Method and industrial plant for separating waste materials

Abstract

The present invention relates to a method and industrial plant for separating waste (1) containing at least one metal (2) and at least one organic matter (3). Separated fractions (4) of the waste (1) are provided, separated from the waste (1) during mechanical processing. The separated fractions (4) include briquettes (5) made from the waste (1) and, optionally, coarse fractions (6) of the waste (1) or another waste (7). The separated fractions (4) have a calorific value of 5 MJ / kg to 30 MJ / kg and a maximum copper content of 0.1% to 20% by weight. The separated fractions (4) are continuously or discontinuously charged into a reactor (8) where they are combusted. The separated fractions (4) are then melted into at least one liquid slag phase (10) and a liquid metal-containing phase (11). At least a portion (12) of the incompletely combusted flue gas (13) is conducted from the reactor (8) and introduced into a thermal secondary combustion plant (14) where the portion (12) is subjected to secondary combustion.

Description

[Technical Field]

[0001] The present invention relates to a process for separating waste materials and to an industrial plant for carrying out such a process. [Background technology]

[0002] Various types of waste can be mechanically processed, for example in shredding plants, and separated into reusable or recyclable fractions. The resulting fractions, i.e. the shredder light fraction (SLF) and the shredder heavy fraction (SHF), can be separated into recyclable material streams and subsequently treated in a treatment process, which can then be returned to the recyclable material cycle.

[0003] However, both SLF and SHF always leave residues with a relatively low content of valuable materials, especially metals. Methods for treating these shredder residues are known in the industry. However, these methods are not very satisfactory from an economic point of view, especially because the composition of shredder residues varies widely in terms of quality and composition. Therefore, shredder residues are usually returned to a thermal energy plant (TVA) for incineration or landfill.

[0004] Conventionally, in particular light shredder fractions, as examples of heavy metal-containing residues from crushing plants or other wastes with a high proportion of organic and mineral components and a low proportion of metals, have been disposed of in landfill construction, mine backfilling, waste incineration plants, etc. However, this method does not allow for the recovery and reuse of some valuable components of this waste.

[0005] However, these solutions are contrary to the spirit of sustainable economics and therefore have limited satisfaction, especially since metals that would normally have to be recovered at a cost are lost forever through incineration or landfill without being returned to the circulation of valuable materials.

[0006] In order to be able to partially or as completely as possible reuse the raw materials contained in such waste, it is necessary to selectively separate these materials as purely as possible from the waste, which is particularly important for heavy metals, and especially precious metals, in order to return the raw materials to the material cycle. Conventional disposal methods, in particular waste incineration plants, are not suitable for this. The result of waste incineration is that, due to its structure, it is impossible to separate the components.

[0007] Although methods for recovering metals from primary and secondary raw materials in metal smelters are known in principle, the known methods do not allow for the ecologically and economically satisfactory treatment of waste fractions with high inputs and relatively low metal contents. This is particularly the case when the metal traces are in finely divided materials. In particular, fine residues with low metal contents and a high degree of amalgamation, such as those from shredder residues (so-called tertiary waste, i.e. waste that forms residues or residues remaining after multiple treatment stages) generated, for example, in the processing of waste electrical and electronic equipment, cannot currently be satisfactorily recovered. Summary of the Invention [Problem to be solved by the invention]

[0008] The object of the present invention was to provide a method and an industrial plant for separating waste materials which overcome the drawbacks of the prior art and which allows for ecological treatment and, in addition, economical recovery of valuable materials. [Means for solving the problem]

[0009] The above-mentioned problem is solved by a method and an industrial plant as set forth in the claims.

[0010] The present invention relates to a method for separating waste materials, the waste materials comprising at least one metal and at least one organic material. The waste materials may be residues containing at least one metal resulting from mechanical processes, such as residues from the processing of electrical and electronic scrap or shredder residues. The organic materials may be, for example, any type of plastic, any organic material that cannot be composted, but also any type of cellulose-containing material, such as wood or natural fibers. The organic materials may be, for example, epoxy resins, which are components of electronic waste.

[0011] According to the method, separated waste fractions are provided, which contain at least one metal and at least one organic material separated from the waste during mechanical processing. The mechanical processing may be performed in a single stage or multiple stages, for example, in a crushing plant or in a plant downstream of the crushing plant. The separated fractions include briquettes made essentially from the waste and, optionally, coarse waste fractions or coarse waste fractions of another waste. Preferably, the material used for briquetting or briquetting consists primarily of fine material. The term briquette is well known in the art to mean a compact pressed from fine material, and therefore a detailed definition will not be provided here. The coarse fractions may originate from the same waste as the briquettes. However, it is also conceivable that the coarse fractions are fractions of another waste, such as electrical and electronic equipment scrap, scrap metal, plastic waste, or coarse fractions resulting from automobile processing. The term coarse material here refers to material that is coarse compared to the fine briquetting material and that is impossible or difficult to briquette. Advantageously, the coarse fragments may have a higher proportion of valuable materials, especially iron, as well as non-ferrous and precious metals, compared to the briquettes, so that adding a certain amount of coarse fragments makes the separation process more economical. In this case, it may be useful if the metal content, especially the copper content, and / or calorific value of the briquettes and the coarse fragments are known. These parameters, in particular, can be measured or checked continuously or discontinuously at suitable intervals. Such continuous quality control can be carried out, for example, using a central control, regulation, and measurement system.

[0012] The separated fractions have a calorific value of 5 MJ / kg to 30 MJ / kg and a maximum copper content of 0.1% to 20% by weight. Quality control of the separated fractions can also be carried out, for example, by means of a control, regulation and measurement system. If at least the calorific value and copper content parameters of the briquettes and coarse fractions are known, the separated fractions can be processed or melted particularly precisely and efficiently in a reaction plant or reactor, in particular a melting furnace.

[0013] In the next process step, the separated pieces are continuously or discontinuously charged into a reactor. An oxygen-containing gas, i.e., combustion air, is then introduced into the reactor as an oxidant, and the separated pieces are oxidized or burned in an incomplete combustion process, whereby the reaction or melting occurs self-heating, ideally without additional fuel. Because the separated pieces have a high calorific value, process control by incomplete combustion or oxidation is important, thereby protecting the reactor from overheating and thermal collapse and the resulting damage.

[0014] The separated fragments are melted into at least one liquid slag phase and at least one liquid metal-containing phase using the thermal energy generated during combustion of the separated fragments. Initially, an emulsion-like mixture of phases, known as the mixed phase, is formed. It has been shown that incomplete combustion is sufficient to melt the separated fragments. During the melting process, the separated fragments can be melted at temperatures of approximately 1220°C to 1250°C.

[0015] At least one slag phase and / or at least one metal-containing phase are drained from the reactor. This can be done separately, for example, by first separating the at least one slag phase after a certain time required for gravity phase separation, followed by separating the at least one metal-containing phase. However, it is also possible to remove the phases together, i.e., as a mixed phase, from the reactor and transfer them to a separation furnace for gravity separation.

[0016] In a further method step, at least a portion of the incompletely burned flue gas is led out of the reactor and introduced into a thermal secondary combustion plant for secondary combustion of at least a portion of the incompletely burned flue gas. The thermal secondary combustion plant can essentially comprise a secondary combustion boiler having one or more subsections. This pyrometallurgical process can be performed cyclically, with the batch period being approximately the same length as the melting cycle in the reactor. This type of process management also results in cyclical heat loads from the reactor, which must be compensated for by adding secondary or supplemental fuel to the secondary combustion boiler to ensure stable operation of the waste heat recovery plant, if any, that follows the thermal secondary combustion plant.

[0017] The method has the advantage that large quantities of material streams with a relatively low content of valuables, in particular copper, can be treated in an ecological manner while at the same time recovering the copper components economically, which is made possible, inter alia, by the process control according to the invention and the precise adjustment of the calorific value and copper content of the separated fractions.

[0018] It is noted here that the individual method steps and their chronological order do not necessarily have to be performed in the order described, and a different chronological order is also possible, however it is preferred that the described method steps are performed consecutively and thus in a successive chronological order.

[0019] Essentially, three main valuable streams are recovered from the separated fractions or waste materials used in this process: at least one liquid metal-containing phase or metal alloy, at least one liquid slag phase, and usable waste heat. The alloy can then be processed into valuable metals up to pure copper. The slag phase can also be processed similarly, particularly if qualitatively improved with additives, and granulated for use in concrete, for example, as a latent hydraulic binder. Alternatively, the slag phase can also be used in road construction or as a sandblasting agent. Since the processed slag phase is at least substantially free of hazardous substances and valuable materials, it can also be considered for landfilling at a low landfill level. The waste heat generated in the process can be converted into electricity, for example, in a waste heat recovery plant, and used to supply local and / or remote heat supply networks.

[0020] Furthermore, it may be useful if the waste contains at least one mineral and / or if a mineral slag-forming agent is added to the separated fraction. The presence of minerals in the waste or separated fraction, as well as the addition of additional mineral slag-forming agents as additives, can promote the formation of a slag phase with a suitable viscosity, thereby favorably influencing separation from the metal phase. The additives can be added to the separated fraction or directly to the reactor as it enters the reactor.

[0021] Furthermore, the separated fractions can be provided with a calorific value of 8 MJ / kg to 25 MJ / kg, preferably 11 MJ / kg to 18 MJ / kg, which has proven to be particularly useful for precise and efficient process control.

[0022] Furthermore, it is possible to provide separated fractions with a maximum copper content of 0.3% to 10% by weight, preferably 0.5% to 3% by weight, which has proven particularly useful for precise and efficient process control.

[0023] Also advantageous is an embodiment in which briquettes are provided with a calorific value of 5 MJ / kg to 30 MJ / kg, preferably 8 MJ / kg to 25 MJ / kg, particularly preferably 11 MJ / kg to 18 MJ / kg. This calorific value has proven to be particularly useful for precise and efficient process control. This can have a decisively positive impact on process control, especially if the calorific values ​​of the separated pieces and of the briquettes themselves are known or precisely adjusted.

[0024] In a further development, briquettes can be provided that contain fine fragments and / or fluff fragments. Advantageously, particularly fine material streams are used for processing into briquettes. This allows for precise adjustment of the calorific value and copper content, and also facilitates charging into the reactor.

[0025] Fine fragments can have components primarily with a maximum particle size of less than 15 mm, preferably less than 10 mm. The term "fine fragments" is known in the field of mechanical waste processing and refers to fragments consisting of sand and other small particles produced during single-stage or multi-stage mechanical waste processing. Therefore, fine fragments are often a mixture of glass, fine iron, rust, thin copper wire, lead- and zinc-containing dust, plastic particles, fluff, paint residue, etc. Fine fragments are typically relatively light, requiring significant storage and transportation space. Their calorific value is typically in the range of 5 MJ / kg ± 5 MJ / kg. Furthermore, fine fragments can contain a high proportion of oxidizing substances, which can be used as slag formers in subsequent melting processes. Fine fragments can have an iron content of up to 20% by weight. Furthermore, fine fragments can contain 5% by weight of non-ferrous metals (e.g., copper, zinc, gold). According to the classification of the Austrian Waste Cataloging Ordinance, or OeNORM S 2100 "Waste Cataloging", section 5, table 1, fine fragments fall under key number SN 91103 for residues of mechanical treatment. This classification also applies correspondingly to this type of material outside Austria, even if the material is not classified as waste.

[0026] The term fluff fragments (Flusenfraktion) or fluff (Flusen) is known in the mechanical processing of waste and refers to a mixture of lightweight, porous, and / or fibrous materials (e.g., textile fibers, foams, wood or cellulose, foils) produced during single- or multi-stage mechanical waste processing. The calorific value of fluff fragments is typically in the range of 22.5 MJ / kg ± 10 MJ / kg, and is therefore often significantly higher than that of fine fragments. Fluff fragments may also contain lead, zinc, and / or chlorine compounds. Fluff fragments may contain up to 6% iron. Furthermore, plastic fragments may contain up to 5% by weight of non-ferrous metals (e.g., copper, zinc, gold). According to the classification of the Austrian Waste Cataloging Ordinance, or OeNORM S 2100 "Waste Cataloging," Section 5, Table 1, fine fragments fall under key number SN91103 for residues of mechanical processing. This classification also applies correspondingly to materials of this type outside Austria, even if the material is not classified as waste.

[0027] However, it is also possible to add plastic fragments to the separated fractions, particularly briquettes. In this case, the plastic fragments can be, for example, fragments from a crushing plant. Typically, plastic fragments include solids, chunks, or rounded pieces generated during mechanical waste processing operations. Typically, the calorific value of plastic fragments is in the range of 18.5 MJ / kg ± 10 MJ / kg. Plastic fragments may also contain a high proportion of chlorine compounds. Plastic fragments may have an iron content of up to 5% by weight. Furthermore, plastic fragments may contain non-ferrous metal components (such as copper, zinc, or gold) of up to 5% by weight. The use of plastic fragments as a second fraction allows for easy and flexible adjustment of the calorific value of the briquette mixture. Plastic fragments can also be added to the separated fractions as coarse fragments depending on their nature or coarseness.

[0028] Furthermore, it may be useful if the gas is air, especially ambient air, but it may also be in line with efficient process control implications for the gas to be oxygen-enriched air or atmospheric air.

[0029] Furthermore, the oxygen content, composition and / or temperature of at least a portion of the incompletely combusted flue gas can be measured, preferably continuously, and the ratio of the briquette charge and / or the coarse fragment charge to the amount of gas can be controlled based on this measurement. This has the advantage that a particularly precise and efficient process control is possible. The measurement and control of the parameters can be carried out, for example, by a central control system.

[0030] Furthermore, the oxygen content, composition and / or temperature of at least a portion of the incompletely combusted flue gas can be measured, preferably continuously, and the calorific value of the briquettes in the upstream briquetting plant can be controlled based on this measurement. This has the advantage that a particularly precise and efficient process control is possible. The measurement and control of the parameters can be carried out, for example, by a central control system.

[0031] According to a particular embodiment, the at least one metal-containing phase can be at least substantially a copper-iron alloy. This means that the copper-iron alloy accounts for 50% or more by weight of the at least one metal-containing phase. Preferably, the copper-iron alloy accounts for 90% or more by weight of the at least one metal-containing phase. Producing a copper precursor instead of pure copper has the advantage that the melting and separation process can be carried out efficiently and relatively quickly. Therefore, additional process steps that may limit or slow the process can be carried out in a processing plant specially designed for the processing of copper-iron alloys.

[0032] In an advantageous development, the at least one slag phase and the at least one metal-containing phase can be transferred together, i.e., at least approximately in the form of a mixed phase, from the reactor to a separation furnace, where gravity separation of the at least one slag phase and the at least one metal-containing phase takes place, and the at least one slag phase and the at least one metal-containing phase can be removed separately from the separation furnace. By separating the mixed phase in a separate plant part or separate vessel, the reactor can be emptied and then recharged. This can increase plant efficiency, energy efficiency, and utilization.

[0033] In particular, it may be advantageous if the extraction of the at least one slag phase is carried out more frequently than the extraction of the at least one metal-containing phase, since this separated fraction has a low content of valuables and metals and a relatively high content of slag.

[0034] Furthermore, the briquettes, coarse fragments, and gas can be charged into the reactor using a charging lance, and the charging lance can have a diameter corresponding to 2 to 5 times, preferably at least 3 times, the maximum diameter of the separated fragments, which has the advantage that charging into the reactor can be performed simply and in a manner that is less susceptible to malfunction while still being controlled.

[0035] Additionally, a natural gas-oxygen combustion lance may be provided that extends into the reactor, preferably for use during the start-up process, such as when the plant is first started up or ramping up after a shutdown or cool-down. Additionally, the natural gas-oxygen combustion lance may be used to prevent or compensate for reactor cool-down between batches.

[0036] An advantageous embodiment includes a metallurgical consumable lance, which extends into the reactor and is used to inject oxygen-containing gas into the reactor. The gas can be blown directly onto the separated fragments or the metallurgical consumable lance can be immersed in the separated fragments. This allows compressed air to be introduced into the reactor as needed. The consumable lance can be used to blow directly onto the surface of the separated fragments, which have been molten into a slag phase and a metal-containing phase, or it can be immersed in both phases. Blowing compressed air onto the liquefied surface homogenizes the surface, which favorably affects the decomposition of the briquettes. When the consumable lance is immersed in both phases, the iron contained in the metal-containing phase is partially oxidized. This prevents an excessively high proportion of metallic iron in the metal-containing phase, which undesirably increases the melting point of the metal-containing phase and thus undesirably affects the slag properties, and prevents metallic iron from adhering to the inner walls of the reactor.

[0037] In a further development, the hot process gas from the thermal secondary combustion plant can be introduced into a waste heat recovery plant, where it is cooled and the energy released during cooling is used to generate superheated steam. This allows optimal utilization of the energy from the hot process gas, for example, for a combination of power generation, regional heat supply, and local heat supply. In this case, the hot process gas is cooled and the energy released during cooling is used to generate superheated steam. The waste heat recovery plant includes the main areas of a waste heat boiler and a turbine. The waste heat boiler is used, on the one hand, to cool the process gas before exhaust gas cleaning, and, on the other hand, to generate superheated steam by installing an economizer, an evaporator, and a superheater header within the boiler. Most of the superheated steam is then converted into electricity using a turbine. A portion of the steam is branched off via an intermediate extraction to feed the local regional heat supply network through a heat exchanger. Furthermore, a separate intermediate extraction within the turbine allows the steam to be used in a remote regional heat supply network.

[0038] Furthermore, it can be useful to introduce cooled process gas into a waste gas cleaning plant. A waste gas cleaning plant can include the main areas of process gas cleaning and sanitary gas cleaning. In sanitary gas cleaning, various extraction points are provided to extract emissions from briquetting plants, charging plants, and reaction plants, as well as from building extraction systems in general. Polluted, dispersed sulfur dioxide-free emissions from different points are sent to a central sanitary gas filter for dedusting or cleaning. Process gas cleaning can essentially be operated as a three-stage process. In this case, dust, i.e., solids in the process gas, are separated by filtration through one or more dust filters. Additives can also be added during this process. This is followed by the removal of harmful substances, particularly nitrogen oxide reduction by an SCR system (selective catalytic reduction), as well as the reduction of acidic components and heavy metals by adsorption methods.

[0039] Furthermore, the waste gas cleaning plant preferably comprises at least one filter for separating solids from the process gas cooled to a temperature of 210°C to 240°C, in which at least one filter separation of metal dust, in particular zinc dust, can be carried out.Since metal dust or atmospheric dust contains a large amount of zinc chloride or zinc oxide, a hygroscopic additive, for example lime powder, can be added as an additive.

[0040] However, the object of the present invention is also achieved by an industrial plant, which is adapted to carry out the method according to any one of the claims, and which comprises a charging plant, a reactor and a thermal secondary combustion plant. To avoid unnecessary repetition, reference is made to the above-mentioned description and advantages.

[0041] According to a particular embodiment, the industrial plant may include a waste heat recovery plant and / or a waste gas cleaning plant.

[0042] The present invention relates to a method for treating waste containing metals and other materials, particularly when present in the form of fluff or the like, for example shredder light fractions, to recover metals.

[0043] In this context, the object of the present invention is to provide a method suitable for treating waste containing metals and other materials, especially if they are present in the form of fluff or the like, for example shredder light fractions, in order to recover valuable metals.

[0044] This problem is solved by the method. Advantageous configurations of the invention are set forth in the dependent claims.

[0045] In a method for treating such waste containing metals and other materials to recover metals, the waste is compressed into briquettes and then introduced into a melting furnace where it is melted into at least two phases.

[0046] It is known in principle to use melting furnaces capable of melting waste materials to produce different phases, containing individual raw materials selectively or combined groups of raw materials.

[0047] However, to operate such a melting furnace, it is necessary to determine and adjust the composition of the reactants, including the air, as accurately as possible, which has not previously been possible in the case of light shredder fractions and similar wastes with a high proportion of organic and mineral components and a low proportion of metals.

[0048] The briquetting process allows the waste to be continuously charged into the melting furnace at a predetermined rate. Furthermore, the briquetting process ensures that the waste conversion reaction in the melting furnace occurs under favorable, safe, and controllable conditions. In other words, the briquetting process allows the materials fed into the melting furnace, particularly the material mixture required for the autothermal reaction, and thus the reaction mixture of waste, pyrolysis gas, and air inside the melting furnace to be precisely adjusted. In this way, the correct ratio of the individual reaction partners to each other, particularly the ratio of waste to air, can be ensured in an efficient and easily controllable manner. The method according to the present invention allows a large portion of the energy contained in the waste to be used for melting via the autothermal melting reaction, without sacrificing the possibility of recovering the metals contained in the waste. Metals can therefore be recovered in a particularly energy-efficient manner. In addition to recovering metals, particularly non-ferrous and precious metals, any mineral fractions present in the waste, such as those from the light shredder fraction, can also be reused as raw materials.

[0049] Briquettes are produced by compressing the waste material in a press, preferably designed as a piston press. Such devices, also known as briquetting presses, are generally known and, compared to other options for compressing waste material, are simpler and more reliable for continuous operation, even with large volumes.

[0050] Preferably, the waste metals include copper, lead, tin, zinc, nickel, iron, and precious metals for which the methods described herein are certainly feasible, although other metals may also be recovered from waste in the manner described herein.

[0051] Preferably, the other substances of the waste comprise organic matter and / or minerals. Particularly preferably, the waste has a high proportion of organic and mineral components and a low proportion of metal components, especially heavy metal components. Such types of waste can be treated particularly reliably and advantageously by the method described herein.

[0052] Preferably, the briquettes are used in a self-heating manner in the melting furnace with the addition of air to generate hot process gas. Compressing the waste into briquettes is particularly advantageous here because, compared to methods where the waste is not introduced into the melting furnace in other forms, the briquettes facilitate the continuous feeding of precisely measured amounts of waste into the melting furnace. Therefore, the reaction partners can be configured so that no additional energy supply is required for the reaction.

[0053] In this case, the hot process gases are preferably used at least in part to generate steam in a waste heat boiler, which can be used, for example, to generate electricity or the like by being fed to a steam turbine. However, the hot process gases, and in particular their thermal energy, can also be used in other ways, for example in a district heat supply system.

[0054] Furthermore, the hot process gas can at least partially contribute to the melting of the waste in the melting furnace by providing its thermal energy to the reaction, thus ensuring that the metallic and mineral components in the waste are melted.

[0055] Advantageously, by appropriately controlling the atmosphere in the melting furnace, a slag phase is generated that is poor in, and preferably substantially free of, valuable metals, in particular copper, lead, tin, zinc, nickel, iron, or precious metals. The slag phase is considered to be poor in valuable metals if its content of valuable metals is 0.7% by weight or less. The slag phase is considered to be substantially free of valuable metals if its content of valuable metals is 0.5% by weight or less. In addition, a liquid metal phase, in particular a liquid copper phase, is generated that is enriched in other heavy metals, in particular lead, tin, zinc, nickel, and precious metals. Individual components of the waste can be selectively recovered relatively easily from the slag phase and the enriched liquid copper phase. By feeding the waste in the form of briquettes, the atmosphere in the melting furnace can be controlled particularly well, in particular continuously.

[0056] Preferably, the molten waste is transferred to a separation furnace where separation of the slag and metal phases takes place, in particular gravity separation.

[0057] The object of the present invention is also achieved by an industrial plant adapted to carry out a method for treating waste containing metals and other substances to recover the metals, the industrial plant comprising a press, preferably designed as a piston press, for compressing the waste into briquettes and a melting furnace for melting the briquettes into at least two phases.

[0058] Other advantages and developments of the invention will become apparent from the claims and the detailed description that follows.

[0059] For a better understanding of the present invention, reference is now made to the following detailed description taken in conjunction with the accompanying drawings.

[0060] The figures are each shown in a highly simplified schematic representation. [Brief explanation of the drawings]

[0061] [Figure 1] FIG. 1 is a schematic process flow diagram. [Figure 2] FIG. 2 is a detailed diagram of the reaction plant shown in FIG. [Figure 3] FIG. 3 is a simplified schematic diagram of a system in which the preferred method can be implemented. DETAILED DESCRIPTION OF THE INVENTION

[0062] It should be noted at the outset that the same elements in the different embodiments described will be designated by the same reference numerals or part names. In this case, the disclosure contained in the entire description applies mutatis mutandis to the same elements having the same reference numerals or part names. Positional terms selected in the description, such as top, bottom, side, etc., are also based on the displayed figures directly described, and these positional terms will apply mutatis mutandis to the new positions if the positions change.

[0063] It should be understood that the term "particularly" hereinafter may refer to a possible more specific configuration or more detailed description of an object or method step, but not necessarily to a mandatory preferred embodiment or manner thereof.

[0064] As used herein, the terms "comprises," "has," "had," "includes," "included," "included," "including," and all variations thereof refer to a non-exclusive inclusion.

[0065] 1 shows a schematic process flow diagram of the most important method steps and material flows. It goes without saying that not all of the plant components and material flows shown or described below are absolutely necessary, and further plant components and material flows may be provided alongside those shown or described below.

[0066] The process shown in FIG. 1 or the industrial plant 27 shown diagrammatically therein essentially comprises six main plant areas: a briquetting plant 19, a charging plant 28, a reaction plant 29, a thermal secondary combustion plant 14, a waste heat utilization plant 25, and a waste gas cleaning plant 26. A waste treatment plant 48, e.g., a shredding plant, may also be attached to or precede the overall plant. A detailed view of the reaction plant 29 is shown in FIG. 2. To avoid unnecessary repetition, the following description of FIGS. 1 and 2 will be combined. The industrial plant 27 may be configured with a central control unit 30 that allows monitoring, measuring, controlling, and regulating the individual plant areas. However, it is also possible for the main plant area or the individual plant areas to have separate or independent control units 30.

[0067] In the illustrated embodiment, the briquetting plant 19 and the charging plant 28 are configured within the overall plant. The overall plant is fed substantially via a main conveying section for the additives 32 and a main conveying section for the waste 1. The waste 1, which contains at least one metal 2 and at least one organic substance 3, is treated or broken down in a waste treatment plant 48 in the illustrated example to provide separated fractions 4 of the waste 1. The briquetting plant 19 and the charging plant 28 are used for further processing of the separated fractions 4, which, upon leaving the briquetting plant 19 and the charging plant 28, essentially comprise briquettes 5 and, optionally, coarse fractions 6 of the waste 1 or of another waste 7. The briquetting plant 19 and the charging plant 28 also serve to transport the separated fractions 4, i.e., the briquettes 5 and, optionally, the coarse fractions 6, to a subsequent reaction plant 29. However, the production of the separated pieces 4, or simply the production of briquettes from the separated pieces 4, may also take place in a structurally or spatially separated briquetting plant 19, with the subsequent charging plant 28 simply storing the briquettes 5 or separated pieces 4 and transporting them to the reaction plant 29 as required.

[0068] In the waste treatment plant 48, the waste 1 undergoes single- or multi-stage mechanical processing, resulting in separated fractions 4 containing at least one metal 2 and at least one organic material 3. In the briquetting plant 19, briquettes 5 are produced from the waste 1. Optionally, coarse fragments 6 of the waste 1 or of other or different waste 7 are also produced. The coarse fragments 6 of the waste 1 can be, for example, fragments from a rough shredder sorting process containing a relatively high proportion of metals, especially non-ferrous metals. The coarse fragments 6 of other waste 7 can be, for example, electronic scrap, metal scrap, and / or plastic fragments. The separated fractions 4 thus comprise briquettes 5 and, optionally, the coarse fragments 6, and have a calorific value of 5 MJ / kg to 30 MJ / kg, with a maximum copper content of 0.1% to 20% by weight. In particular, the separated fractions 4 can have a calorific value of 8 MJ / kg to 25 MJ / kg, preferably 11 MJ / kg to 18 MJ / kg. Additionally or alternatively, the separated pieces 4 may have a maximum copper content of 0.3% to 10% by weight, particularly 0.5% to 3% by weight. The briquettes 5 may have a calorific value of 5 MJ / kg to 30 MJ / kg, preferably 8 MJ / kg to 25 MJ / kg, particularly 11 MJ / kg to 18 MJ / kg. The briquettes 5 may include fine fragments 17 and / or fluff fragments 18. Furthermore, the briquettes 5 may also include plastic fragments 31.

[0069] The structures of the briquetting plant 19 and the charging plant 28 are basically known and will not be described in detail here. The briquetting plant 19 and the charging plant 28 can have, for example, a screw conveyor, a screen, an intermediate bunker, a silo, one or more briquetting presses, one or more containers equipped with load cells, and / or a conveyor belt. The load cells enable the briquettes 5 and coarse pieces 6, and possibly also additives 32, to be accurately metered into the reaction plant 29 or reactor 8.

[0070] The separated pieces 4 are transported by a charging plant 28 to a reaction plant 29, where the separated pieces 4 are continuously or discontinuously charged into the reactor 8. The reactor 8 can be a melting furnace, in particular a so-called rotary furnace, or alternatively a top-blown converter furnace (TBRC). The reactor 8 is preferably a pear-shaped furnace vessel that can rotate about its longitudinal axis and tilt at a tilting point near the circular furnace opening. The reactor 8 consists of a cylindrical steel shell, a dish end, and an attached cone, and is lined with, for example, magnesite-chromium-based refractory bricks. The reactor 8 is rotatably supported, and the rotation and tilting movements can be performed using electric or hydraulic drives.

[0071] In the reactor 8, the separated fractions produced from the waste 1, including briquettes 5, and possibly coarse fractions 6 and additives 32, are burned or oxidized to melt, and the separated fractions 4 contain organic matter 3 and metals 2, in particular metallic iron, non-ferrous metals, and precious metals. The waste 1 may contain at least one mineral 15. Alternatively or additionally, a mineral slag former 16 may be added to the separated fractions 4. The mineral slag former 16 can be added to the reactor 8, especially if the separated fractions 4 contain no or only a small amount of minerals 15.

[0072] The reactor 8 is preferably operated in batch mode. To compensate for reactor cool down between batches and to facilitate heating of the reactor 8 during start-up or start-up, the reactor 8 is equipped with a natural gas-oxygen combustion lance 22. The natural gas-oxygen combustion lance 22 is powered by natural gas 50 and oxygen 49 and can be water cooled via a water 51 conduit.

[0073] The input materials, essentially the separated pieces 4, optionally with additional additives 32, and an oxygen-containing gas 9 as an oxidizer, are oxidized or burned in an incomplete combustion state in a preheated reactor, and the reaction or melting is ideally carried out self-heatingly without the addition of fuel. In this case, the thermal energy generated during the combustion of the separated pieces 4 is used to melt the separated pieces 4 into a liquid slag phase 10 and a liquid metal-containing phase 11. The oxygen-containing gas 9 can be air, particularly ambient air, but can also be oxygen-enriched ambient air.

[0074] The reactor 8 is charged with the briquettes 5, the coarse pieces 6, possibly additives 32 such as slag formers 16, and gas 9 by a charging lance 21. The charging lance 21 can be water-cooled and, for this purpose, has a water 51 conduit and can be equipped with a cleaning system like a pipe cleaner. The briquettes 5 are fed into the reactor 8 by means of the gas. The charging lance 21 can have a diameter corresponding to 2 to 5 times, preferably at least 3 times, the maximum diameter of the separated pieces.

[0075] A metallurgical consumable lance 23 or a compressed air lance 39 is also used to deliver compressed air 57 into the reactor 8 as needed. The consumable lance 23 can be blown directly onto the surface of the separated fragments 4 fused into the slag phase 10 and the metal-containing phase 11, or can be immersed in both phases 10 and 11. Blowing compressed air onto the liquefied surface homogenizes the liquefied surface, favorably affecting the decomposition of the briquettes. When the consumable lance 23 is immersed into both phases 10 and 11, the iron contained in the metal-containing phase 11 is partially oxidized. This prevents an excessively high proportion of metallic iron in the metal-containing phase, which would undesirably increase the melting point of the metal-containing phase 11 and thus undesirably affect the slag properties and prevent metallic iron from adhering to or adhering to the inner walls of the reactor 8.

[0076] The reactor area may be provided with an overhead crane with a series of hoists, which is used for operating the lances 21, 22, 23, during repair and shutdown phases, and for removing refractory and re-cladding the reactor 8.

[0077] During melting of the separated fraction 4, non-ferrous metals and precious metals, especially copper, are recovered as a metal-containing phase 11 or a copper-iron alloy or black copper phase. Due to its high specific gravity, the metal-containing phase 11 forms below the slag phase 10 after the melting process is completed and a certain time has passed for gravity separation of the phases 10 and 11. As soon as a sufficient filling level is reached in the reactor 8, the introduction of the separated fraction 4, especially the briquettes 5, is terminated. The lances 21, 22, and 23 are withdrawn from the reactor 8. After the melting process is completed, the reactor contents, consisting of the metal-containing phase 11 or black copper phase and the slag phase 10, are transferred together into a channel system and transported to the separation furnace 20 for gravity separation. Alternatively, although not shown, both phases 10 and 11 can remain in the reactor 8 for gravity separation, and then, after separation based on the difference in specific gravity, the two phases 10 and 11 can be removed separately from the reactor 8. According to the illustrated embodiment, the slag phase 10 and the metal-containing phase 11 are transferred from the reactor 8 to a separation furnace 20 where gravity separation of the slag phase 10 and the metal-containing phase 11 occurs. The slag phase 10 and the metal-containing phase 11 are discharged separately from the separation furnace 20. Regardless of whether gravity separation of the phases occurs in the reactor 8 or in the separation furnace 20, the slag phase 10 can be discharged more frequently than the metal-containing phase 11.

[0078] The separation furnace 20 is preferably a horizontal cylindrical furnace vessel, or a so-called tube furnace, supported for rotation around its longitudinal axis. Since no self-heating combustion reaction takes place in the separation furnace 20, the separation furnace 20 can be equipped with one or more heat burners or secondary fuel-natural gas-oxygen burners to prevent undesired cooling of the phases. For this purpose, the feed channel between the reactor 8 and the separation furnace 20 can also be equipped with heat burners or secondary fuel-natural gas-oxygen burners. If necessary, additives 32 can be added to both phases 10, 11 if necessary to modify the slag composition, particularly with regard to viscosity. The separation furnace 20 includes an opening (slag hole) for discharging the slag phase 10 in the direction of granulation and an opening (metal hole) for discharging the metal-containing phase 11 or black copper in the direction of the ingot casting belt.

[0079] Subsequent process steps of treating the metal-containing phase 11 on a slag granulation or ingot casting belt are well known in the art and will not be described in detail here.

[0080] Due to the high calorific value of the separated fragments 4, particularly the briquettes 5, process control involving incomplete combustion or oxidation is important to protect the reactor 8 from overheating, thermal collapse, and associated damage. It has been shown that incomplete combustion is sufficient to melt the separated fragments 4 into the two phases 10 and 11. During the melting process, the separated fragments 4 are melted at temperatures between approximately 1220°C and 1250°C. In particular, only a portion of the combustion energy is used to melt the separated fragments 4. In this process, incompletely combusted flue gas 13, or unburned pyrolysis process gases rich in CO, are generated in the reactor 8. At least a portion 12 of this incompletely combusted flue gas 13 is led from the reactor 8 to a thermal secondary combustion plant 14, where single- or multi-stage secondary combustion of at least a portion 12 of the incompletely combusted flue gas 13 is carried out.

[0081] Preferably continuous measurements can be made of the oxygen content, composition and / or temperature of at least a portion 12 of the incompletely combusted flue gas 13. Based on this measurement, the ratio of the amount of briquettes 5 and / or coarse pieces 6 charged to the amount of gas 9 is controlled by a control device 30.

[0082] However, it is also possible to carry out a preferably continuous measurement of the oxygen content, composition and / or temperature of at least a portion 12 of the incompletely combusted flue gas 13. Based on this measurement, the calorific value of the briquettes 5 in the upstream briquetting plant 19 is controlled by a control device 30.

[0083] Secondary combustion of incompletely combusted flue gases 13 or dust-laden process gases with high heat content in a thermal secondary combustion plant 14 is necessary and required by law in many countries. The thermal secondary combustion plant 14 essentially comprises a secondary combustion boiler. In this case, the secondary combustion must be carried out after the last fresh air supply, at a temperature of 1100°C and with a residence time of at least 2 seconds. This pyrometallurgical process can be performed cyclically, with the batch period being approximately the same length as the melting cycle in the reactor 8. This type of process control also results in a cyclical heat output from the reactor 8, which must be compensated for by adding secondary or supplemental fuel to the secondary combustion boiler to ensure stable operation of the waste heat recovery plant 25 downstream of the thermal secondary combustion plant 14.

[0084] The process gases leaving the reaction plant 29 or reactor 8 are collected in an exhaust gas hood, where air or ambient air, in an amount depending on the vacuum level, is mixed into the process gas 24 to remove the combustible components of the process gas 24 (CO, H, C x H y ) begins partial combustion. At this time, the temperature of the process gas 24 can rise to approximately 1450°C in the short process gas duct leading to the boiler. The necessary combustion air and, if necessary, supplemental fuel are supplied to the secondary combustion boiler inlet. For safety reasons, an adjustable natural gas burner can be operated at minimum power as a pilot burner at all times to ensure safe ignition of the process gas. One section of the secondary combustion boiler's combustion chamber is lined with refractory material and configured to maintain a two-second residence time and a temperature of 1100°C after the last fresh air supply. Two combustion air distributors, preferably equipped with nozzles, are provided to blow combustion air into the secondary combustion chamber. The combustion air distributors incorporate nozzle systems that can be used to burn waste oil, methanol-water mixtures, acetone, or natural gas. The supplemental fuel is adjusted depending on the temperature required for the secondary combustion section of the thermal secondary combustion plant 14. Another section of the combustion chamber of the secondary-fired boiler is configured as a deflector and is arranged immediately behind the preceding section of the secondary combustion chamber.

[0085] The deflector section can also be divided into two sections with a changing cross section. In the lower region, at the direct connection to the chimney, the deflector section has a circular cross section. At the transition, the cross section changes from circular to square. This makes it possible to connect the deflector section to the first flue of the boiler system, which has a square cross section. The tube walls of the deflector section are designed to maintain a residence time of 2 seconds at 1100°C after the last fresh air supply.

[0086] The hot process gas 24 generated during the secondary combustion in the thermal secondary combustion plant 14 can be directed to a waste heat recovery plant 25, where the energy derived from the hot process gas 24 can be optimally utilized, for example, for power generation or for heat supply to local and remote areas. In this case, the hot process gas 24 is cooled, and the energy released during cooling is utilized to generate superheated steam. The waste heat recovery plant 25 includes the main areas of a waste heat boiler and a turbine. The waste heat boiler is used, on the one hand, to cool the process gas before exhaust gas cleaning, and, on the other hand, to generate superheated steam by installing an economizer, an evaporator, and a header for a superheater within the boiler. Most of the superheated steam is then converted into electricity using a turbine. A portion of the steam is diverted via an intermediate extraction to supply the local heat supply network through a heat exchanger. Furthermore, another intermediate extraction within the turbine allows the steam to be used for heat supply networks in remote areas.

[0087] The cooled process gas 24 can then be introduced into the waste gas cleaning plant 26. The waste gas cleaning plant 26 includes the main areas of process gas cleaning and sanitary gas cleaning. In sanitary gas cleaning, various extraction points are provided for extracting emissions from the briquetting plant 19, the charging plant 28, the reaction plant 29, and generally from the building's extraction system. Polluted, sulfur dioxide-free dispersed emissions from different points are sent to a central sanitary gas filter for dedusting or cleaning. Process gas cleaning can essentially be operated as a three-stage process. In this case, dust, i.e., solids in the process gas 24, are separated by filtration in one or more dust filters, possibly with the addition of additives. This is followed by the removal of harmful substances, in particular nitrogen oxide reduction by an SCR system (selective catalytic reduction), as well as the reduction of acidic components and heavy metals by adsorption methods. The waste gas cleaning plant 26 comprises at least one filter for separating solids from the process gas 24 cooled to a temperature between 210°C and 240°C, in which at least one filter separation of metal dust, in particular zinc dust, takes place. As metal dust or atmospheric dust contains a large amount of zinc chloride or zinc oxide, a hygroscopic additive, for example lime powder, can be added as additive 32.

[0088] Figure 3 is another simplified schematic diagram of a system in which the preferred method may be practiced, showing briquettes produced by the method. 5 is used or processed in the reaction plant 29 is shown in the overall process or plant.

[0089] In this context, the shredder light fraction, which is an example of waste 1 containing metals 2 and other substances from which it is desired to fully recover its metal content, is first fed into a storage bunker 33 for further processing. From the storage bunker 33, the waste 1 is conveyed via a screw conveyor 34 or the like to a briquetting press designed as a piston compactor 35, where the waste 1 is compressed into briquettes. The shredder light fraction may contain as metals 2, in particular copper, lead, tin, zinc, nickel and / or precious metals.

[0090] In a specific plant, for example, four briquetting presses designed as piston compressors 35 are capable of compressing and briquetting about 10 tons of shredder light fraction per hour.

[0091] The briquettes 5 are then transported via a weighing machine 36 to a metering bunker 37, from where they are charged into a melting furnace 38 via a charging lance 21. In addition to the briquettes 5, air 47 is also charged into the melting furnace 38 to generate a reactive mixture inside the melting furnace 38. The briquettes are charged in batches, i.e., in one amount at a time.

[0092] Before the briquettes 5 are fed into the melting furnace 38, the melting furnace 38 is heated to, for example, 1200°C to 1250°C. 5 By compressing the organic matter 3 to a temperature of 1000°C, the amount of organic matter 3 introduced into the melting furnace 38 can be adjusted very precisely. In this regard, it has been found that the ratio of organic matter to the introduced mass is, for example, 35% to 50% in order to cause a self-exothermic reaction involving the air 47 delivered by a dedicated compressed air lance 39 and the pyrolysis gases.

[0093] The self-heating reaction can be stabilized by controlling the amount of air and pyrolysis gas added. To achieve this, it is essential to know how much organic matter 3 is present in the melting furnace 38. Air 47 is supplied only in the amount necessary for the reaction to occur within the melting furnace 38—i.e., for the combustion of the organic matter 3 and pyrolysis gas. However, the supply of air 47 is limited to prevent direct combustion of all the pyrolysis gas, in order to prevent overheating the melting furnace. This reaction proceeds within the melting furnace 38 for, for example, 5 to 5.5 hours without the addition of external fuel, resulting in the formation of a molten liquid consisting of liquid slag 10 and liquid metal 11 within the melting furnace 38.

[0094] Hot process gases 24 are generated during the autothermal reaction and are drawn through an inlet hood 40 and fed via a secondary combustion chamber 41 to a boiler 42. Steam can be generated in the boiler 42 in the usual way and this steam can be used to generate electrical energy by means of a turbine 43. Alternatively and additionally, the steam can be used for local and remote area heat supply networks.

[0095] After the reaction in the melting furnace 38 has been completed as completely as possible, the melting furnace 38 can be emptied and its liquid contents can be further transported via the transport section 44. Preferably, in this way, the molten liquid consisting of the liquid slag 10 and the liquid metal 11 is fed into the separation furnace 20. The separation furnace 20 can be realized, for example, as a rotary furnace, and the temperature inside can reach, for example, 1200°C to 1250°C. Unlike the melting furnace 38, the separation furnace 20 no longer undergoes any reaction inside, and therefore is externally refueled to reach and maintain the predetermined temperature. After the melting furnace has been emptied, it can be filled with the next batch of waste 1.

[0096] In the separation furnace 20, the separation of the slag phase 10 from the metal phase 11 can be carried out for, for example, 5 to 5.5 hours. 3 ~3.5t / m 3 whereas the specific gravity of the metal phase 11 is about 8t / m 3Therefore, gravity separation is suitable for this purpose. However, these values ​​are only examples and will of course vary depending on the material. If two or more phases have different specific gravities, these phases will be layered relative to each other in the separation furnace 20.

[0097] In the separation furnace 20, the slag is prepared for, for example, 3 to 4 hours, and then the slag is granulated for, for example, 2 to 3 hours, and can be removed from the separation furnace 20 through the slag discharge section 45.

[0098] Preferably, metal 2 can then be removed from separation furnace 20 through metal discharge section 46 and thereby recovered. Metal 2 can be present, for example, as a liquid metal phase, for example a liquid copper phase, which can be enriched with other or heavy metals, such as lead, tin, zinc, nickel and / or precious metals.

[0099] The above-described exemplary embodiments are illustrative of possible embodiments, and it should be noted at this point that the present invention is not limited to the specifically illustrated embodiments, but rather the individual embodiments can be combined with one another in various ways, and this variation is within the ability of a person skilled in the art based on the teachings of the present invention regarding the technical operations.

[0100] The scope of protection is defined by the claims. However, the detailed description and the drawings are to be relied upon for interpreting the claims. Individual features or combinations of features described in the different illustrated and described embodiments may constitute independent inventive solutions in themselves. The problems underlying these independent inventive solutions can be read off from this description.

[0101] In describing the present invention, all references to ranges of values ​​should be understood to include any and all subranges within that range. For example, a reference to 1 to 10 should be understood to include all subranges beginning at a lower limit of 1 and ending at an upper limit of 10. That is, all subranges begin at a lower limit of 1 or more and end at an upper limit of 10 or less, such as 1 to 1.7, or 3.2 to 8.1, or 5.5 to 10.

[0102] Finally, it should be pointed out that, formally, in order to make the structure easier to understand, some elements have been represented not to scale and / or enlarged and / or reduced. The following are some embodiments of the present invention. [Aspect 1] A method (1) for separating waste containing at least one metal (2) and at least one organic substance (3), comprising: providing a separated fraction (4) of the waste (1), the separated fraction (4) being separated from the waste (1) during mechanical treatment and comprising at least one metal (2) and at least one organic matter (3); the separated pieces (4) comprise briquettes (5) made substantially from the waste material (1) and, optionally, coarse pieces (6) of the waste material (1) or coarse pieces (6) of another waste material (7); providing the separated fragments (4), the separated fragments (4) having a calorific value of 5 MJ / kg to 30 MJ / kg and a maximum copper content of 0.1 wt % to 20 wt %; continuously or discontinuously charging the separated pieces (4) into a reactor (8); introducing an oxygen-containing gas (9) as an oxidant into the reactor (8) to combust the separated fractions (4) in an incomplete combustion process; a step of melting the separated pieces (4) into at least one liquid slag phase (10) and at least one liquid metal-containing phase (11) using thermal energy generated when the separated pieces (4) are combusted; Discharging the at least one slag phase (10) and / or the at least one metal-containing phase (11) from the reactor (8); conducting at least a portion (12) of the incompletely combusted flue gas (13) from the reactor (8) and introducing at least a portion (12) of the incompletely combusted flue gas (13) into a thermal secondary combustion plant (14) for secondary combustion of at least a portion (12) of the incompletely combusted flue gas (13). [Aspect 2] 2. The method of claim 1, wherein the waste (1) comprises at least one mineral (15) and / or the separated fractions (4) are added with a mineral slag former (16). [Aspect 3] 3. The method according to aspect 1 or 2, wherein the separated fragment (4) has a calorific value of 8 MJ / kg to 25 MJ / kg, preferably 11 MJ / kg to 18 MJ / kg. [Aspect 4] 4. The method according to any one of aspects 1 to 3, wherein the separated fraction (4) has a maximum copper content of 0.3 wt. % to 10 wt. %, preferably 0.5 wt. % to 3 wt. %. [Aspect 5] 5. The method according to any one of aspects 1 to 4, wherein briquettes (5) having a calorific value of 5 MJ / kg to 30 MJ / kg, preferably 8 MJ / kg to 25 MJ / kg, particularly preferably 11 MJ / kg to 18 MJ / kg, are provided. [Aspect 6] 6. The method of any one of aspects 1 to 5, wherein briquettes (5) are provided comprising fine fragments (17) and / or fluff fragments (18). [Aspect 7] 7. The method according to any one of aspects 1 to 6, characterized in that the gas (9) is air, in particular ambient air. [Aspect 8] 8. The method according to any one of aspects 1 to 7, characterized in that a preferably continuous measurement of the oxygen content, composition and / or temperature of at least a portion of the incompletely combusted flue gas (13) is performed, and based on this measurement the ratio of the briquette (5) charge and / or the coarse pieces (6) charge to the amount of the gas (9) is controlled. [Aspect 9] 9. The method according to any one of aspects 1 to 8, characterized in that a preferably continuous measurement of the oxygen content, composition and / or temperature of at least a portion of the incompletely combusted flue gas (13) is performed, and the calorific value (5) of the briquettes (5) in an upstream briquetting plant (19) is controlled based on this measurement. [Aspect 10] 10. The method of any one of the preceding aspects, wherein the at least one metal-containing phase (11) is at least substantially a copper-iron alloy. [Aspect 11] 11. The method of any one of aspects 1 to 10, wherein the at least one slag phase (10) and the at least one metal-containing phase (11) are transferred from the reactor (8) to a separation furnace (20), where gravity separation of the at least one slag phase (10) and the at least one metal-containing phase (11) occurs, and the at least one slag phase (10) and the at least one metal-containing phase (11) are separately discharged from the separation furnace (20). [Aspect 12] 12. The method of any one of the preceding aspects, wherein the pouring out of the at least one slag phase (10) occurs more frequently than the pouring out of the at least one metal-containing phase (11). [Aspect 13] 13. The method according to any one of aspects 1 to 12, wherein the briquettes (5), the coarse pieces (6), and the gas (9) are charged into the reactor (8) using a charging lance (21), and the charging lance (21) has a diameter corresponding to 2 to 5 times, preferably at least 3 times, the maximum diameter of the separated pieces (4). [Aspect 14] 14. The method of any one of aspects 1 to 13, wherein a natural gas-oxygen combustion lance (22) is provided and extends into the reactor (8), and is preferably used for firing the reactor (8) during a start-up process. [Aspect 15] 15. The method of any one of aspects 1 to 14, wherein a metallurgical consumable lance (23) is provided, projecting into the reactor (8), and used to inject an oxygen-containing gas (9) into the reactor (8), the gas (9) being either sprayed directly onto the separated pieces (4) or the consumable lance (23) being immersed in the separated pieces (4). [Aspect 16] 16. The method according to any one of aspects 1 to 15, wherein the hot process gas (24) from the thermal secondary combustion plant (14) is introduced into a waste heat recovery plant (25), where the process gas (24) is cooled and the energy released by the cooling is used to generate superheated steam. [Aspect 17] 17. The method according to aspect 16, wherein the cooled process gas (24) is introduced into a waste gas cleaning plant (26). [Aspect 18] 18. The method according to claim 17, wherein the waste gas cleaning plant (26) comprises at least one filter for separating solids from the cooled process gas (24), and wherein separation of metal dust, in particular zinc dust, is carried out in the at least one filter. [Aspect 19] 19. An industrial plant (27) for carrying out the method according to any one of embodiments 1 to 18, comprising a charging plant (28), a reactor (8), and a thermal secondary combustion plant (14). [Aspect 20] 20. An industrial plant (27) according to aspect 19, characterized in that it comprises a waste heat utilization plant (25) and / or a waste gas cleaning plant (26). [Explanation of symbols]

[0103] 1. Waste 2 metal 3 Organic matter 4 Separated fragments 5 Briquettes 6 Coarse fragments 7. Other waste 8. Reactor 9. Oxygen-containing gases 10 Slag phase 11 Metal-containing phase 12 part 13 Incompletely combusted flue gas 14 Thermal secondary combustion plant 15 Minerals 16 Mineral slag formers 17 Micro-fragments 18 fluff fragments 19 Briquetting Plant 20 Separation furnace 21 Charging lance 22 Natural Gas-Oxygen Combustion Lance 23 Consumable Lance 24 Process Gas 25 Waste heat utilization plant 26 Waste Gas Purification Plant 27 Industrial Plants 28 Charging Plant 29 Reaction Plant 30 Control device 31 Plastic Fragments 32 Additives 33 Storage Bunker 34 Screw conveyor 35 Piston compressor 36 Measuring instrument 37 Adjustment Bunker 38 Melting furnace 39 Compressed Air Lance 40 Suction Hood 41 Secondary combustion chamber 42 Boiler 43 Turbine 44 Transport Section 45 Slag discharge section 46 Metal discharge section 47 Air 48 Waste Treatment Plant 49 Oxygen 50 Natural Gas 51 water 52 Wastewater 53 Heat supply networks in remote areas 54 Local area short-distance heat supply network 55 Dust 56 Exhaust 57 Compressed Air

Claims

1. A method (1) for separating waste materials containing at least one metal (2) and at least one organic substance (3), comprising the steps of: providing a separated fraction (4) of the waste (1), the separated fraction (4) being separated from the waste (1) during mechanical treatment and comprising at least one metal (2) and at least one organic matter (3); The separated pieces (4) comprise briquettes (5) made substantially from the waste (1) and optionally coarse pieces (6) of the waste (1) or coarse pieces (6) of another waste (7), providing the separated fraction (4), the separated fraction (4) having a calorific value of 5 MJ / kg to 30 MJ / kg and a copper content of 0.1 wt% to 20 wt%; continuously or discontinuously charging the separated pieces (4) into a reactor (8); introducing an oxygen-containing gas (9) as an oxidant into the reactor (8) to combust the separated fractions (4) in an incomplete combustion process; Using the thermal energy generated when the separated pieces (4) are combusted, the separated pieces (4) are melted into at least one liquid slag phase (10) and at least one liquid metal-containing phase (11); Discharging the at least one slag phase (10) and / or the at least one metal-containing phase (11) from the reactor (8); and conducting at least a portion (12) of the incompletely combusted flue gas (13) from said reactor (8) and introducing at least a portion (12) of the incompletely combusted flue gas (13) into a thermal secondary combustion plant (14) for secondary combustion of at least a portion (12) of the incompletely combusted flue gas (13).

2. 2. The method according to claim 1, characterized in that the waste (1) contains at least one mineral (15) and / or that a mineral slag former (16) is added to the separated fractions (4).

3. 3. The method according to claim 1 or 2, characterized in that the separated pieces (4) are provided with a calorific value of between 8 MJ / kg and 25 MJ / kg.

4. 4. A method according to any one of claims 1 to 3, characterized in that the separated pieces (4) are provided with a copper content of between 0.3% and 10% by weight.

5. 5. The method according to any one of claims 1 to 4, characterized in that briquettes (5) are provided having a calorific value between 5 MJ / kg and 30 MJ / kg.

6. 6. The method according to any one of claims 1 to 5, characterized in that briquettes (5) are provided which comprise fine fragments (17) and / or fluff fragments (18).

7. 7. A method according to any one of claims 1 to 6, characterized in that the gas (9) is air, in particular ambient air.

8. 8. The method according to claim 1, wherein the oxygen content, composition and / or temperature of at least a portion of the incompletely combusted flue gas (13) is measured, and the ratio of the charge of briquettes (5) and / or the charge of coarse pieces (6) to the amount of gas (9) is controlled based on this measurement.

9. 9. The method according to claim 1, wherein measurements are made of the oxygen content, composition and / or temperature of at least a portion of the incompletely combusted flue gas (13) and, based on these measurements, the calorific value (5) of the briquettes (5) in an upstream briquetting plant (19) is controlled.

10. 10. The method according to any one of claims 1 to 9, characterized in that the at least one metal-containing phase (11) is at least substantially a copper-iron alloy.

11. 11. The method according to claim 1, wherein the at least one slag phase (10) and the at least one metal-containing phase (11) are transferred from the reactor (8) to a separation furnace (20), in which gravity separation of the at least one slag phase (10) and the at least one metal-containing phase (11) is carried out, and wherein the at least one slag phase (10) and the at least one metal-containing phase (11) are separately discharged from the separation furnace (20).

12. 12. The method according to any one of claims 1 to 11, characterized in that the pouring out of the at least one slag phase (10) is performed more frequently than the pouring out of the at least one metal-containing phase (11).

13. 13. The method according to any one of claims 1 to 12, characterized in that the briquettes (5), the coarse pieces (6) and the gas (9) are charged into the reactor (8) using a charging lance (21), the charging lance (21) having a diameter corresponding to 2 to 5 times the diameter of the largest diameter of the separated pieces (4).

14. A method according to any one of claims 1 to 13, characterized in that a natural gas-oxygen combustion lance (22) is provided to plunge into the reactor (8).

15. 15. The method according to any one of claims 1 to 14, characterized in that a metallurgical consumable lance (23) is provided, projecting into the reactor (8) and used to inject an oxygen-containing gas (9) into the reactor (8), the gas (9) being either sprayed directly onto the separated pieces (4) or the metallurgical consumable lance (23) being immersed in the separated pieces (4).

16. 16. The method according to any one of claims 1 to 15, characterized in that the hot process gas (24) from the thermal secondary combustion plant (14) is introduced into a waste heat utilization plant (25), the process gas (24) is cooled, and the energy released by the cooling is utilized to generate superheated steam.

17. 17. The method according to claim 16, characterized in that the cooled process gas (24) is introduced into a waste gas cleaning plant (26).

18. 18. The method according to claim 17, characterized in that the waste gas cleaning plant (26) comprises at least one filter for separating solids from the cooled process gas (24), in which at least one filter separation of metal dust, in particular zinc dust, takes place.

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