein said separate includes: separate pastel, let one of the said output fractions settle less 15 heterogeneous of the ground heterogeneous material and elutriate the sedimented material to separate from it a lead-based metallic fraction. The invention concerns, in one aspect, a treatment plant for 20 exhausted and / or discarded lead-acid batteries, including: a grinding device configured to receive a plurality of exhausted and / or disused lead-acid batteries and emit a material heterogeneous ground, a plurality of separating devices, each separating device 25 being configured to receive a respective heterogeneous material of input and extract from it at least two respective output fractions, each output fraction being homogeneous or less heterogeneous than the heterogeneous input material, wherein said heterogeneous input material input is called ground heterogeneous material or is one of the fractions of 30 output of another of said separating devices, wherein said plurality of separating devices comprises: a sink-float device, one of the respective output fractions including plastics floating in the material being separated, a rotary sieve device, the respective heterogeneous material of 5 input being the other output fraction of the sink-float device, one of the respective output fractions being a lead-based metallic fraction, a hydrodynamic separator, the respective heterogeneous material of input being another fraction of output of the rotary screen device, one of the respective output fractions being a heterogeneous fraction 10 including plastics that sink into you. The Applicant perceived that the use of a screening device rotating downstream of a sink-float device allows extraction from the material treated the lead-based metallic fraction, allowing a good operation of the hydrodynamic separator, planned further downstream 15 (i.e., downstream of the rotary screen device) and configured for extract a heterogeneous fraction including plastics that sink into it (e.g. derived from PET separators), as it prevents such particles metals reach the hydrodynamic separator, where they would weigh down too many plastics that sink, preventing effective separation, for 20 example for ascension. The hydrodynamic separator can be configured to extract the heterogeneous fraction including plastics that sink into it via a updraft. The lead-based metallic fraction can be derived from 25 contact components of lead / acid batteries. Particles of the said lead-based metallic fraction may have size less than or equal to a pre-set upper threshold and predominantly higher than or equal to a pre-established lower threshold. This lead-based metallic fraction may therefore include 30 particles having a size between a predetermined lower threshold and a predetermined upper threshold and a negligible amount of particles dimensions smaller than the lower threshold. The pre-set lower threshold can be between 0.5 and 4 mm, preferably between 1 and 3 mm, even more preferably 2 mm. 5 The preset upper threshold can be between 6 and 16 mm, preferably between 8 and 12 mm, even more preferably 10 mm. Another output fraction of the hydrodynamic separator may include also plastics that float in the material being separated. Alternatively or in addition, another fraction of the separator output 10 hydrodynamic may be a second lead-based metallic fraction. The second lead-based metallic fraction can be derived from battery contact components. Particles of the said second lead-based metallic fraction can have a size greater than the pre-set upper threshold. 15 It is understood that in practice, the second metal-based fraction lead may also include a negligible amount of lead particles dimensions smaller than the pre-set upper threshold. Said plurality of separating devices may further comprise a device for separating plastics that sink into the material being processed 20 separate, whose input material is the said heterogeneous fraction including plastics that sink into it. Said plurality of separating devices may further comprise at least one of: a crayon separating device, a crayon separating device electrolyte, a device for separating a third metal-based fraction 25 of lead. The third lead-based metallic fraction can be derived from battery contact components. Particles of the said third lead-based metallic fraction can have a size smaller than the pre-set lower threshold (“par ti ce lle 30 fine ss ime”). The pastel separator device, where provided, can be arranged at upstream of the sink-float device. The electrolyte separator device, where provided, can be arranged upstream of the sink-float device. 5 The separation device of the third lead-based metallic fraction, where applicable, it can be placed downstream of the hydrodynamic separator. The invention concerns, in one aspect, a process for the treatment of exhausted and / or disused lead-acid batteries, including: 10 grinding a plurality of exhausted lead-acid batteries and / or decommissioned, to emit a ground heterogeneous material, separate said ground heterogeneous material into a plurality of fractions of output, each output fraction being homogeneous or less heterogeneous of the ground heterogeneous material, 15 wherein said separation comprises, in sequence: separate by floating-sinking, where by floating plastics that float in the material that is being separated separate, to separate, by means of a rotating sieve, a metallic fraction based on 20 lead, hydrodynamically separate a heterogeneous fraction comprising plastics that sink into you. The implementation of one or more of the above aspects may also include 25 a non-lead-acid battery separator device, arranged to grinder's hill. Alternatively or in addition, the implementation of one or more of the above aspects may also include a metal separator device decommissioned ferrous / ferromagnetic materials, located upstream of the grinder. Alternatively or in addition, the implementation of one or more of the above aspects may include at least one additional grinder configured to grind an output fraction of a separator of said plurality of separators first to feed it as heterogeneous input material to another separator 5 of said plurality of separators. The installation of one or more of the above aspects can be configured to treat batches of exhausted and / or disused lead-acid batteries or to treat a continuous flow of such accumulators. In the process of one or more of the above aspects, separation can 10 occur due to subsequent separations. Alternatively or in addition, in the process of one or more of the aspects the above mentioned can be foreseen at least one further grinding during the separation. 15 Two or more of the characteristics of the various aspects described above may be combined with each other and advantageously a system according to the invention includes features of at least two of the above aspects described and preferably of all the aspects described above. For example, it is possible to predict the diffusion of compressed air from the 20 second aspect at the exit of a sieve type separator device on to which a flow of pressurized water is fed, according to the first I wait. For example, it is possible to predict the diffusion of compressed air from the second aspect at the exit of the reader and of the third aspect and / or at the exit of the 25 sink-float device and / or internally to the rotating screen device of the fourth aspect. In all these cases, the components under consideration can also be fed a flow of pressurized water, according to the first aspect. For example, it is possible to feed, according to the first aspect, a flow of pressurized water on a sink-float device screen and / or on the screen 30 rotating of the fourth aspect, as it is possible to feed such a flow of pressurized water on screen-type separator devices also in association with the use of a sedimenter and an elutriator as in third aspect. In all these cases, it is possible to predict the diffusion of air second aspect compressed at the exit of the third aspect elutriator 5 and / or at the output of the sink-float device and / or internally to the device rotating sieve of the fourth aspect. For example, it is possible to foresee in the same system a plurality of separator devices configured in accordance with the third aspect and configured in accordance with the fourth aspect. Even in all these cases, it is 10 It is possible to predict the diffusion of compressed air from the second aspect at the output of the el ut riator and the third aspect and / or at the output of the sink device- float and / or internally to the rotating sieve device of the fourth aspect. In all the above cases, it is also possible to feed a flow of water pressurized on one of the sieve-type separator devices, according to the 15 first aspect, as an alternative or in addition to the diffusion of compressed air of the second aspect. Preferred characteristics of the plant and the invention process are reported in the dependent claims. 20 Further features and advantages of the present invention will be better understood from the following detailed description of some of its preferred embodiments, made with reference to the attached drawings, in which: - FIG. 1 illustrates a general scheme of a wastewater treatment plant 25 exhausted and / or discarded lead-acid batteries; - FIG. 2-7 and FIG. 8 divided into FIG. 8A, 8B illustrate, each, a diagram of a lead-acid battery treatment plant exhausted and / or decommissioned according to the matter disclosed herein, - FIG. 9 is a reduced version of the system in FIG. 8, on which are 30 highlighted areas of the system diagram according to FIG. 7. Figure 1 illustrates the general scheme of a treatment plant 10 of exhausted and / or disused lead-acid batteries. The plant 10 It includes a grinder 14 which receives the lead-acid batteries 5 exhausted or decommissioned 12. The grinder emits a heterogeneous material ground 16. The system 10 comprises a plurality of separators 18 (the number of three in the figure is purely illustrative and not limiting and at least some aspects innovative products disclosed here can find application in plants or sub- 10 particularly simple systems, in which there is also only one separator) responsible for separating the ground product into fractions 20, 22 outputs as homogeneous as possible, if not even made up of a single homogeneous material (chemical element or chemical compound). In the case of the system shown, the separators 18 are arranged in 15 sequence, whereby the first separator 18A (the most upstream) receives the material heterogeneous ground 16 by the grinder 14 and extracts (at least) a first fraction 20A (“fraction F1” in figure 1), which is a homogeneous fraction, in meaning of the term above, or even a pure material. The first separator 18A emits two output fractions 20A, 22A: the first one 20 fraction 20A and a heterogeneous fraction 22A formed from the remaining material after the extraction of fraction 20A. It is observed that fraction 22A is less heterogeneous of ground heterogeneous material 16. The second separator 18B receives, as heterogeneous material of input, the heterogeneous output fraction 22A of the first separator 18A and 25 extracts (at least) a second fraction 20B (“fraction F2” in figure 1), which is a homogeneous fraction, in the meaning of the term indicated above, or even a pure material. The second fraction 20B separated from the second separator 18B is of a generally different composition than that of the first fraction 20A separated from the first separator 18A. The second separator 18B also emits two output fractions 20B, 22B: the said second fraction 20B and a heterogeneous fraction 22B formed by material remaining after the extraction of the second fraction 20B. It is observed that fraction 22B is less heterogeneous than fraction 22A, and even less 5 heterogeneous of the ground heterogeneous material 16. Similarly, each subsequent separator 18 receives as input a heterogeneous fraction of output from the previous separator 18 and emits (at least) two respective output fractions 20, 22, each output fraction 20, 22 being homogeneous (the respective fraction 20 which is extracted from the 10 material flow), or less heterogeneous than the respective heterogeneous material of input (the respective remaining fraction 22, supplied to the separator next). In the case of the last 18N separator, the (at least) two output fractions 20N, 22N (“Fra tion FN ” and “Fra tion FN + 1 ” in figure 1) can be 15 both homogeneous, in the above meaning of the term, in the case of optimal treatment of exhausted lead-acid batteries and / or decommissioned 12. Each of the output fractions 20, 22 is reusable as raw material first secondary, after any specific treatment, or is it one 20 waste. It is understood that it is advantageous that the waste fraction is also as homogeneous as possible and in particular does not contain valuable materials. In the plant 10, one or more of the separators 18 may perform a multiple separation, i.e. the respective output fractions can be more than two, for example two homogeneous fractions and one fraction 25 heterogeneous subject to further separation in the plant. Such a case does not It is shown for simplicity. Alternatively or in addition, it is possible to foresee, in the system 10, also of the separators 18 in parallel (not shown), i.e. they receive the same heterogeneous input material (from grinder 14 or another of the separators 18) and extract respective output fractions, equal to or different. Such a case is not shown for simplicity. The system 10 may further comprise a separator device 24 non-lead-acid batteries, for detection and removal 5 from the battery system 28 other than lead-acid batteries, in particular lithium-ion batteries, which have been mistakenly disposed of together with the separate collection of lead-acid batteries; such a device 24 may for example be of the X-ray type as described in the Applicant's document WO2021 / 099930A1, here 10 incorporated for reference. Such a device 24, optional in the system 10, is not shown in some of the subsequently described systems for simplicity, but it can be equally predictable. The system 10 may further comprise a separator device 28 disused ferrous / ferromagnetic metals located upstream of the grinder 15 12. Such a ferrous / ferromagnetic metal separator device 28, optional in plant 10, not shown in some of the plants described below for simplicity, but it can be equally expected. 20 In the plant 10 only one grinder 14 is shown, upstream of the separators 18. The plant 10, as well as the plants subsequently described, but may include one or more additional grinders, not shown for simplicity, each configured to grind a 20 output fraction of one of the separators 18 before feeding it, as heterogeneous material of 25 entrance, to another of the separators 18. Plant 10, as well as the plants described below, can be configured to handle batches of spent lead-acid batteries and / or decommissioned 12, or to treat a continuous flow of such accumulators. Figure 2 illustrates the general scheme of a treatment plant 40 of exhausted and / or disused lead-acid batteries. In this case, the treated accumulators are of the Absorbent Glass Mat, AGM, and / or with separators made of textile material, possibly mixed with accumulators with 5 plastic separators. The system 40 includes, in addition to the components discussed above reference to figure 1 and the respective variants, a device of water pressurization 42 and at least one injector device 44 configured to selectively supply pressurized water 10 generated by the pressurization device 42 against an outlet face of a sieve 46 of at least one of said separating devices 18. The direction of injection of pressurized water can be understood between a direction orthogonal to the exit face of the sieve 46 and a direction tangential to the exit face of the sieve 46. The extreme directions above 15 mentioned are intended to be included in the possible injection directions. In figure 2 an injector device 44 is shown at a single separator 18 equipped with sieve 46, but some or all of the separators 18 equipped with a 46 sieve can be equipped with a respective injector device 44. 20 A control unit (not shown) can regulate the cycles of turning on / off the flow of pressurized water intended for or each specific injector device 44 of a specific separator 18, in addition to supervise the flow adjustments, report any malfunctions etc. 25 The water fed to the water pressurization device 42 can be mains water, for example coming from the industrial water network, and / or water recirculated in the system 40. The water pressurization device 42 can be made in any appropriate manner. By way of example and not limitation, 30 it can be formed by a piston pump coupled to a pump priming centrifuge, the latter being connected to a tank of waterfall. The water pressurization device 42 can be connected to the injector device(s) 44 through a suitable system of pipes, valves, 5 control instrumentation, e.g. pressure control, valves safety etc. The pressure of the injected water is preferably higher than 100 bar. As discussed in the introductory part of this disclosure, with the selective injection of pressurized water is performed advantageously 10 “counter-current” washing of screen 46 (with respect to the flow of material in separation through the sieve, symbolized by the arrow 48). This washing results in the detachment of the fibres from the mesh wall of sieve 46 of glass wool and / or textile fibres from ground separators (as well as the detachment of particles of other materials that may have formed 15 stuck in the filter mesh), which would otherwise risk blocking the screening. It is therefore possible to treat AGM type lead-acid batteries and / or with textile separators in the same designated system for the treatment of lead-acid batteries with separators in plastic material, even the simultaneous treatment of these three different 20 types of accumulators (or two of them), which makes their collection unnecessary differentiated or an operation for their separation before the introduction in the plant. Furthermore, the various separators 18 equipped with sieve 46 can remain constantly, or almost constantly, operational – and with them the entire 25 plant 40 – no plant shutdown required for cleaning of the 46 screens, or in any case such need being less recurrent. The separator 18 comprising the sieve 46 may be, for example, a lead pastel separator; a lead pastel and lead pastel separator a lead-based metallic fraction, derived from contact components; 30 a separator of floating plastics in water or more generally in the material being separated (lightweight plastics); a plastics separator that sink in water or more generally in the material being separated (heavy plastics). 5 The system 40 shown may further comprise, as shown schematically, a power supply device (for example, a dispenser) of a flocculant material 50 at or near of (or each) separating device 18 comprising the sieve 46. The flocculant material allows the fibres to aggregate into floccules, which 10 due to their greater weight they can sink and be collected, as precipitate or sediment, in the same separator device 18 equipped with screen 46 or in a device downstream of it, for example in another device separator 18. The flocculant material may include a flocculant material 15 anionic and / or a cationic flocculant material. Predicting two such flocculant materials you get the advantage that with the cationic flocculant you ionize the glass fibers (coming from the battery separators) type AGM) and / or textile fibres (coming from battery separators with textile type separators); the fact that the fibres are ionised allows 20 to the anionic flocculant material to be more effective in making them aggregate in floccules. The formed floccules, instead of being disposed of (which is not the case, by the way) necessarily excluded), can be collected in an output fraction of plant 40 including lead-bearing material. This output fraction 25 comprising lead material can be separated from the same separating device 18 comprising the screen 46 subjected to counter- washing, or from another separator device 18 downstream of it. As discussed in the introductory part of this disclosure, the subsequent metallurgical process for treating lead-bearing material 30 benefits from the presence of fibres collected in the form of floccules – fibres which instead they would be dispersed in the rinsing water if a offline screen washing, with plant shutdown. In fact, glass fibres provide silica, which promotes slagging; textile fibres provide an energy supply, which is also of a non-essential type 5 pollutant. The flocculant material can be fed directly into the separator device 18 comprising the sieve 46 and / or in the flow of material immediately upstream of the separation device 18 10 comprising the sieve 46 and / or in a device (e.g. in another separator) upstream of the separator device 18 comprising the sieve 46 and / or in the material flow immediately downstream of the device separator 18 comprising the sieve 46 and / or in a downstream device of the separator device 18 comprising sieve 46. 15 When both a cationic 50 flocculant material and a 50 anionic flocculant material, then the cationic flocculant material can be fed into a device upstream of the separator device 18 including the sieve 46 and / or in the material flow immediately after upstream of the separating device 18 comprising the sieve 46 and / or 20 directly into the separating device 18 comprising the sieve 46; and the anionic flocculant material can be fed directly into the separator device 18 comprising the sieve 46 and / or in the flow of material immediately downstream of the separator device 18 comprising the sieve 46 and / or in a device downstream of the device 25 separator 18 including sieve 46. Figure 3 illustrates the general scheme of a treatment plant 60 of exhausted and / or disused lead-acid batteries. The plant 60 includes, in addition to the components discussed above with reference to figure 1 30 and their respective variants, an air pressurization device 62 and at least one diffuser 64 configured to diffuse compressed air generated by the pressurization device 62 on at least one of said output fractions 20, 22 (Fraction F1, Fraction F2, …, Fraction FN, Fraction FN+1) of at least one of said separating devices 18. 5 Figure 3 shows a diffuser corresponding to each of the separators 18, but one or more of the separators may be missing diffuser; one or more of the separators 18 could be equipped with more than one diffuser 64, for example one diffuser for each of its fractions of exit. 10 A control unit (not shown) can regulate the pressure, the flow rate, on / off cycles of compressed air flow, etc. intended for the or each specific diffuser 64 of a specific separator 18, as well as supervising the flow adjustments, reporting any malfunctions etc. 15 The air pressurization device 62 can be made in any appropriate manner. By way of example and not limitation, it may include, for example, a rotary compressor. The air pressurization device 62 can be connected to the diffusers 64 through a suitable system of ducts, valves, diverters, 20 control instruments, such as pressure gauges. The diffuser 64 can be arranged, for example, at a screw conveyor device (not shown) provided downstream of the respective separator 18 to convey its output fraction 20, 22 further downstream in the plant 60, for example to convey it to a 25 container of the dried output fraction. According to an alternative, not shown in figure 3 for simplicity, but represented in the figure 4 described below, the air diffuser 64 compressed air can be provided inside the separator device 18 same. As discussed in the introductory part of this disclosure, through the diffusion of compressed air, the various fractions 20, 22 (Fraction F1, Fraction F2, …, Fraction FN, Fraction FN+1) which are gradually separated from the ground heterogeneous material 16 produced by the grinder 14 of 5 exhausted / disused accumulators, specifically those that represent secondary raw materials or possibly waste, are dried at least partially, significantly reducing its residual humidity, which reduces or eliminates the risk of contamination from acidic water. The reduced content of residual humidity also facilitates and speeds up, especially as regards 10 concerns the lead-based metallic fraction derived from the components of contact and lead pastel, the subsequent metallurgical treatment in oven, thus making it more economical and sustainable. The use of compressed air blades via diffusers eliminates most part of the residual moisture of the output fractions of the phase separators 15 liquid, allowing to obtain substantially dry products, where for drying is meant, in this description and in the claims attached, a reduction of the residual moisture content below a pre-set threshold, for example 10% (in standard atmosphere). Experimental tests have shown that it is possible to obtain, for 20 example, a residual moisture content as indicated below: Polypropylene and ABS: ≤3% by weight; PET: ≤30% by weight; metal fraction derived from contact components: ≤ 2% by weight for fine particles and ≤ 8% by weight for very fine particles. 25 Figure 4 shows, by way of example and not as a limitation, a embodiment of a plant 60 with separators 18 on whose fractions of exit 20, 22 it can be particularly advantageous to use a compressed air diffuser 64. Diffusers 64 are shown at the exit of plastic separators, for example 30 example of a separator of plastics floating in the material that is separated (e.g. polypropylene) and a plastic separator that they sink into the material being separated. A diffuser 64 is shown at a separator of pastel. The 64 diffuser is shown, for example purposes only and not 5 limiting, inside the separator 18 itself. This can be, for example, for example the case of a separator device configured as a filter press. 64 diffusers are shown at the exit of fraction separators lead-based metal, derived from contact components, for example three fraction separators having particles of different sizes, indicated in the 10 figures as fine, coarse and very fine, the said terms being comparative among themselves. In more detail: - the adjective “gr ossolane” is used to indicate particles having size greater than a higher threshold, 15 - the adjective “fini” is used to indicate particles having dimensions between a lower threshold and the upper threshold (threshold values included), - the adjective “very fine” is used to indicate particles having a size lower than the lower threshold. 20 It is understood that in practice, the coarse fraction may include even a negligible amount of particles smaller than the threshold size upper and the fine fraction may also include a quantity negligible number of particles smaller than the lower threshold. For example, the upper threshold is between 6 and 16 mm, 25 preferably between 8 and 12 mm, even more preferably 10 mm. For example, the lower threshold is between 0.5 and 4 mm, preferably between 1 and 3 mm, even more preferably it is 2 mm. Preferably the coarse particles have a size between the said upper threshold and the maximum size obtained by the grinder, which for example can be 80 mm. Preferably the very fine particles have a size between 5 0.1 mm and the said lower threshold. It is emphasized that the use of three separators of metallic fractions and in detail of a very fine particle separator is innovative in itself, as will become clear below with reference to figure 5. However, it is not foreseen to use a compressed air diffuser 64 in 10 correspondence of an output fraction comprising the electrolyte, which can for example being the second output fraction of the pastel separator, as shown. The separators 18 are shown in sequence in figure 4 for illustrative purposes only. by way of example and not by way of limitation. 15 It is emphasized, again, that in any form of embodiment the 60 system does not necessarily include a 64 in. diffuser correspondence of each of the fractions shown in figure 4 and above listed. 20 Figure 5 illustrates the general scheme of a treatment plant 80 of exhausted and / or disused lead-acid batteries. The plant 80 includes the components discussed above with reference to figure 1 and the respective variants, but some particularities are highlighted. One of said separators 18, also indicated with the reference 82, is 25 configured to extract pastel as one of said respective fractions of exit 20, 22, here indicated as fraction of exit 84. Another of said separators 18, herein referred to as separator 86, comprises a settler 88 and an elutriator 90 configured to receive inlet the material 92 settled in the settler 88 and to extract 30 from it a lead-based metallic fraction (derived from components of contact of the accumulators), as one of said output fractions of said another separator 18, 86, here indicated as output fraction 94. This 18, 86 lead-based metal fraction separator is placed upstream of the pastel separator 18, 82, but it is not strictly 5 it is necessary that it is immediately upstream, otherwise it is possible that between the two, one or more additional separators are placed between them. As mentioned in the introductory part of this disclosure, thanks to this separator 18, 86 comprising the elutriator 90 downstream of the sedimentation tank 88, located upstream of the separator 18, 82 of the paste, is 10 possible to extract the metallic residue of lead or lead alloy, derivative from contact components of the accumulators, which has not been separated from previous separator devices. In particular, the very fine particles of the ground fraction of contact components represent a material very valuable as they are free from sulphates and other impurities, which are 15 present instead in the active mass and therefore in the pastel. Separating specifically and separately these very fine particles, rather than leaving that are collected in the lead pastel separated downstream, a material having a metallurgical yield superior to that of pastel, therefore of greater value. 20 Even in this context, they can be considered “particles very fine” those having a size smaller than the pre-established lower threshold mentioned above. Among the said separators 18 a separator can also be provided configured to extract, as one of said respective output fractions, a 25 second lead-based metallic fraction, having particle size greater than the particle size of said metal-based fraction lead separated from the elutriator and 90, in particular higher than the said threshold lower predetermined. It is understood that in practice, the second metal-based fraction lead may also include a negligible amount of lead particles dimensions smaller than the pre-set lower threshold. 5 As shown, two such separators 18 may be provided, configured to extract, respectively: - a lead-based metallic fraction having particle size higher than the pre-set lower threshold and lower than an upper threshold predetermined (and a negligible amount of smaller particles 10 at the predetermined lower threshold), here called “fine particles”, - a lead-based metallic fraction having particle size higher than the pre-set upper threshold, here called “parti ce lle coarse”. The upper threshold set may have, in this context too, the 15 values ​​indicated above. These lead-based metal fractions can also be derived from the contact components of the accumulators. These two additional separating devices 18 can be provided for upstream of the separator 18, 86 comprising the elutriator 90 and the 20 sedimenter 88. In plant 80, other separators 18 may be configured to emit, as one of the respective output fractions 20, 22, one or more polymer fractions, specifically, in the case shown, a fraction comprising plastics that float in the liquid material that is 25 treated and a fraction comprising plastics that sink into the material liquid being treated; as well as a fraction comprising electrolyte and / or a further fraction of lead pastel. In Figure 5, all these additional 18 separators are shown upstream of the separator 86 comprising the settler 88 and the ut riat ore 90, but this is not strictly necessary, as long as the conditions are met reciprocal positionings mentioned above. In Figure 5, the various output fractions are shown with some order, but this is purely illustrative and not limiting. When it is 5 also foreseen is the lead-based metal fraction separator having fine particles, upstream of the above combination of settler 88 and elutriator 90 which forms the separator 18, 86 of metal fraction based on lead, a very high purity and therefore a very high quality of the very fine lead powders separated from the elutriator and 90. Figure 6 illustrates the general scheme of a 100 system. treatment of exhausted and / or disused lead-acid batteries. The system 100 comprises the components discussed above with reference to the figure 1 and the respective variants, but some particularities are highlighted. 15 One of the separators 18 is a sink-float device 102, one of the respective output fractions 20, 22, referred to as output fraction 104, including plastics floating in the material being separated, for example polypropylene. One of the separators 18 is a rotary screen device 108, the respective 20 heterogeneous input material being the other output fraction 106 of the sink-float device 102, one of the respective outlet fractions 20, 22, referred to as output fraction 110, being a metal-based fraction of lead. The lead-based metallic fraction 110 can be derived from 25 battery contact components. The particle size of the metal fraction 110 based on lead can be between a pre-set lower threshold and a threshold superior pre-established ( “cell-fine parts”), there being, however, in practice, even a negligible amount of particles smaller than the threshold size lower than the pre-established threshold. These thresholds may also have, in this context, the values ​​indicated above. One of the separators 18 is a hydrodynamic separator or hydro-separator 114, the respective heterogeneous input material being another fraction 5 of the output 112 of the rotary sieve device 108, one of the respective fractions of exit 20, 22, indicated as fraction of exit 116, being a fraction heterogeneous including plastics that sink into it, for example including fragments of battery containers and lids. The hydrodynamic separator 114 can be configured to extract the 10 heterogeneous fraction including plastics that sink into it 116 through an updraft. Another outlet fraction 20, 22 of the hydrodynamic separator 114, here indicated as output fraction 118, may also include plastics that float in the material being separated. 15 Alternatively or in addition, another fraction of output 20, 22 of the hydrodynamic separator 114, herein referred to as output fraction 120, can be a second lead-based metallic fraction. The second lead-based metallic fraction 120 can also be derived from contact components, specifically grids that form a 20 electrode supporting structure of single battery cells, poles and small bridges or “p ont i- polo”. The particle size of the second metallic fraction 120 a lead base may be higher than the pre-set upper threshold (“par ti ce llegr oss ol ane”), there could be, in practice, also a quantity 25 negligible particles smaller than the upper threshold pre-established. Among the separators 18 of the system 100, a 122 plastic separator that sinks into the material being separated (output fraction 124), whose input material is the said fraction heterogeneous including plastics that sink into it 116 and therefore arranged immediately downstream of the hydrodynamic separator 114. Alternatively or in addition, between the separators 18 of the system 100 can a pastel separator 126 (output fraction 128) may also be provided, 5 preferably, but not necessarily, placed upstream of the device sink-float 102. Alternatively or in addition, between the separators 18 of the system 100 can an electrolyte separator 130 (output fraction) may also be provided 132), preferably, but not necessarily, placed upstream of the 10 sink-float device 102. Alternatively or in addition, between the separators 18 of the system 100 can a separator 134 of a third metallic fraction may also be provided lead base (output fraction 136), preferably arranged, but not necessarily, downstream of the hydrodynamic separator 114. 15 The third lead-based metallic fraction can be derived from battery contact components. The particles of the third lead-based metallic fraction 128 can have a size smaller than the pre-set lower threshold (“par ti ce lle very fine”). 20 As discussed in the introductory part of this disclosure, the use of the rotary screen device 108 downstream of the sink-float device 102 allows the extraction of the metal-based fraction from the treated material of lead, for example fine particles of lead-calcium alloy, allowing a good functioning of the hydrodynamic separator 114, expected 25 further downstream (specifically, downstream of the rotary screen device 108) and configured to extract the heterogeneous fraction comprising plastics that sink into it 116. In fact, the rotating sieve 108 prevents that such lead-based metal particles reach the separator hydrodynamic 114, where the sinking plastics would weigh down too much, 30 preventing an effective separation, for example by ascension. As widely indicated in the introductory part of this disclosure, the various measures indicated with reference to the systems of the Figures 2-6, or some of them, can be combined in the same 5 treatment of exhausted and / or disused lead-acid batteries. Figure 7 illustrates the general scheme of a 200 system. treatment of exhausted and / or disused lead-acid batteries, which highlights a possible flow of treated material and possible flows of 10 auxiliary materials, as well as a possible flow of recirculated materials in the plant for further treatment or as auxiliary materials. The 200 plant comprises four areas arranged in sequence and defining the direction of the treatment flow of lead-acid batteries exhausted and / or disused 202: a first area 204, a second area 206, a 15 third area 208, a fourth area 210. Exhausted and / or discarded lead-acid batteries 202 are sent to the first area 204, where they are subjected to preliminary treatment with which, for example: - foreign metals (ferrous and / or ferromagnetic) are removed, which 20 are for example collected in a container 212, - the accumulators are subjected to an initial grinding (pre- crushing) which releases the electrolyte (H SO and HO) (or at least a part of it 2 4 2 preponderant) without changing its concentration, electrolyte which is sifted and filtered and then collected in a container 214 for reuse as 25 secondary raw material (e.g. as pickling product in galvanizing), after any treatment, for example with processes purification or neutralization. The remaining fraction of material, sent to the second area 206, is represented by the over-sieve 216, which includes pastel (PbSO , PbO and 30 PbO ), metallic lead from contact components (Pb-CA, Pb- Sb) and plastics, in particular polypropylene (PP), polyethylene terephthalate (PET) and acrylonitrile butadiene styrene (ABS), as well as possibly glass fibres and / or textile material in the case of accumulators of AGM type and / or with textile separators, in addition to a part 5 of the electrolyte that was not separated in the first area 204. This over-sieve material 216 continues along the direction of flow of treatment, to the second area 206, dedicated for example: - upon extraction of the pastel, collected (after possible filtration) in a container 218 for reuse, for example in new accumulators 10 lead-acid, after specific treatment in a manner known per se, for example a melting treatment to produce pure lead or lead alloys lead and - the extraction of floating plastics, for example polypropylene, collected in a 220 container for recycling as raw materials 15 secondary, subject to any specific treatment in a manner known per se. In the second area 206 a second grinding can take place. In the second area 206, the over-sieve 216 is washed with water 222, so as to allow its treatment in liquid phase, which in general is more advantageous than a solid phase treatment. 20 By “water” is meant to include water acidified by acid contained in the electrolyte. The extraction of the pastel preferably occurs by subjecting it to thickening and filtration. Alternatively or in addition, the pastel can be subjected to a 25 at least partial drying using compressed air as indicated above. The extraction of floating plastics can take place, for example, in sink-float device and / or in the hydrodynamic separator discussed above. In any case, even floating plastics can be subjected to at least partially dried using compressed air as indicated above. The remaining fraction of material 224, sent to the third area 208, includes sinking plastics (specifically polyethylene terephthalate (PET) filled with silica), and metallic lead derived from the components of contact, as well as possibly glass fibres and / or textile materials. 5 Washing with water 222 of the material treated in the second area 206 It also facilitates the release of any residual electrolyte, which for for example, it soaks other materials into the battery. The electrolyte residue 228, which is therefore diluted, is recirculated (after possible filtration) in part to the second area 206 itself, and partly sent to the third one too 10 area 208, subject to possible storage in a container 226. In the third area 208 the extraction of metallic lead takes place, derived from the contact components of the accumulators. Extraction can take place with a classification by size, For example: - extraction of metallic lead having particle size 15 lower than a higher threshold (“par ti c el lefini ”), but typically (and preferably) in prevalence higher than a lower threshold (e.g. lead- calcium), which in practice can also include a quantity negligible of particles smaller than the lower threshold, which is collected in a 230 container for recycling, subject to any 20 specific treatment in a manner known in itself, for example a treatment of fusion and - the extraction of metallic lead having particle size higher than this upper threshold (“coarse particles”) (e.g. lead- antimony), which in practice can also include a quantity 25 negligible particles smaller than the upper threshold pre-established, which is collected in a container 232 for recycling, after any specific treatment in a manner known in itself, for example merger or reduction. Even in this context, the thresholds can have the values ​​indicated above. Separated metallic lead fractions can also be subjected to at least partial drying using compressed air as above, before storage in container 230 and / or in the container 232. 5 The extraction of coarse particles of metallic lead can occur, for example, via the hydro-separator discussed above. The extraction of fine particles of metallic lead can take place, for for example, via the rotary sieve discussed above. The remaining fraction of material 234, sent to the fourth area 210, is 10 mainly represented by plastics that sink in water. When using, in the third area 208, a rotary sieve as above discussed, this allows to recover the remaining residual electrolyte with pastel residue; this material 236 is recirculated from the third area 208 to the second area 206. 15 In the fourth area 210, for example, the following happens: - the extraction of sinking plastics (e.g. silica-filled PET), collected in a container 238 for recycling as raw materials secondary or for eventual disposal as waste, after treatment specific in a way that is known in itself, 20 - when using, in the fourth area 210, a sedimentation tank and a elutriator as described above, the extraction of metallic lead having particle size less than the lower threshold (“par ti ce lle very fine”), collected in a 240 container for recycling, after specific treatment in a manner known in itself. 25 Even sinking plastics and / or very fine lead particles can be subjected to at least partial drying by air compressed as indicated above, before storage in container 238 and / or in container 240. The clarified water 242 in the settler of the fourth area 210, where expected, can be recirculated from this fourth area 210 to the third area 208, specifically to the hydro-separator, if used in such third area 208. When using, in the fourth area 210, an elutriator as above 5 discussed, this allows to recover the remaining residual electrolyte with pastel residue; this material 244 is recirculated from the fourth area 210 to the second area 206. In the system 200 of figure 7 the provision of can be used backwash the various sieves with pressurized water. 10 In the system 200 of figure 7 the provision of can be used add flocculant material, especially a flocculant material cationic and an anionic flocculant material, as indicated above. The various containers can also be replaced, each, by a suitable collection box or be absent and replaced by an 'id on ea area of 15 collection. The various containers (or their variants) shown in the system 200 can be omitted when the respective material is sent directly to a dedicated treatment plant or a waste reuse station same. Figure 8, divided into two figures 8A and 8B, illustrates the scheme of a embodiment of a 300 battery treatment plant exhausted and / or decommissioned lead-acid incorporating all the innovative aspects of the matter disclosed here. 25 The plant 300 includes a magnetic separator / metal detector 304 which receives exhausted and / or discarded lead-acid batteries as input 302 and separates the ferrous and / or ferromagnetic components 306, which are sent for example to a respective container 308 (for recycling or disposal), from the material flow 310, which continues in the plant 300 in a 312 grinder or pre-crusher and which can be, for example, a hammer mill. The ground heterogeneous material 314 continues in the plant 300 in a separator, which may be a vibrating screen 316. The output fraction 318 5 which passes through the vibrating screen 316 substantially comprises concentrated electrolyte (H SO and HO ) and pastel (PbSO , PbO and PbO ), and is 2 4 2 4 2 temporarily stored in a stirred tank 320; subsequently is filtered in a filter 322, which separates the electrolyte 324, stored in a container 326, from pastel 328, which is temporarily stored in 10 a stirred tank 330 and subjected to further treatments described below forward. The collected electrolyte is destined, for example after having been purified or neutralized, to be recycled as secondary raw material or disposed of as waste, as indicated above with reference to figure 7. The other output fraction of the vibrating screen 316, i.e. the above- 15 sieve 332 including among other things metallic lead derived from contact components, plastics and possibly glass fibres and / or textile material (if there are 302 batteries among them) AGM batteries and / or with textile separators), in addition to a part of previously unseparated pastel and electrolyte, continues 20 in the plant or in a second grinder 334, for example a mill hammers, and then, as ground fraction 336, in a separator of the type rotary screen 338. Water 340 is also fed into the grinder 334, preferably water recycled in plant 300 and temporarily stored in a 25 tank 342, and / or clarified electrolyte 344 which is stored temporarily in a container 346, being recovered by a decanter 348 in which it is collected (in addition to other material such as (will say later) the suspension of pastel and electrolyte 350 which is one of the output fractions from the rotary screen 338. It should be noted from now on that the water 340 in the tank 342, being recycled elsewhere in the plant 300 as will be discussed later, can be acidified by the acid contained in the electrolyte; nevertheless in the following refers to water for brevity. 5 In the container 346, the electrolyte is in turn added with water 352, also in this case preferably recycled water in the plant 300 and temporarily stored in the above-mentioned tank 342. In the rotary screen 338, the pastel residue is washed away with a high efficiency, even greater than 90%, using in this case too 10 clarified electrolyte 354 temporarily stored in container 346. The separation meshes of the rotary screen 338 can be subjected to to a backwash with high pressure water 356, for example temporarily stored in a 358 container, to remove the filaments in glass wool fibre and / or textile fibre possibly present in the case of 15 treatment of exhausted / disused batteries 302 of the AGM type and / or with textile separators, possibly mixed with accumulators with plastic separators, filaments that could block the holes of the networks themselves. In figure 8, for simplicity, a device is not shown pressurized water injector. 20 A 360 water pressurization device supplies the water at high pressure 362 in container 358, preferably drawing from nch 'e ss o to the water 364 recycled in the plant 300 and temporarily stored in the tank 342 mentioned above. Alternatively or in addition, the device 360° water pressurization can be fed with mains water 25 365, preferably coming from the industrial water network. As mentioned, the 348 decanter is powered, among other things, by the Paste and electrolyte suspension 350 exiting the rotary screen 338. In the decanter 348, the pastel 366 is collected on the bottom using the high specific weight, and conveyed into the agitated tank 330 above 30 mentioned. Pastel 366 represents one of the exit fractions of the decanter 348, the others being represented by clarified electrolyte 368 sent to the above mentioned container 346 and from clarified electrolyte 370 sent to a separator located further downstream in the plant, described subsequently (elutriator 450). 5 To accelerate the settling speed of the pastel and fibres glass / textiles inside the decanter 348, in or immediately downstream of the rotating screen 338 a device 372 may be provided feeding of a flocculant material, preferably two different ones types of flocculant: anionic and cationic. Preferably, the material 10 cationic flocculant is fed into the rotary screen 338, while the material anionic flocculant is fed downstream of the rotary screen 338, via a another power device, not shown for simplicity. The cationic flocculant material ionizes glass fibers and / or fibers textiles released from the types of lead / acid batteries that contain them; 15 the anionic flocculant material promotes aggregation into floccules and consequently the sedimentation of these fibres. The other output fraction of the rotary screen 338, which is still a rather heterogeneous material 374, is subjected to further processing separation, for example in a sink-float device 376. 20 In the sink-float device 376, the plastics 378 floating in the material that is separated is separated thanks to the lower weight specific, washed and partially dried in a device 380, where Drying takes place, for example, via a compressed air diffuser as indicated above; said dried floating plastics 382 are for 25 example stored in a container 384 for recycling as raw materials secondary, subject to any specific treatment in a manner known per se. The air pressurization device and the supply system of the compressed air to the device 380 and to other points of the system 300, as described below, they are not shown in figure 8 for simplicity. Another fraction of the output 386 of the sink-float device 376, collected on the its background is rather heterogeneous and includes metallic lead derived from from contact components and plastics that sink into the treated material, heavier than those already separated, as well as possibly glass fibres 5 and / or textile material; fraction 386 is sent to a second sieve rotating 388. The sink-float device 376 can also be subjected to control- washing with pressurised water 390 coming for example from container 358 mentioned above. In figure 8, for simplicity it is not 10 shows a pressurized water injector device. The electrolyte solution 392 and any pastel residues in suspension, which represents another of the device's output fractions sink-float 376, is fed to the decanter 348. The second rotary screen 388, for example, consists of four 15 sectors 394, 396, 398, 400. In the first sector 394, the heterogeneous input material coming from from the sink-float device 376 (the output fraction 386 of the latter) is immersed inside an aqueous solution - the water 402 being for example recycled (acidic) water supplied from the above mentioned tank 342- 20 in order to thoroughly remove any pastel still present. In the second sector 396, a fraction of exit 404, comprising pastel together with electrolyte, is drained and, for example, collected in a agitated tank 406, to be fed to the decanter 348. The material from which the output fraction 404 has been washed away is 25 subject to partial drying, for example through a diffuser 408 of compressed air as discussed above, before being transferred to the third sector 398. In the third sector 398 the metallic fraction 410 is separated lead whose particles have a size smaller than a predetermined threshold 30 higher and, typically, predominantly, size above a threshold prefixed lower (“celluloid parts”), thus being able to include, in the in practice, even a negligible amount of smaller particles at the pre-set lower threshold. For example, fraction 410 is stored in a 412 container for recycling, after any treatment 5 specific in a manner known per se, for example, a fusion treatment as described above with reference to figure 7. From the fourth and final sector 400 the remaining material comes out, which is a still quite heterogeneous fraction 414, including among others the metallic lead from contact components and plastics that 10 sink into the treated material, as well as possibly the glass fibres and / or of textile material. The second rotating screen 388 can also be subjected to check- washing with pressurised water 416 coming for example from container 358 mentioned above. Again, for simplicity's sake, I do not 15 shows a pressurized water injector device. The heterogeneous fraction 414 continues in plant 300 to a separator hydrodynamic or hydro-separator 418. In the hydro-separator 418, any plastics 420 that float in the material that is separated, escapes separation in the sink-device 20 float 376, are recovered and sent to the washing device and drying 380 mentioned above, to then be collected in the container 384 mentioned above. The lead-based metallic fraction 422, arising from the contact components (e.g., Pb-Sb), collected on the bottom, is extracted and collected for example in a 424 container. It can 25 a material feeding device 426 be provided flocculant to the hydro-separator 418 to facilitate the collection of such waste on the bottom materials. The heterogeneous fraction of output 428 containing sinking plastics in the material being separated, separated in the hydro-separator 418 via an upward current, continues in the plant 300 in a separator of the sieve type 430. In sieve 430, the plastics that sink into the material that is separated 432 are separated, they can be subjected to drying 5 for example via a compressed air diffuser 434 as indicated above, and the 436 plastics that sank and were dried are collected in a container 438. The 430 screen can also be backwashed with water under pressure 440 coming for example from container 358 above 10 mentioned. Again, for simplicity, no one is shown. pressurized water injector device. The liquid fraction 442 which drains into the sieve 430, and which carries the residual lead-based metallic fraction, originating from the components of contact, having very small particle size, which can be 15 escaped separation in the rotary sieve 388, and the pastel residue of lead, continues in the plant 300 in a sedimentation tank 444. Also in in this context, particle size can be considered lower than a pre-set lower threshold for which the values ​​apply numbers indicated above (“parti cel le fini ssi me”). 20 To accelerate the sedimentation rate inside the sedimentation tank 444, a feeding device 446 may be provided of a flocculent material in the sieve 430 and / or in the settler 444. When, for the reasons discussed above, both a material are used cationic flocculant is an anionic flocculant material, the material 25 cationic flocculant can be inserted into the 430 screen, where it ionizes the fibers glass and / or textile fibres released from lead / acid types of batteries which contain them; the anionic flocculant material is subsequently inserted into the sedimentation tank 444, where it promotes aggregation into floccules and consequently the sedimentation of these fibres. The fraction 448, still heterogeneous, settled in the sedimentation tank 444 continues in the 300 plant in a 450 elutriator, while the liquid fraction 452 is recirculated to the hydro-separator 418, where it dilutes the fraction 414 which comes to you from the second rotating sieve 388 after partial drying 5 via the compressed air diffuser 408. The lead-based metallic fraction 454 with size of particles below the lower threshold are collected on the bottom in the 450 elutriator, it can be dried at least partially, for example through a compressed air diffuser 456 as indicated above, and the fraction 10 dried 458, very valuable for the reasons above, is collected in a 460 container for recycling, subject to any specific treatment in a manner known in itself, for example a fusion treatment. In the 450 elutriator the pastel is also separated, by means of of the clarified electrolyte 370 coming from the decanter 348 as above 15 mentioned, and thanks to the internal agitation of the 450 eluter itself; such fraction 462 comprising paste and electrolyte is recirculated in the decanter 348. As described above, the pastel is collected in the agitated tank 330 separated into several points of the 300 system, therefore with high efficiency. 20 Paste 464 taken from the stirred tank 330 is filtered into through a 466 filter, specifically a filter press, which separates the liquid fraction 468 which feeds the (acidic) water tank 342 process, recycled in plant 300 as described above, for replenishment of the operational level of some components. 25 Recycled acidic process water can also be used for different uses, for example for washing lines. The accumulated and dehydrated paste in the filter press 466 can be dried to reduce its residual humidity, via a 470 air diffuser compressed as indicated above, and possibly squeezed, for example 30 by equipping the filter with a squeezing device not shown. The dried pastel 472 is collected in a container 474 for the reuse in new lead-acid batteries, after specific treatment in a manner known in itself, for example a fusion treatment for produce pure lead or lead alloys, as above indicated with 5 refer to figure 7. In figure 8, a possible identification device is omitted and removal from the plant of accumulators other than batteries lead-acid, which can be foreseen upstream of the separator magnetic / metal detector 304. 10 In the 300 system there may be a system for removing the acid fumes, not shown for simplicity. Figure 9 is a scaled-down version of the setup in Figure 8 above. described, on which the four areas 204, 206, 208, 210 of the 15 system diagram according to figure 7 described above. The various alternative embodiments, variants and / or possibilities of each component or group of components that have been described must be understood as combinable with each other in any way, unless 20 that are not incompatible with each other. The above is a description of various embodiments of aspects inventive, and further changes can be made without going out of from the scope of the present invention. The shape and / or size and / or position and / or orientation of the various components and / or the succession of the 25 different phases can be varied. The functions of an element or module can be performed by two or more components or modules, and vice versa. Components shown directly connected or in contact may have intermediate structures arranged between them. Phases shown directly subsequent phases may have intermediate phases carried out between them. The details 30 shown in a figure and / or described with reference to a figure or a embodiment can be applied in other figures or forms of realization. Not all details shown in a figure or described in the same context must necessarily be present in the same embodiment. Features or aspects that are innovative. 5 compared to the prior art, alone or in combination with other features, are to be considered described in themselves, regardless of how much explicitly described as innovative. 10 Barzanò & Zanardo Milano SpA

Claims

1. A plant (80; 200; 300) for the treatment of spent and / or disused lead-acid batteries, comprising: a grinding device (14; 312) configured to receive a plurality of spent and / or disused lead-acid batteries (12; 202; 302) and emit a ground heterogeneous material (16; 314), a plurality of separator devices (18; 82, 86; 316, 322, 338, 348, 376, 388, 418, 430, 450, 466), each separator device (18; 82, 86; 316, 322, 338, 348, 376, 388, 418, 430, 450, 466) being configured to receive a respective heterogeneous input material and extracting therefrom at least two respective output fractions (20, 22; 84, 94; 366, 448, 454), each output fraction (20, 22; 84, 94; 366, 448, 454) being homogeneous or less heterogeneous than the heterogeneous input material, wherein said heterogeneous input material is said ground heterogeneous material (16; 314) or is one of the output fractions (20, 22; 84, 92, 94;366, 448, 454) of another of said separating devices (18; 82, 86; 316, 322, 338, 348, 376, 388, 418, 430, 450, 466), wherein a first (82; 348) of said separating devices (18; 82, 86; 316, 322, 338, 348, 376, 388, 418, 430, 450, 466) is configured to extract pastel (84; 366) as one of said respective output fractions (20, 22; 84, 92, 94; 366, 448, 454), wherein a second (86) of said separating devices (18; 82, 86; 316, 322, 338, 348, 376, 388, 418, 430, 450, 466) is arranged upstream of said first (82; 348) of said separator devices (18; 82, 86; 316, 322, 338, 348, 376, 388, 418, 430, 450, 466) and comprises a settler (88; 444) and an elutriator (90; 450) configured to receive as input the output fraction (20, 22; 92; 448) settled in the settler (88; 444) and to extract therefrom a lead-based metallic fraction (20, 22; 94; 454) such as a of the said output fractions (20, 22; 84, 92, 94;366, 448, 454) of said second (86) of said separating devices (18; 82, 86; 316, 322, 338, 348, 376, 388, 418, 430, 450, 466). Barzanò & Zanardo Engitec Technologies SpA A141393; 2. a battery (80; 200; 300) according to claim 1, wherein the lead-based metallic fraction (20, 22; 94; 454) is derived from contact components of lead / acid batteries.

3. The system (80; 200; 300) according to claim 1 or 2, wherein the particle size of the lead-based metal fraction (20, 22; 94; 454) is less than or equal to a predetermined lower threshold.

4. The implant (80; 200; 300) according to claim 3, wherein the predetermined lower threshold is between 0.5 and 4 mm, preferably between 1 and 3 mm, even more preferably it is 2 mm.

5. The plant (80; 200; 300) according to any of the preceding claims, wherein a third (418) of said plurality of separator devices (18; 82, 86; 316, 322, 338, 348, 376, 388, 418, 430, 450, 466) is configured to extract, as one of said respective output fractions, a second lead-based metallic fraction (422), wherein particles of the second lead-based metallic fraction (422) have a size larger than a particle size of said lead-based metallic fraction (20, 22; 94; 454).

6. The system (80; 200; 300) according to claim 5, wherein said third (418) of said plurality of separator devices (18; 82, 86; 316, 322, 338, 348, 376, 388, 418, 430, 450, 466) is arranged upstream of said second (86) of said separator devices (18; 82, 86; 316, 322, 338, 348, 376, 388, 418, 430, 450, 466).

7. The system (80; 200; 300) according to claim 5 or 6, wherein the particle size of the second lead-based metallic fraction (422) is greater than a predetermined upper threshold, greater than a or respectively the predetermined lower threshold of the particle size of said lead-based metallic fraction (20, 22; 94; 454).

8. The plant (80; 200; 300) according to claim 7, wherein a fourth (388) of said plurality of separator devices (18; 82, 86; 316, 322, 338, 348, 376, 388, 418, 430, 450, 466) is configured to extract, as one of said respective output fractions, a third lead-based metallic fraction (410), wherein particles of the third lead-based metallic fraction (410) have a size between the predetermined lower threshold and the predetermined upper threshold.

9. The system (80; 200; 300) according to claim 8, wherein said fourth (388) of said plurality of separator devices (18; 82, 86; 316, 322, 338, 348, 376, 388, 418, 430, 450, 466) is arranged upstream of said second (86) of said separator devices (18; 82, 86; 316, 322, 338, 348, 376, 388, 418, 430, 450, 466).

10. A process for treating spent and / or discarded lead-acid batteries, comprising: grinding a plurality of spent and / or discarded lead-acid batteries to emit a ground heterogeneous material, separating said ground heterogeneous material into a plurality of output fractions, each output fraction being homogeneous or less heterogeneous than the ground heterogeneous material, wherein said separating comprises: separating the paste, allowing one of said output fractions to settle that is less heterogeneous than the ground heterogeneous material, and elutriating the settled material to separate therefrom a lead-based metallic fraction.