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    • 专利摘要:
    Disclosed is a single-chamber furnace for fumigating a vaporizable metal or metal compound from a metallurgical charge, comprising a bath furnace for containing a molten charge to a certain level, the furnace being equipped with a non-transfer arc plasma torch for generating of plasma and a first submerged injector for injecting the plasma below the determined level, the furnace further comprising an afterburning zone for forming an oxidized form of the at least one vaporizable metal or the at least one vaporizable metal compound, and a recovery zone for recovering the oxidized form from the gas formed in the post-combustion zone, the furnace further being equipped with a second submerged injector for injecting additional gas into the furnace below the determined level. Further disclosed is the use of the furnace and a method for fumigating a vaporizable metal or vaporizable metal compound from a metallurgical charge.
    公开号:BE1027793B1
    申请号:E20205842
    申请日:2020-11-20
    公开日:2021-06-23
    发明作者:Bert Coletti；Charles Geenen；Visscher Yves De；Mathias Chintinne
    申请人:Metallo Belgium；
    IPC主号:
    专利说明:

    4; BE2020/5842 Improved Plasma Induction Fumigation Furnace
    FIELD OF THE INVENTION The present invention relates to the field of pyrometallurgical recovery of non-ferrous metals, such as copper, lead, tin and zinc, from primary and/or secondary feed materials, also known as recyclables, or from combinations thereof. More particularly, the invention relates to the recovery of volatile metals, such as zinc and lead, from a bath of molten slag and/or metal, by a process step commonly referred to as fumigation.
    BACKGROUND OF THE INVENTION The production processes of non-ferrous metals such as copper, nickel, lead, tin and zinc generally involve at least one and usually a plurality of pyrometallurgical process steps in which metals and metal oxides both exist in the liquid molten state, and wherein the metal oxides are gravity as a separate lower density liquid slag phase can be separated from the higher density molten metal phase. If the slag phase is poor in valuable metals, the slag phase is usually withdrawn from the process as a separate stream, and that separation can lead to the production of a slag as the metal production by-product, a by-product that is also a "final slag" or a " final slug” can be called. WO 2013/133748 A1 and US 2015/0040722 A1 disclose a two-step smelting reduction process for the production of molten iron from iron oxide containing raw materials. The raw materials are first processed by a smelting reactor and then by a smelting reduction reactor. The atmospheres in the two reactors are kept strictly separated in such a way that in the smelting
    reduction reactor strongly reducing conditions can be maintained to increase the yield of the reduction to liquid iron melt, while more neutral conditions can be maintained in the melt reactor such that better use can be made of the combustion energy from the combustion of carbonaceous materials. The smelting reduction reactor is heated by submerged plasma generators, and the reducing atmosphere is obtained by adding a reducing agent such as coal or petroleum coke. The reaction produces a combustible gas mixture comprising CO and/or Hz, and usually also low levels of CO: and H:O. That gas mixture, after the removal of impurities, mainly comprises CO and/or Hz, and is partly recycled to the plasma generator which heats the smelting reduction reactor. The remainder of the gas mixture is used to heat the melt reactor by further combustion, by means of another submerged plasma generator and/or by injecting an oxygen-containing gas and the combustible gas mixture into a blowpipe below the surface of the molten furnace contents. Any sulfur present in the ferrous feedstock will usually be removed in the melt reactor, either in the reactor gases or as part of a matte phase.
    Copper present in the feedstock will typically be removed as metallic copper and/or matte copper in the bottom of the smelting reactor. The process can exhibit much lower CO 2 emissions than a conventional blast furnace process. WO 2013/133748 A1 and US 2015/0040722 A1 make no mention of any stripping or fumigation of a vaporizable metal or vaporizable metal compound, and the equipment described is not provided for its recovery as a separate product. The furnace described is therefore not suitable for fumigating a vaporizable metal or vaporizable metal compound from a metallurgical charge.
    US Patent 4,601,752 discloses a less complex process for producing metals and/or generating slag, illustrated for the production of ferrochrome from chromite ore. Oxide ore finely powdered, optionally together with slag formers, is treated in a single-chamber reactor comprising three zones, an upper oxidation zone in which the material is preheated and optionally melted by the combustion of carbon monoxide and hydrogen gas rising from the middle zone below with a gas containing oxygen, a middle zone consisting of a slag bath in which the preheated and possibly molten oxide material is at least partially reduced by the simultaneous injection of carbonaceous material and/or material containing hydrocarbon, and thermal energy mainly supplied by plasma generators, and a lower zone at the bottom of the reactor into which the metal formed during the reduction process settles, and from which the metal product and the slag by-product can be drawn off.
    The oxygen-containing gas introduced into the middle zone is 99.5% by weight pure oxygen.
    The addition of oxygen is controlled to generate sufficient energy to preheat and melt the ore and additives added to the chamber in the more oxidizing atmosphere prevailing in the middle and upper zones of the chamber reactor.
    The energy supplied by the plasma generators is controlled to drive the endothermic reactions between slag and carbon, under the reducing atmosphere prevailing in the lower part of the chamber reactor.
    Most of the exhaust gas from the furnace is treated for the removal of H:O and CO2, and is returned to the furnace as feed gas for the plasma generator.
    The remainder of the exhaust gas is removed from the process for use as fuel.
    US 4,601,752 makes no mention of any stripping or fumigation of a vaporizable metal or vaporizable metal compound, and the equipment described is not provided for its recovery as a separate product.
    The material balance in Figure 2 shows that no other gas is introduced into the furnace besides the plasma gas and the oxygen gas.
    This furnace is therefore also not suitable for fumigating a vaporizable metal or vaporizable metal compound from a metallurgical charge.
    WO 2016/078959 A1 discloses a one bath furnace for smelting metallurgical charges and separating metals in flexible oxidation-reduction conditions. The furnace is equipped with a plasma torch or burner of 3 MW, as well as a conventional so-called “oxygas” burner of 1.5 MW. The device makes it possible to carry out oxidation steps and reduction steps in the same furnace. The document proposes to use the oxygas mode for smelting and/or to create light reducing or any oxidizing conditions in the smelting furnace, and to use the plasma mode to achieve the highly reducing conditions. If a very high energy input is required, the two heating technologies can also be used simultaneously.
    The final slags extracted from pyrometallurgical processes used to produce non-ferrous metals are generally cooled, pelletized and crushed/cut to size, and can be used in concrete production, as a substitute for stone and grit or as aggregate in road construction. When ground, the slag can also be useful for use as sandblasting sand or blasting grit.
    Some of the substances that can be found in the slag products known in the art are considered potentially harmful to the environment. Mainly lead, but also zinc to some extent, are important examples of such undesirable substances. Zinc and lead are both metals that may be present at least partially in forms capable of leaching from the slag, and the presence of significant levels thereof preclude many uses of the slag product, especially the more economically attractive ones, and can make the dumping of such slag as backfill much more complex and difficult, generally having to be considered as “hazardous waste”. The acceptability of use in certain applications is often determined by testing the leaching behavior of slag. Typically, elements such as Pb and Zn are more prone to leaching, and they may be the reason why a particular snail fails such acceptability tests.
    In addition, Applicants have found that zinc levels on the order of 5% by weight and above in slag significantly retard the setting of concrete and other building material compositions, such as cement, when the slag is used in such building material compositions. That effect on the curing speed is an obstacle to the use of slags containing significant amounts of Zn as cement material and/or as aggregate in concrete or cement. For at least some of the above reasons, non-ferrous metal producers have attempted to reduce the levels of zinc, and if present also lead, in their slag by-products, often through a so-called “fumigation step”.
    Michael Borelli describes in “Slag — a resource in the sustainable society”, during the congress “Securing the Future. An International Conference on Mining and the Environmental Metals and Energy Recovery”, which took place in Skellefteà, Sweden, in 2005, pp. 130-138 of the Congressional Publication, how, since the 1960s, the liquid slag from an electric smelting furnace that produces a copper frost can be treated with reducing gases in a slag fumigation furnace, also referred to as a "box fumigator", a batch process step in which the zinc content in the copper smelting slag — and in additional zinc recycling material — is reduced to 1.2% by weight. The fumigated slag is further cleaned in a settling furnace where residual droplets of copper alloy and copper sulphide are allowed some residence time to separate into a heavier liquid phase before the slag is pelletized, dewatered and sold for road construction and sandblasting. The reducing gases for the fumigation plant are obtained by carefully mixing pulverized coal into the primary air injected into the furnace. The problem with this type of fumigation is that the reaction of coal with air must be limited to the production of mainly carbon monoxide, in order to maintain reducing conditions, and therefore most of the heat of reaction, ie the part generated by the successive reactions that oxidize carbon monoxide to carbon dioxide, remains unavailable in the furnace core to drive endothermic reactions, such as the reduction of metal oxides, such as zinc oxide, to the elemental metal that can be stripped from the liquid bath. Another disadvantage of a box fume installation is the high volumes of furnace exhaust gases that are generated, which must be cooled, filtered and treated to recover the fumigated metals and to clean them before they are released into the atmosphere.
    US 4,588,436 discloses a process for recovering metals from a charge of liquid slag in metallic or sulfide form by reduction with a carbonaceous reducing agent, wherein the thermal energy required to maintain the temperature and the reduction and sulfidation is provided by blowing gas preheated in a plasma generator below the surface of the slag bath. The vapor of volatile metals is condensed in a condenser, and recovered as liquid metal. The non-volatile metals and the sulphides formed are collected in the form of molten droplets which are allowed to settle from the slag. Reducing conditions must be maintained throughout the described process, downstream of the capacitor, to allow for the condensation of the volatile metals in the capacitor as a liquid metal product. The flue gases from the furnace containing the volatile metals also pose a significant safety risk. They are extremely reactive and have a high temperature. Any ingress of air, however small, will lead to the spontaneous combustion and possibly even explosion of the flue gases.
    In “ScanArc's Development of Plasma Based Processes for Recovery of Metals and Heat Energy from Waste and Hazardous Waste Materials”, presented at the International Workshop on Plasma Technologies for Hazardous Waste Destruction, Como, Italy, September 12-15, 1992, the company introduced ScanArc Plasma Technologies AB a submerged, non-transfer arc type plasma generator for the reduction of slag from the metallurgical industry by fumigation, which allowed the reduction of heavy metals, the recovery of the metals, and a vitrified, non-leachable slag could be produced. The plasma generator is able to operate on most gases, at any oxygen potential, to generate a very high usable enthalpy while keeping the gas flows relatively low, even with a lean gas mixture, thus offering great advantages in terms of flexibility. S.O. Santén delivered a very similar story at the 21st McMaster Symposium on Iron and Steelmaking, “Pretreatment and Reclamation of Dusts, Sludges and Scales”, at McMaster University, Hamilton, Ontario, Canada, May 11-13, 1993. applied commercially, inter alia, in Norway by Energy Recycling AS (ERAS) at the site of Hgyanger Sink Gjenvinning AS, as evidenced by the environmental permit application “Recovering of Metal Values from EAF Dust by the Arcflash fuming Process” filed October 10, 2002 and made public about two weeks before the public hearing on that subject, which took place on October 31, 2002. The application is also very detailed in terms of the process itself, the compositions of the raw materials and the products, including the flux components (“flux components ”), also known as the slag formers, the operating parameters, and the design of the equipment.
    WO 2005/031014 A1 also discloses such a fumigation reactor for treating Zn-containing residues using a submerged plasma-fired blower attached to a plasma torch as a source of heat and gas. WO 2008/052661 A1 discloses a method of fumigating Zn using a submerged plasma torch generating an oxidizing gas mixture into which a reducing agent in solid form is fed to melt.
    WO 2016/046593 A1 describes the smelting and fumigation of a metallurgical charge using a jet of hot gas from a submerged plasma torch, wherein the hot gas (or more correctly, "the plasma") produced has an enthalpy of at least 200 MJ/kmol. WO 2016/156394 A1 discloses a method for fumigating zinc from a metallurgical slag using a submerged plasma torch, wherein the zinc content of the produced slag was at most 1.00% by weight and the clean slag had the advantage offered fast curing when the slag was finely ground and used as an active binder, in a 50/50 mixture with sodium silicate, for tile making. The plasma fumigation furnaces described in the above-mentioned documents used as their heat source only plasma generators, i.e. burners that generate a very high temperature by consuming electricity, a source of energy that is quite expensive in many countries.
    However, the applicants have found that the gas flow that can be produced by an industrial scale plasma generator is limited in order to keep the electric arc active and stable, and to keep the enthalpy content of the hot gas from the plasma generator high enough to desired plasma. This is explained in more detail later in this document. Thus, there is a limit to the amount of stripping gas that can be made available by a plasma generator for stripping the vaporizable substances from the liquid bath in the furnace. This also limits the extent to which the gas injected from the plasma generators can agitate the liquid bath contained in the furnace.
    High reducing conditions are preferred in slag fumigation because the oxides of zinc and other vaporizable metals may need to be reduced to their respective elemental forms in order for the metals to become vaporizable. Strong reducing conditions can be obtained by adding at least one reducing agent, which can be a gas, a liquid, a solid, or a combination thereof, preferably a reducing agent in solid form, preferably carbon, and it can be are added to the hot plasma gas injected into the furnace.
    However, because of the small amount of plasma gas available per plasma generator, this method of introducing additional reducing agent remains limited. Additional reducing agent may be added to the furnace by preferably dropping a reducing agent in solid form onto the surface of the bath through the furnace fill opening.
    However, this additional method of introducing additional reducing agent leaves something to be desired.
    A reducing agent in gaseous form, such as natural gas, cannot be introduced by this addition method through the filling port of the furnace, since it would not reach the liquid bath in which it is to exert its reducing effect, because the reducing agent gaseous form would therefore have to go against the flow of the furnace exhaust gases. Injection of a liquid reducing agent, such as fuel oil, is also less preferred because its evaporation causes a large volumetric expansion, leading to foaming and spattering in the furnace, and some of the reducing agent may be entrained with the exhaust gases. before it can perform its intended function. The choice of suitable reducing agents is therefore quite limited.
    The additional reducing agent conventionally added through the fill and outlet opening in the top of the furnace must travel down through the gas space in the top of the furnace before it is able to reach the liquid surface. Just prior to the furnace gases entering the exhaust pipes, additional air is typically introduced to oxidize the vaporized elemental metals or metal compounds to their corresponding metal oxides. The oxides have much higher boiling points and melting points than the corresponding metals. The oxides formed readily appear as entrained flue gas dust and as such can be recovered further downstream in the furnace exhaust gas system. During its passage through the top of the furnace, the additional reducing agent is thus brought into contact with air, and at the high temperatures in the furnace, at least a portion of the reducing agent can be readily oxidized before the remaining portion is able to reach the surface of the liquid bath. The heat generated by this oxidation also does not reach the liquid bath, but remains with the exhaust gases. Rather than a benefit, that heat becomes an additional burden on the exhaust gas treatment system.
    The additional reducing agent that may be able to reach the surface of the liquid bath will not be able to perform its function properly unless it is properly mixed into the liquid bath. However, the gas flow available from the plasma generators does not cause very intense agitation of the bath.
    The additional reducing agent must also be able to travel down the gas space of the furnace, against the ascending stream of stripping gas, before permeating to the surface of the liquid bath. The particle or droplet size of the solid or liquid reducing agent must therefore be sufficiently high to avoid the particles and/or droplets being entrained too much with the stripping gas into the exhaust gas treatment system. However, large particles offer a limited surface area per unit mass, and are therefore less reactive when mixed in the liquid bath. Most reducing agents, such as solid carbon, have a much lower density than the liquid bath in the furnace. Larger particles exhibit greater buoyancy and therefore have a greater tendency to float to the surface of the liquid bath, further reducing the contact area between the solid reducing agent and the liquid bath.
    That additional method of adding additional reducing agent therefore suffers from a considerable lack of efficiency and effectiveness.
    The plasma-driven fumigation processes and furnaces known in the art therefore leave much to be desired. There is still a need for an improved plasma-driven fumigation process and apparatus that offers an increased fumigation rate, particularly through increased bath agitation and/or a greater amount of fume gas, as well as the ability to add additional reducing agent at a more efficient and effective way. The present invention aims to eliminate or at least alleviate the problem described above, and/or to provide improvements in general.
    SUMMARY OF THE INVENTION According to the invention there is provided an apparatus and a method as defined in any one of the appended claims.
    In one embodiment, the present invention provides a single-chamber furnace or apparatus for fumigating at least one vaporizable metal or metal compound from a metallurgical charge, comprising a bath furnace capable of containing a molten charge to a certain level, wherein the furnace equipped with at least one non-transfer arc plasma torch for generating plasma grade first hot gases and with at least one first submerged injector for injecting first hot gases from the plasma torch below the specified level, the furnace further comprising an afterburning zone comprises for oxidizing the at least one vaporizable metal or the at least one vaporizable metal compound in the flue gas to form an oxidized form of the at least one vaporizable metal or the at least one vaporizable metal compound, and a recovery zone for recovering the oxidized form of the at least e ne vaporizable metal or the at least one vaporizable metal compound from the gas formed in the post-combustion zone, characterized in that the furnace is further equipped with at least one second submerged injector different from the first submerged injector for injecting additional gas in the oven below the specified level.
    In another embodiment, the present invention provides a method of fumigating at least one vaporizable metal or metal compound from a metallurgical charge using the furnace or apparatus of the present invention, the method comprising the steps of: introducing the metallurgical charge comprising at least one vaporizable metal or vaporizable metal compound in the furnace and forming a bath of molten charge to the determined level; fumigating an amount of at least one vaporizable metal or metal compound from the bath using the plasma-grade hot gases from the at least one plasma torch and at least one reducing agent to produce flue gas containing the vaporizable metal or metal compound; ° post-combustion of the flue gas in the post-combustion zone to oxidize the at least one vaporizable metal or metal compound to an oxidized form of the at least one vaporizable metal or metal compound, ° extract from the furnace of the gas generated in the furnace and recovering the oxidized form of the at least one vaporizable metal or the at least one vaporizable metal compound from the gas generated in the post-combustion step; characterized in that, during at least part of the fumigation step, additional gas is injected through the at least one second injector into the bath and below the determined level, thereby increasing the amount of flue gases comprising the vaporizable metal or metal compound .
    The term metallurgical charge in the context of the present invention denotes a broad family of compositions that may occur at any time as, or as part of, a furnace contents or furnace charge during a pyrometallurgical process step, preferably a step that is part of the manufacturing process. for a non-ferrous metal.
    Preferably, the metallurgical charge is a first slag, and the product obtained from the process of the present invention is a second slag having a content of the at least one vaporizable metal or the at least one vaporizable metal compound that is reduced in comparison with the content of the same evaporable metal or the same evaporable metal compound in the first slag.
    In another embodiment, the present invention provides the use of the furnace of the present invention for fumigating at least one vaporizable metal or vaporizable metal compound from a metallurgical charge.
    The applicants have found that fumigating a vaporizable metal or metal compound from a metallurgical charge, wherein the fumigation step uses plasma-grade first hot gases from a plasma torch injected into the molten liquid bath through a first submerged injector, can be significantly improved by injecting additional gas through the at least one second submerged injector into the molten liquid bath.
    Applicants have found that the additional gas introduced through an additional submerged injector provides an additional injection point and additional gas volume for stripping the vaporizable metal or metal compound from the molten metallurgical charge. The applicants have found that if only the volume of plasma or hot gases coming out of the plasma torches is available for stripping zinc from a copper smelter slag, the zinc concentration in the gas bubbles rising through the molten slag bath can reach high values, up to as much as 40 mol%. Because at best an equilibrium condition can be reached for the zinc fumigation reaction (I), ZnO + C — Zn(g) + CO(g) (1) despite the favorable equilibrium constant enjoyed by the process at the very high temperatures of the hot plasma-grade gases from the plasma torch, the high Zn content in the gas bubbles results in a significant amount of zinc oxide remaining in the liquid bath. Applicants have found that that concentration in the gas phase can be significantly reduced by the present invention, due to the additional gas made available for stripping via an additional injector, and further due to the increased presence of the reducing agent throughout the liquid bath. that it makes possible. Since the amount of hot gases that can be produced by a plasma torch is limited, the applicants have found that it is advantageous to inject additional gas into the molten liquid bath, especially advantageous because of the injection through the at least one second submerged injector, which different from the first submerged injector.
    Thus, another advantage of the present invention is also that the invention provides at least one additional submerged gas injection point into the molten liquid bath. This brings the advantage of additional agitation of the molten liquid bath in the furnace, which improves mixing in the bath, leads to a more even distribution of temperature and reducing agent that can be added in the furnace, and thereby also promoting the chemical reactions that take place, also providing a more even distribution of the reduced metal or metal compound formed by the reaction with the reducing agent. The additional submerged gas injection point therefore also leads to an improvement of the fumigation effect via these mechanisms.
    Yet another advantage of the present invention is that it provides at least one additional means for further introducing reducing agent into the molten liquid bath in the furnace. At the same time, because the at least one second injector is a submerged injector, this additional agent provides a wider selection of suitable reducing agent compared to adding large particles of a solid reducing agent and/or a liquid reducing agent through the fill and outlet port. in the top of the oven. While by conventional means, all coke particles thrown into the furnace through the filling opening preferably have an average particle size in the range of at least 6 mm, such that most of the particles are able to fall down into the furnace and entrainment thereof with the exhaust gases leaving the furnace through the same opening is limited, the second submerged injector offers a much wider selection of suitable reducing agent. The reducing agent introduced through the second submerged injector may be a gas, liquid, solid or combinations thereof, and the reducing agent, when solid, may exhibit a much finer granulometry, providing additional advantages over the face of a high surface-to-volume ratio and a larger contact area, and thus a higher reactivity when the agent comes into contact with the molten liquid bath in the furnace. Submerged introduction of the reducing agent also offers the advantage of more intimate contact between the reducing agent and the liquid bath. That advantage applies to all states of aggregation of the reducing agent, but appears particularly prominent when the reducing agent is a solid, especially a finely divided solid. The present invention therefore accomplishes more than just providing more stripping gas to strip the vaporizable metal or metal compound from the metallurgical charge. An additional effect is the additional agitation of the bath, which leads to greater homogeneity in the bath in the oven, and an additional advantage is the possibility of injecting more, and possibly also a different and more effective reducing agent, in a more efficient manner. manner. These additional effects contribute to an even improved fumigation due to improved conditions that promote the intended chemical reactions.
    DETAILED DESCRIPTION The present invention will hereinafter be described in specific embodiments and with possible reference to specific drawings; however, it is not limited thereto, but is determined solely by the claims. The drawings described are only schematic and are non-limiting. In the drawings, the size of some elements may be exaggerated for illustrative purposes and not drawn to scale. The dimensions and relative dimensions do not necessarily correspond to actual practical embodiments of the invention.
    Furthermore, the terms first, second, third, and the like are used in the specification and claims to distinguish between like elements, and not necessarily to describe a sequential or chronological order. The terms are interchangeable in appropriate circumstances, and the embodiments of the invention may function in orders other than those described or illustrated herein.
    Furthermore, the terms top, bottom, top, bottom, and the like are used in the specification and claims for descriptive purposes, and not necessarily to describe relative positions. The terms so used are interchangeable in appropriate circumstances, and the embodiments of the invention described herein may function in orientations other than those described or illustrated herein.
    The term "comprising" used in the claims is not to be construed as being limited to the means listed in its context. He does not exclude other elements or steps. The term should be interpreted as meaning the required presence of the stated properties, numbers, steps or components, but does not exclude the presence or addition of one or more other properties, numbers, steps or components, or groups thereof. Thus, the scope of the expression "an item comprising means A and B" should not be limited to an article composed solely of components A and B. It means that for the subject matter of the present invention, A and B are the only relevant are components.
    Accordingly, the terms "comprise" or "enclose" also include the more restrictive terms "consist essentially of" and "consist of." Thus, when "comprise" or "contain" is replaced by "consist of", these terms represent the basis of preferred, but narrowed, embodiments, which are also provided as part of the contents of this document with respect to the present invention.
    Unless otherwise indicated, all values reported herein include the range up to and including the endpoints indicated, and the values of the ingredients or components of the compositions are expressed in percent by weight, or percent by weight, of each ingredient in the composition.
    Terms such as "% by weight," "% by weight" "% by weight" "percent by weight," "% by weight," "ppm by weight," "ppm by weight," "ppm by weight," ppm” or “ppm” and variations thereof, as used herein, refers to the concentration of a substance as the weight of that substance divided by the total weight of the composition and multiplied by 100 or by 1000000, as appropriate , unless otherwise noted It should be understood that the terms "percent," "%," used herein are intended to be synonymous with "percent by weight," "% by weight," etc.
    It should further be noted that, in the present specification and the appended claims, the singular forms "a", "the" and "the" may also refer to plural matters unless the content clearly indicates otherwise. For example, a reference to a composition comprising "a compound" also includes a composition having two or more compounds. It should also be noted that the term "or" is generally used to mean "and/or" unless the content clearly indicates otherwise.
    Furthermore, any compound used herein may be interchangeably discussed by its chemical formula, chemical name, abbreviation, etc...
    Plasma is considered the 4% state of matter, completing the series formed by solid, liquid and gas with an additional category on the high energy side. As the temperature of a gas is increased, at least some of the atoms separate into ions and electrons, forming an ionized gas, which is "a plasma", but may be called a hot plasma gas, or according to other sources even simply a “hot gas”. The ionization of atoms can be partial or complete, and the transition from gas to plasma is therefore not as sharp. A characteristic of a plasma is that the ionization must be maintained, which means a high temperature.
    In a non-transfer arc plasma torch, the plasma arc is generated between two electrodes in a torch body through which flows a gas that is converted to plasma by the energy released by the electric arc.
    Plasma torches with a non-transferring arc are in contrast to transferring plasma, where the substance to be processed is placed in an electrically grounded metal vessel and acts as an anode, so the reacting material must be an electrically conductive material. In transferring plasma, the anode can also be made of carbon. However, a carbon electrode has the disadvantage of capturing the reducing conditions, greatly reducing the versatility of the equipment compared to the fumigation process.
    To obtain a plasma, the enthalpy content of the plasma gas produced by the plasma generator should be at least 1 kWh/Nm*. Plasma quality hot gases therefore have an enthalpy content of at least 1kWh/Nm . Plasma torches known in the art can have a power of up to 5 or even 7 MW. A more typical plasma torch delivers about 3 MW, which means they cannot possibly exceed 3000 Nm can generate plasma-grade hot gases. A more typical operating regime yields a plasma with an enthalpy content in the range of 3.5-5.5 kWh/Nm3, i.e. a 3 MW plasma torch typically in the range of 600-800 Nm®/h hot gases of plasma quality. A plasma torch of a given electrical power is therefore unable to produce more than a corresponding volume of plasma-grade hot gases.
    In the context of a plasma torch, the gas volumes quoted include only the volumes of gas added to the plasma torch, and are at standard/normal conditions. The volumes quoted in the context of the present invention for the volumes of plasma-grade hot gases produced by a plasma generator (PG) include only the gas that has passed through the PG itself, ie what is the “primary gas” or is called the “primary gas volume”. Thus, they do not take into account any additional gases that are additionally fed directly to the downstream blowpipe, which are referred to as "secondary gas volumes" in the context of the present invention, and which are usually mixed with the plasma-grade hot gases from the plasma generator and which are injected into the bath together with it. After that mixing, the mixed gas may no longer qualify as “plasma grade” because the enthalpy content per unit volume may no longer meet the lower limit specified elsewhere in this document for such gases. All these gas volume figures are expressed under “normal” conditions. Thus, they also do not take into account any volumetric changes that may occur due to changes in temperature, pressure, chemical reactions or phase changes that may occur in the plasma generator or in the blowpipe downstream thereof.
    Submerged injector means a connecting pipe, tuyere or blowpipe between a gas source and an injection point which is located below the bath level or a certain liquid level in a furnace, and thus in a submerged position or a position intended to be submerged during operation . This ensures a more direct and intensive contact between the gas and the molten mass.
    The tuyeres, blowpipes or injectors should preferably be short, so that they are subject to minimal wear. This also ensures low heat losses. The blowpipes can be cooled to reduce their wear under the influence of the extreme temperature conditions. The blowpipes can be mounted horizontally, piercing the wall of the furnace below the level of the contents of the bath. The plasma or oxygas fired torches or burners to feed the blowpipes are then outside the furnace in a submersible (i.e. "submerged") position. When a liquid bath of a metallurgical charge is present in the furnace, they are preferably constantly fed with gas to prevent the molten mass from flowing back into the blowpipe, which could lead to flooding of the blowpipe, possibly causing severe damage. resulting in the blowpipe and possibly also the torch or burner feeding the blowpipe. Alternatively, the blowpipes can be mounted at an angle, still blowing into the bath, but the burners or torches can be above the level of the bath and outside the furnace. This arrangement results in slightly longer blowpipes, but can be arranged to also ensure that no molten material can storm back into the burners or torches. While that may be less advisable in large ovens, the blowpipes can also be placed vertically. The blowpipes for injecting the additional gas may be similarly arranged, i.e. submerged and through the wall of the furnace, perpendicular to or at some other angle to the furnace wall.
    By non-transferring arc plasma torch is meant a thermal gas generator that uses a plasma torch in which an electric arc is maintained between electrodes within the torch unit. A gas is introduced through an inlet opening into a flow-through chamber in which an electric arc is maintained. The gas heats to extreme temperatures and is expelled as plasma-grade hot gases, at least partially as a plasma, through an exit port.
    Between the plasma torch and the injection point in the furnace, additional substances can be added to the torch to injection point flow, such as envelope gas or diluent gas. In the context of the present invention, the amount of hot gases generated by a plasma torch is deemed to include only the primary gas flowing through the plasma generator and no added secondary gas, such as additional gas or other substances that may be added between the plasma torch itself and the injection point or blowpipe through which the first plasma-grade hot gases from the plasma torch are injected into the furnace.
    By oxygas burner is meant a thermal gas generator in which a carbonaceous fuel and an oxygenated gas are mixed and burned. In order to easily reach the high temperatures required for proper operation of the oxygas burner, the oxygen-containing gas is preferably rich in oxygen, more preferably substantially pure oxygen with low levels of inert components. This not only leads to higher flame temperatures, but also reduces the amount of inert gases that come along and have to be processed by the furnace exhaust system. The mixing zone of the oxygas burner is located in the burner unit, while the combustion zone of the oxygas burner can be located inside or outside the burner unit.
    The metallurgical charge, in the context of the present invention, may be any composition that may exist in a liquid molten state in a pyrometallurgical process step for the production of a non-ferrous metal. Thus, the metallurgical charge may be, for example, a molten metal composition comprising at least one non-ferrous metal, but may also be a molten slag phase occurring in such a process step. The metallurgical charge may be in the form of a molten liquid, but may alternatively be in any kind of solid form, for example the charge may take the form of aggregates obtainable by cooling or pelletizing a liquid molten phase from a furnace in which the pyrometallurgical process step has been performed.
    A metallurgical slag is usually not a pure substance but a mixture of many different components.
    As a result, a metallurgical slag has no apparent melting temperature. It has become common in the art to use the term "liquidus temperature", which is the temperature at which the slag is completely liquid.
    As mentioned in the background section is
    “fumigation” is an activity that has been used commercially in pyrometallurgy as early as the 1960s. The skilled person is well aware that certain metals or metal compounds can be vaporized from a metallurgical charge by stripping with a gas, also called "fumigation", at a pressure close to atmospheric pressure, i.e. no deep vacuum is needed as for the distillation of lead from tin. This ability is due to the fact that the vapor pressure of the vaporizable metal or metal compound is much higher than that of most of the rest of the other compounds in the batch. Such a compound is therefore considered in the art to be "evaporable" from the metallurgical charge, and also so called.
    Well-known examples are the fumigation of zinc from other pyrometallurgical compositions. That zinc fumigation can even be performed as part of another pyrometallurgical step, such as the removal of (usually some of the) zinc via the exhaust gases generated during a copper smelting step or a copper refining step. Less commonly, fumigation is performed as a separate process step, e.g. as in the "box fumigation" described by Michael Borrell or by ScanArc authors discussed above. And as also discussed above, when the metallurgical charge is a slag, the zinc may be mainly present in the charge as the non-volatile oxide ZnO, such that fumigation may need to be made possible by first reducing the oxide to elemental metal, a compound that can be stripped by fumigation. Another example is the recovery of lead and tin as their oxides by volatilization during the recovery of copper from copper-containing scrap, as discussed in the background section of U.S. Patent 3,682,623. Also elements such as bismuth, indium and/or germanium are known as vaporizable metals or have metal compounds which are vaporizable in the context of the present invention. Vaporizable metal compounds can be the corresponding oxides, chlorides and/or sulfides.
    In this document, unless otherwise indicated, amounts of metals and oxides are expressed in accordance with common practice in pyrometallurgy. The presence of any metal is usually expressed as its total presence, regardless of whether the metal is present in its elemental form (oxidation state = 0) or in a chemically bonded form, usually in an oxidized form (oxidation state > 0). For the metals which can be relatively easily reduced to their elemental form, and which can often exist as molten metal in the pyrometallurgical process, it is quite common to express their presence in terms of their elemental metal form, even when the composition of a slag or scratch is indicated, where the majority of such metals may in fact be present in an oxidized form. Therefore, in the composition of a slag such as the slag of the present invention, the content of Fe, Zn, Pb, Cu, Sb, Bi as elemental metals is expressed. Less precious metals are more difficult to reduce under non-ferrous pyrometallurgical conditions and largely exist in an oxidized form. These metals are usually expressed in terms of their most common oxide form. Therefore, in slag compositions, the content of Si, Ca, Al, Na is usually expressed as SiO2, CaO, Al2O3, Nas0, respectively.
    Because the oxygen in the slag bound to the nobler metals is not reflected in the composition, which only gives the elemental metal content, a slag composition reported by this method often does not come to a total approaching 100% by weight. .
    In an embodiment of the device or furnace according to the present invention, the device is equipped for injecting, through the at least one second injector, a total amount of additional gas which is at least 10%, preferably at least 15%, with more preferably at least 20%, 25%, 30%, 35%, 40%, 45%, 50% or 55%, more preferably at least 60%, preferably at least 70%, more preferably at least 75%, 80%, 90%, 100%, 110%, 120%, 125%, 130%, 140%, 150%, 175%, 200%, 225% and even more preferably at least 230% the amount of plasma grade hot gases which can be generated by the one element of the at least one highest power plasma torch when that torch delivers a plasma having an enthalpy content of at least 3.5 kWh/Nm 2 , expressed in volumetric units under normal conditions.
    Optionally, the device is equipped for injecting, through the at least one second injector, an amount of additional gas that is at most 500%, preferably at most 450%, more preferably at most 400%, 350%, 325%, 300%, 290%, 280%, 275%, 270%, 265%, 260%, 250%, 240%, 230%, 220%, 210%, 200%, 180%, 165%, 150%, 135% , 120%, 110%, 100%, 90%, 80%, 70%, 60%, 50%, 40%, 30% and more preferably at most 20% of the amount of plasma that can be generated by the one element of the at least one highest power plasma torch when that torch delivers a plasma with an enthalpy content of at least 3.5 kWh/Nm3, expressed in volumetric units under normal conditions.
    The applicants have found that a great advantage of the present invention can already be realized by injecting through the second injector an amount of extra gas flow closer to the indicated lower limit, especially when the extra gas flow is used as carrier gas for additional reducing agent, in especially when a fine powder, such as coal powder or pet coke dust, is used as an additional reducing agent.
    Applicants have found that the advantages of the present invention, which are set forth in detail in the summary section above, can be further enhanced as the amount of additional gas is further increased.
    However, the applicants prefer also to comply with the specified upper limit, in order to reduce the risk of splashing and foaming of the liquid bath, vibration and other types of dynamic stresses on the blowpipes and also on the rest of the furnace structure. and to reduce the volumes of gas that have to be processed downstream from the top of the furnace, for example through the post-combustion zone and the recovery zone.
    In the post-combustion zone of the furnace or apparatus of the present invention, the at least one vaporizable metal or metal compound in the flue gas is oxidized to create an oxidized form of the at least one vaporizable metal or at least one vaporizable metal compound in the flue gas. metal compound. The purpose of this step is to reduce the safety risk posed by the flue gas and to allow easier recovery of the metal from the flue gas.
    The flue gas formed in the upper part of the furnace poses a safety risk. The gas is very hot. The vaporized metal or metal compound present in the gas generally represents a reduced form of the metal and thus is also highly reactive when exposed to oxidizing conditions, such as in contact with oxygen. The flue gas formed in the upper part of the furnace therefore poses a significant safety risk. Any oxygen entering the equipment in an uncontrolled manner and coming into contact with the flue gas from the furnace, for example as part of ambient air possibly drawn into the top of the furnace or downstream thereof into the exhaust gas treatment section of the facility, would react quickly and oxidize the vaporized metal or metal compound, a reaction that is highly exothermic. In insufficiently controlled conditions, for example with low mixing and/or in particular in relatively stationary zones, such a combination of the hot gases with oxygen can almost inevitably lead to uncontrolled combustion, and possibly even a gas cloud explosion.
    In a steady and relatively fast flow of the gas and with good mixing, such combination of the gas with a known influx of air or other source of oxygen gas is able to create a flame front that can be stably and well controlled. . Applicants therefore provide, as part of the present invention, an afterburner zone in which, in a controlled manner, the hot gases are extracted from the top of the fumigation furnace, brought to a steady and relatively rapid flow rate, and mixed intensively with oxygen such that the conditions in the gas mixture change from reducing to oxidizing. The result of the good mixing and the high temperature is that a flame front develops and settles in the gas stream withdrawn from the top of the furnace, and this flame front can be easily maintained in a steady state. The applicants prefer to provide the flame front in the space above the fumigation furnace, which has the advantage that radiation from the stable flame front can still reach the liquid bath in the furnace and some of the heat from the flame front can be returned to the liquid bath.
    Another result of the post-combustion step or zone is that the safety risk posed by the hot and highly reactive gas in the top of the furnace is limited to the gas volume upstream of the flame front.
    The oxidized form of the at least one vaporizable metal or the at least one vaporizable metal compound is usually a metal oxide. The oxide forms of the metal or metal compound are generally non-volatile and usually form a fine particulate matter which is entrained in the gas stream, making it easier to recover them therefrom.
    The furnace of the present invention further includes a recovery zone for recovering the oxidized form of the at least one vaporizable metal or the at least one vaporizable metal compound from the gas generated in the post-combustion zone. The method of the present invention also includes the corresponding step of recovering the oxidized form of the at least one vaporizable metal or the at least one vaporizable metal compound from the gas generated in the furnace and subjected to the post-combustion step.
    In an embodiment of the device or furnace according to the present invention, the device comprises a plurality of second injectors and each injector is equipped for injecting, through each second injector, an amount of additional gas which is at least 10%, preferably at least 15%, more preferably at least 20%, 25%, 30%, 35%, 40%, 45% or 50%, more preferably at least 55%, preferably at least 60%, more preferably at least 65 %, even more preferably at least 70%, even more preferably at least 75%, preferably at least 80% of the amount of plasma-grade first hot gases that can be generated by the one element of the at least one plasma torch having the highest power when that torch delivers first hot gases with an enthalpy content of at least 3.5 kWh/Nm3, expressed in volumetric units under normal conditions. Optionally, each second injector is equipped to inject through the second injector an amount of additional gas that is at most 200%, preferably at most 190%, more preferably at most 180%, 170%, 160%, 150%, 140% 130%, 125%, 120%, 115%, 110%, 105%, 100%, 95%, and even more preferably at most 90% the amount of plasma-grade hot gases that can be generated by the one element of the ten at least one highest power plasma torch when that torch delivers a plasma with an enthalpy content of at least 3.5 kWh/Nm3, expressed in volumetric units under normal conditions.
    In an embodiment of the furnace or device according to the present invention, the device is connected to at least one compressed gas supply and/or equipped with a compressor for supplying compressed gas to the at least one second injector.
    Applicants have found that this provides a very convenient method of supplying additional gas to the furnace. The term "compressor" can be interpreted in its very broad sense, and can for example include a gas-fired turbine from which the combustion gases can be made available at a pressure higher than atmospheric pressure.
    In one embodiment of the furnace or apparatus of the present invention, the supply source for the additional gas for the apparatus comprises a source of a gas selected from the group consisting of hydrogen, nitrogen, air, carbon dioxide, argon, neon, helium, methane, ethane, propane, butane and combinations thereof, preferably nitrogen or air, more preferably air, even more preferably compressed air. The applicants have found that nitrogen and air, preferably compressed air, is a very practical gas as the basis for the additional gas to be injected into the furnace.
    In an embodiment of the furnace or apparatus of the present invention, the apparatus comprises means for thermally treating the additional gas upstream of the at least one second injector to alter its enthalpy content, the means for thermally treating the additional gas preferably comprises at least one heat exchanger. If, during operation, the gas supply to the furnace is at a temperature lower than the temperature of the liquid bath in the furnace, the applicants prefer to heat the gas before it is injected through the at least one second injector. This reduces the cooling effect that the injection of the additional gas can have on the furnace and makes it easier to maintain the heat equilibrium across the furnace. Preferably, the heat available in the system that processes the exhaust gas from the furnace is used at least in part for that heating.
    In one embodiment of the furnace or apparatus of the present invention, the apparatus is further provided with means for introducing a reducing agent into the additional gas upstream of the at least one second injector. As explained above in the summary section, the injection of the additional gas into the furnace through the at least one second injector represents an additional entry point for adding reducing agent into the furnace. Moreover, because the at least one second injector is a submerged injector, the choice of suitable reducing agents is very wide.
    In one embodiment of the furnace or apparatus of the present invention, the reducing agent to be introduced may be selected from a gas, a liquid, a solid, and combinations thereof. Applicants have found that the injection of additional gas in accordance with the present invention is a suitable carrier for a wide range of reducing agents in terms of volume or weight of reducing agent that can be practically introduced, not only as the reducing agent a is a gas or a liquid, but also when the reducing agent is a solid. In addition, a reducing agent in solid form may have a very fine granulometry such that it offers a high surface-to-weight ratio, and consequently a high reactivity to participate in the intended chemical reactions.
    In one embodiment of the furnace or device according to the present invention, the device comprises means for controlling the lambda value of the additional gas to be injected into the bath by the second injector.
    Lambda (“A”) is the very useful parameter bedosid often used with regard to burners and combustible fuels, especially in combustion engines, where that parameter represents the ratio to the current air-lot-fuel ratio in the numerator and in the denominator the air-to-fuel ratio of the same fuel in stoichiometric ratio. so if an air/fuel mixture is in stoichiometric ratio for complete combustion, its lambda value is 1.0. Applicants apply that lambda parameter tce to any gaseous mixture in which oxygen is present together with another substance that can readily react with oxygen, such as a combustible substance, where the other substance may be a gas, a liquid or a solid. , or a combination thereof.
    The applicants have found that controlling the lambda value of the additional gas injected through the at least one second injector is a very practical means of controlling the atmosphere in the furnace, adjusting whether the atmosphere is neutral, oxidizing or reducing, as well as the degree of oxidation or reduction.
    Applicants have found that the additional reducing agent feed point in the device of the present invention is very versatile and the control of the lambda value in the additional gas to be injected provides a very practical method of controlling the redox conditions in the kiln, thereby controlling the chemical reactions that take place in the kiln.
    The applicants have found that the combination of the injection of additional gas with the injection of hot gases from the plasma generator(s) allows for a wide range of redox conditions, whereby the redox conditions can be controlled almost independently of the heat input to the furnace. as opposed to the more conventional means of heating such as the use of natural gas burners.
    In one embodiment of the furnace or apparatus of the present invention, the apparatus is equipped to inject, as part of the additional gas, oxygen and a gaseous or liquid fuel, and to allow the velocity of the additional gas in the at least one second injector, or at some other location upstream thereof, exceeds the flame propagation rate of the fuel as part of the additional gas. The applicants have found that additional heat input into the furnace can be obtained by injecting, as part of the additional gas, a gaseous or liquid fuel, preferably when the additional gas further includes oxygen, even in the event that the additional gas has not been heated or ignited and therefore the fuel and oxygen have not reacted before reaching the liquid bath. Typically, the temperature of the liquid bath in the furnace is largely above the temperature at which the fuel and oxygen in the additional gas begin to react, even without an ignition source, and can react readily once injected into the liquid bath. Applicants prefer this embodiment because they have found that such a reaction can otherwise travel upstream, against the flow direction of the additional gas, in the lines upstream of the at least one second injector, and also in the second injector itself. Such a “blowback” phenomenon can lead to the release of heat in that pipe or injector and thereby to an increase in temperature, and thus also to more wear, or even an explosion of the extra gas upstream and/or in the injector. The applicants have found that the risk of damage to equipment due to such heating in or upstream of the injector can be reduced if the device is equipped to allow the additional gas to reach a velocity, in the second injector or in another location upstream thereof, which is higher than the flame propagation velocity in the additional gas. An additional advantage is that the extra gases are injected at a lower temperature, which further reduces the wear on the second injector.
    In one embodiment of the furnace or apparatus of the present invention, the apparatus is arranged to limit the amount of fuel injected such that combustion of the injected fuel under the intended operating conditions for the furnace causes an increase in the enthalpy of the additional gas such that that the additional gas at the injection point in the bath is at a temperature not exceeding the temperature of the molten charge intended to be in the furnace during operation. This also contributes to less wear on the second injector.
    In one embodiment of the furnace or apparatus of the present invention, the at least one second injector directs its additional gas to a second volume, as part of the furnace interior space below the predetermined level, which is different from the first volume in which the at least one first injector directs its first hot gases.
    Applicants have found that this feature enhances the benefits associated with the present invention set forth in the summary section above, including improved bath agitation, more homogeneous liquid bath composition, improved chemical reactions, and most certainly improved stripping the vaporizable metal or metal compound from the liquid bath.
    In an embodiment of the furnace or device according to the present invention, the at least one first injector is located in the side wall of the furnace, the at least one second injector is located in the furnace wall opposite the at least one first injector, preferably along the horizontal outer edge of the furnace, extending substantially the same height as the at least one first injector. Applicants have found that this arrangement is very practical and effective in obtaining the desired effects of the present invention as set forth in the summary section above. The at least one first injector may inject its additional gas in a direction approximately perpendicular to the side wall of the furnace. However, the applicants prefer to inject the additional gas at an angle to a horizontal plane, downwards or upwards, because the additional gas provides an additional buoyancy force for vertical circulation in the liquid bath, which prevents the agitation of the bath and also draws more reducing agent that may float on top of the liquid bath into the main body of the liquid bath. Applicants prefer the upward direction because it may be more suitable for establishing a toroidal circulation path in the liquid bath.
    In one embodiment of the furnace or apparatus of the present invention, the apparatus comprises at least two and preferably at least three first injectors distributed along a horizontal outer edge of the side wall of the furnace, the at least one second submerged injector being additional gas. directed to a volume as part of the interior space of the furnace below the predetermined level, approximately close to the vertical axis of the furnace, and/or the at least one second submerged injector is located along the side wall of the furnace at approximately equal distance between the locations of the two nearest of the at least two first injectors. In the embodiment wherein the at least one second submerged injector is located along the side wall of the furnace, the at least one second injector preferably directs its injected additional gas to a volume, as part of the interior space of the furnace below the predetermined level, which is different from the volumes to which the first injectors direct their first hot gases. Applicants have found that this enhances the beneficial effects obtained by the present invention, which are detailed in the summary section above.
    In one embodiment of the furnace or apparatus of the present invention, the apparatus is further equipped for introducing a reducing agent into the first hot gases upstream of the at least one first injector. This entails the advantage that even more reducing agent can be introduced into the furnace, in addition to the amount that can be introduced by other means, e.g. together with the extra gas and/or added via the feed opening. The amount of additional reducing agent that can be introduced through the at least one first injector is independent of the enthalpy input into the furnace. This method of introducing reducing agent is therefore extremely practical for controlling the redox property of the atmosphere in the furnace. An additional advantage is that the reducing agent introduced through the first injector is introduced along with the highest temperature enthalpy fed into the furnace. At a higher temperature, the equilibrium constant of the desired zinc fumigation reaction (I) favors the formation of zinc metal, which is a vaporizable substance. The effectiveness of the reducing agent introduced with the first hot gases is therefore greater, and because this injection also takes place via a submerged injector, it is also very efficient due to the extremely intimate contact of the first hot gases with the liquid in the liquid. bath, that is, only a little of this reducing agent can reach the surface of the liquid bath without coming into contact with liquid from the bath.
    In one embodiment of the furnace or apparatus of the present invention, the reducing agent to be introduced upstream of the at least one first injector may be selected from a gas, a liquid, a solid, and combinations thereof. Applicants have found that introducing the first hot gases from the plasma torch through the first injector provides a very versatile option for introducing additional reducing agent, as it is very tolerant of the choice of reducing agent, especially what in terms of its state of aggregation, but also in terms of the amount that can be introduced.
    In one embodiment of the furnace or apparatus of the present invention, the apparatus is further equipped with at least one oxygas burner for generating additional first hot gases in addition to the amount of plasma grade first hot gases from the at least one plasma torch. This entails the advantage that an additional supply of enthalpy into the furnace can be obtained in addition to the supply of enthalpy provided by the plasma generators. This can facilitate the maintenance of an advantageous heat equilibrium across the furnace, equipment and/or process as a whole.
    In one embodiment of the furnace or apparatus according to the present invention, the apparatus is equipped with at least one submerged third injector for injecting the additional first hot gases below the determined level. This entails the advantage of an extremely intimate contact between the additional first hot gases and the liquid bath, which is beneficial for the heat transfer from the additional first hot gases to the liquid bath in the furnace. This makes the heat transfer very effective.
    In an embodiment of the furnace or apparatus of the present invention comprising the at least one oxygas burner, the at least one oxygas burner is below the determined level.
    In one embodiment of the device according to the present invention, the plasma torch is below the determined level.
    Placing a hot gas and/or plasma generator below the determined level allows very short connecting pipes, the hot gas or plasma generator being positioned at the injection point, on the outside of the furnace. However, measures are needed to prevent the generator from flooding with the molten mass from the furnace. For this, a continuous protective flow of gas through the injector can be used.
    In one embodiment of the furnace or apparatus of the present invention, the post-combustion zone is provided above the predetermined level as part of the single-chamber furnace. Preferably, the post-combustion zone is provided above the liquid bath because of the radiant heat that can be passed from the post-combustion zone back to the liquid bath in the furnace. As set forth elsewhere in this document, oxidizing conditions are created in the post-combustion zone for the purpose of oxidizing the vaporizable metal or metal compound to the corresponding oxidized form. One important effect obtained from a complete conversion of the oxidation of the reduced form generated in the fumigation step is that the gas containing the oxidized form is no longer highly combustible, and that the safety risk created is thus contained by the gas from the fumigation step and is removed downstream from the post-combustion zone or step. A secondary purpose of the post-combustion step is to also oxidize most of the carbon monoxide that may have been generated in the fumigation step by the reaction of carbon in the reducing agent with, for example, the oxygen available in the slag as metal oxide to carbon dioxide. , and/or to oxidize hydrogen to water. This further reduces the safety risk and also makes further processing of the furnace exhaust, including any emissions into the atmosphere, easier, safer and more environmentally friendly.
    Preferably, the applicants carry out the afterburning by adding an oxidizing agent in the flue gas, the oxidizing agent being preferably oxygen.
    In one embodiment of the furnace or apparatus of the present invention, the post-combustion zone comprises a connection to a supply source of an oxygen-containing gas, preferably selected from air, oxygen-enriched air and purified oxygen gas. The applicants prefer to use air because of its hassle-free availability. Preferably, Applicants add the oxygen by injecting the oxygen-containing gas into the flue gas stream exiting the top of the furnace. Typically, the flue gas exiting the top of the furnace is at a pressure below atmospheric pressure due to the draft generated by the downstream exhaust gas treatment, which typically includes at least a furnace chimney and optionally a fan to generate a draft upstream of the furnace. includes the chimney. The oxygen-containing gas can thus be made available at atmospheric pressure. The Applicants prefer to provide the oxygen-containing gas at a pressure higher than atmospheric pressure because that gives a higher pressure difference between the source of the oxygen-containing gas and the flue gas produced in the exhaust gas treatment equipment of the the furnace is drawn by the natural or induced draft as set forth. A higher pressure difference entails the advantage that the flow of the oxygen-containing gas in the flue gas is easier to control more precisely.
    In a simpler embodiment, applicants provide at least one opening to atmosphere in the conduit connecting the furnace to the downstream exhaust gas treatment equipment through which ambient air may be drawn. Preferably, the size of the opening in the conduit is adjustable. A plurality of openings can be provided, which offers the advantage of a faster and more intimate mixing of the oxygen-containing gas with the flue gas.
    The applicants have found that a stable flame front can be formed in the post-combustion zone in which the oxidation reactions take place. The applicants have found that the flame front is more stable the faster the flue gas is moved and the faster and/or more intense the mixing with the oxygen-containing gas is.
    Applicants prefer to feed a substantial excess of the oxidizing agent to the post-combustion zone or step such that the oxidation reactions in the post-combustion zone are substantially complete. This ensures that the safety risk is completely limited to the afterburning zone or step and upstream thereof. It also ensures that the final exhaust gas is virtually free of carbon monoxide, which is a poisonous gas, as well as hydrogen.
    In one embodiment of the furnace or device according to the present invention, the device further comprises a cooling zone for cooling the gas that forms or has formed in the afterburning zone upstream of the recovery zone. The cooling can be carried out in various suitable ways.
    A suitable way is to provide a so-called waste heat boiler, i.e. a heat exchanger in which the heat from the gas from the post-combustion step is used to generate steam. The advantage is that the heat is used to generate steam, and that steam can be used elsewhere to provide power or heat where it can be useful. The high investment costs for a waste heat boiler compared to other alternatives can therefore be compensated by the value of the steam that is generated. However, a steam consumer of the appropriate size is not always available in the vicinity of the furnace according to the present invention.
    Another suitable way of cooling is by using a radiant water cooler, in which the water on the cooling side is circulated sufficiently quickly to prevent steam from being formed, such that only hot water is produced. Preferably, the water is recycled to the radiant water cooler after most of the heat has been removed. Preferably, that hot water can also be used in an economically valuable way for a heating application, such as to heat a plurality of residential buildings, more preferably the water is recycled after it has been used for the heating application. Additionally and/or alternatively, the hot water may be cooled in a conventional cooling tower. The amount of water that evaporates in the cooling tower must be replenished before the remaining water is returned to the radiant water cooler. Because salts accumulate in such a water cycle, the cycle must generally also provide a effluent, and the amount of effluent must also be replenished. A radiant water cooler also offers the advantage that it does not alter the amount of gas to be processed downstream on the gas side of the cooling step. Yet another advantage of a radiant water cooler is that this cooling step can be combined with the post-combustion zone, i.e. the post-combustion step can be performed inside the radiant water cooler. This embodiment provides an additional simplification of the equipment, and therefore a reduction of the investment costs.
    Yet another way of cooling is spray cooling or “evaporative cooling”. This method involves the injection of water into the hot gas stream, and the injected water extracts its heat of vaporization from the gas stream. This method is very efficient and fast, and requires little equipment and therefore low investment costs. The disadvantage is that the process increases the volume of gas to be processed downstream of the cooling step.
    Another suitable way is to use a gas/gas heat exchanger with the gas from the post-combustion stage on one side and, for example, ambient air on the other side of the heat exchanger. This entails the advantage that its volume is compact and does not increase the flow of the gas to be processed downstream of the cooling step.
    The preferred cooling step may comprise a number of similar or different coal processes selected from the list listed above. For example, a suitable combination may be to first provide a radiant water cooler on the hot inlet side to reduce the temperature of the gas from the afterburning step from, for example, about 1500°C to, for example, about 1000°C, followed by a spray cooling device to reduce the gas further down to about 200°C, which may be low enough for the equipment used in the subsequent recovery zone.
    In an embodiment of the oven or device according to the present invention, the recovery zone comprises a gas filter zone, wherein the gas filter zone preferably comprises at least one gas filter cloth. Applicants prefer to use filter sleeves made of polytetrafluoroethylene (PTFE) cloth because they are able to withstand processing temperatures up to about 260°C.
    Typically, the last equipment in the gas processing sequence is a blower or fan to expel the gas from the recovery zone into the emission chimney, and also to amplify the draft upstream by drawing gas through the afterburner zone, optional cooling zone, and recovery zone sequence. The use of a blower or fan has the advantage that the requirements of a natural draft in the emission chimney become less high, so that the chimney can be built less high.
    In one embodiment of the furnace or apparatus of the present invention, the furnace has a generally cylindrical shape, the furnace preferably also having a conical lower portion tapering to a smaller circular bottom, the cylindrical shape of the furnace having a largest has an internal diameter d and the furnace has an overall internal height h, from bottom to top, wherein the ratio of h to d is at least 0.75, preferably at least 0.80, more preferably at least 0.85, with even more preferably at least 0.90, even more preferably at least 0.95, preferably at least 1.00, more preferably at least 1.05, even more preferably at least 1.10, with even more preferably at least 1.15, preferably at least 1.20, more preferably at least 1.25, even more preferably at least 1.30. In the context of the present invention, the internal diameter of the furnace is the distance between two opposing surfaces of the furnace wall, and where a refractory lining is present, the surfaces of the refractory lining in the furnace at the time of construction. .
    The internal diameter is considered not to include any accumulation of frozen slag on those surfaces, a layer which may be termed "freeze coating".
    Applicants have found that this feature has the advantage of less splashing of the molten matter in the furnace bath during operation.
    Such splashing molten matter can solidify against a solid and cooler surface, such as the furnace inlet and/or the furnace exhaust pipes, where it can cause problems due to its high temperature, and where such accumulation of material can cause other operational problems such as blocking the gas flow and/or the possibilities of introducing feed material.
    In one embodiment of the oven or device according to the present invention, the oven comprises the conical lower part, the defined level being approximately at the height where the cylindrical shape merges into the conical lower part.
    Applicants have found that the conical lower portion provides a very practical arrangement in which most of the submerged injectors, and preferably also the corresponding devices supplying the feed materials for those submerged injectors, can be arranged for very efficient injection into the liquid. bath in the oven with a minimum of connecting pipes, while at the same time limiting the amount of floor space the device occupies. This arrangement has the advantage that the first injectors are brought closer to the central vertical axis of the furnace, which is conducive to agitation of the bath. This arrangement also provides greater agitation in the lower section where the first hot gases are injected and where also — in the embodiments where the apparatus includes blowpipes in the furnace wall of the smaller lower section — the additional gas is injected, while in the upper section the splashing is reduced thanks to the larger diameter. An additional advantage is that a liquid stream in the form of a toroid can be formed in the upper section, which is advantageous to draw into the bath any particles of reducing agent in solid form that may float on top of the liquid surface. In one embodiment of the furnace or apparatus of the present invention, the furnace is provided with an internal refractory lining, particularly where contact with molten metal and/or matt may occur. This entails the advantage that metallurgical charges with high melting temperatures and/or high liquidus temperatures can be processed or treated. The refractory lining is preferably provided in the lower section, where there may be a free molten metal and/or a matte phase, which has the advantage of better resistance to harmful chemical and/or mechanical action by those liquids.
    In one embodiment of the oven or device according to the present invention, the outer walls of the oven are cooled with water. The applicants have found that this is conducive to a longer lasting resistance of the equipment to the potentially very high temperatures that can occur in the furnace during operation. An additional advantage is that a freeze coating can form in the oven against the side walls of the oven. Such a freeze coating can provide additional thermal insulation against the potentially very high temperatures in the furnace during operation, and may provide additional protection for the refractory material which may be applied to the furnace walls.
    In an embodiment of the method according to the present invention, the amount of additional gas injected via the at least one second injector is at least 10%, preferably at least 15%, more preferably at least 20%, 25%, 30% , 35%, 40%, 45%, 50% or 55%, more preferably at least 60%, preferably at least 70%, more preferably at least 75%, 80%, 90%, 100%, 110% , 120%, 125%, 130%, 140%, 150%, 175%, 200%, 225%, and more preferably at least 230% of the amount of plasma-grade first hot gases that can be generated by the one element of the at least one highest power plasma torch when that torch delivers first hot gases with an enthalpy content of at least 3.5 kWh/Nm3, expressed in volumetric units under normal conditions. Optionally, the amount of additional gas injected through the at least one second injector is at most 500%, preferably at most 450%, more preferably at most 400%, 350%, 325%, 300%, 290%, 280% , 275%, 270%, 265%, 260%, 250%, 240%, 230%, 220%, 210%, 200%, 180%, 165%, 150%, 135%, 120%, 110%, 100 %, 90%, 80%, 70%, 60%, 50%, 40%, 30% and even more preferably at most 20% of the amount of plasma that can be generated by the one element of the at least one plasma torch having the highest power when that torch delivers a plasma with an enthalpy content of at least 3.5 kWh/Nm3, expressed in volumetric units under normal conditions. The applicants have found that a great advantage of the present invention can already be realized by injecting through the second injector an amount of extra gas flow closer to the indicated lower limit, especially when the extra gas flow is used as carrier gas for additional reducing agent, in especially when a fine powder, such as coal powder or pet coke dust, is used as an additional reducing agent.
    In an embodiment of the method according to the present invention wherein the device comprises a plurality of second injectors, the amount of additional gas injected via each second injector is at least 10%, preferably at least 15%, more preferably at least 20 %, 25%, 30%, 35%, 40%, 45% or 50%, more preferably at least 55%, preferably at least 60%, more preferably at least 65%, even more preferably at least 70 %, even more preferably at least 75%, preferably at least 80% of the amount of plasma grade first hot gases that can be generated by the one element of the at least one highest power plasma torch when that torch first hot gases with an enthalpy content of at least 3.5 kWh/Nm3, expressed in volumetric units under normal conditions.
    Optionally, each second injector injects an amount of additional gas that is at most 200%, preferably at most 190%, more preferably at most 180%, 170%, 160%, 150%, 140%, 130%, 125%, 120 %, 115%, 110%, 105%, 100%, 95% and even more preferably not more than 90% of the amount of first plasma-grade hot gases that can be generated by the one element of the at least one plasma torch with the highest power when that torch delivers first hot gases with an enthalpy content of at least 3.5 kWh/Nm3, expressed in volumetric units under normal conditions.
    In an embodiment of the method of the present invention, the additional gas injected through the at least one second injector comprises at least one gas selected from the group consisting of hydrogen, nitrogen, air, carbon dioxide, argon, neon, helium , methane, ethane, propane, butane and combinations thereof, preferably nitrogen or air, more preferably air, even more preferably compressed air.
    The applicants have found that nitrogen and air, preferably compressed air, is a very practical gas as the basis for the additional gas to be injected into the furnace.
    In one embodiment of the method of the present invention, the additional gas injected through the at least one second injector is thermally treated upstream of the at least one second injector to alter its enthalpy content, whereby the thermal treatment of the additional gas is preferably carried out using at least one heat exchanger. If the gas is supplied to the furnace at a temperature below the temperature of the liquid bath in the furnace, Applicants prefer to heat the gas before it is injected through the at least one second injector. This reduces the cooling effect that the injection of the additional gas can have on the furnace and makes it easier to maintain the heat equilibrium across the furnace. Preferably, the heat available in the system that processes the exhaust gas from the furnace is used at least in part for that heating.
    In one embodiment of the method according to the present invention, the temperature of the additional gas that flows into the at least one second injector is at most equal to the temperature of the bath in the oven, preferably at least 20 degrees Celsius below the temperature of the bath, more preferably at least 50, even more preferably at least 100, even more preferably at least 200 degrees Celsius below the temperature of the bath in the oven. This has the advantage that less wear occurs at the injection point, or the blow pipe. Optionally, the temperature of the additional gas entering the at least one second injector is at most 400 degrees Celsius below the temperature of the bath in the oven, preferably at most 350, more preferably at most 300, even more preferably at at most 250, preferably at most 200, more preferably at most 150, even more preferably at most 100, preferably at most 75, more preferably at most 50, even more preferably at most 25 degrees Celsius below the temperature of the bath in the oven. This has the advantage of reducing the risk of a build-up of solidified slag on the mouth of the injection point or blower pipe, which can be caused by the cooling effect of the additional gas flowing through the injection point or blower pipe and into the gets into the oven.
    In an embodiment of the method of the present invention, the additional gas injected via the at least one second injector comprises at least one first reducing agent, the at least one reducing agent preferably being selected from the group consisting of: any substance containing elements other than oxygen and noble gases and capable of reacting with oxygen under furnace conditions, preferably any substance containing carbon and/or hydrogen in a chemically bonded form suitable for oxidation, wherein the reducing agent is more preferably selected from the group consisting of natural gas, gaseous and/or liquid hydrocarbon, fuel oil, rubber, plastic, preferably a plastic made of at least one polyolefin, more preferably rubber - and/or waste plastics, charcoal or coke, and combinations thereof, even more preferably coke, even more preferably pet coke , which is a by-product of crude oil processing that is very rich in carbon. As explained above in the summary section, the injection of the additional gas into the furnace through the at least one second injector represents an additional entry point for adding reducing agent into the furnace. Moreover, because the at least one second injector is a submerged injector, the choice of suitable reducing agents is very wide.
    In an embodiment of the method according to the present invention using the first reducing agent, the first reducing agent is a solid, preferably in the form of particulate matter, more preferably the particulate matter has an average particle diameter of at most 6 mm even more preferably at most 5, 4, 3, 2 or 1 mm, preferably at most 500 µm, more preferably at most 250, 200, 150, 100 or even 50 µm. Applicants have found that suitable solid reducing agents are available in a wide variety of grades and from a variety of sources. In addition, several of those suitable solid form reducing agents have few, if any, alternative uses in which any significant economic value can be attributed to them. Such solid form reducing agents are therefore a very interesting source for use according to the present invention. As set forth elsewhere in this document, the smaller particle size has the advantage of providing a higher surface area to weight ratio, as well as lower buoyancy, and therefore more efficient and effective use of the reducing agent.
    In an embodiment of the method according to the present invention, the additional gas injected through the at least one second injector further comprises oxygen and an amount of fuel suitable for supplementing, by its combustion under the operating conditions in the furnace, an enthalpy supply. contribute to the furnace compensating for at least 50% of the cooling effect that the additional gas may have on the furnace in the event that the additional gas at the injection point is at a temperature lower than the temperature of the molten charge in the oven. Applicants prefer to add an amount of fuel which compensates for at least 75%, and preferably at least 100% of the described cooling effect. Applicants have found that additional heat input into the furnace can be obtained by injecting, as part of the additional gas, a gaseous or liquid fuel, preferably when the additional gas further comprises oxygen, more preferably at least sufficient oxygen to achieve the desired lambda value in the additional gases. Typically, the temperature of the liquid bath in the furnace is above the temperature at which the fuel and oxygen in the additional gas begin to react, even without an ignition source. Therefore, with sufficient oxygen in the additional gas, the added fuel ignites readily as soon as the additional gas comes into contact with the molten furnace charge. The applicants have found that the gas flows can be adjusted without any problem sufficiently high such that the combustion reaction does not move upstream against the flow direction of the additional gas in the second injector and/or in the lines leading to the at least one second injector. The risk of such a “kickback” phenomenon is therefore very low. The applicants have found that the risk of equipment damage due to such heating in or upstream of the injector can be easily eliminated if the additional gas, in the second injector or at any other location upstream thereof, reaches a velocity higher than the flame propagation rate in the additional gas. The applicants have found that that condition can be easily met for free.
    In an embodiment of the method according to the present invention, the additional gas injected via the at least one second injector has a first lambda value, taking into account only the gaseous and liquid combustibles, of less than 1.0, preferably at most 0.9, more preferably at most 0.8, even more preferably at most 0.7, even more preferably at most 0.6. Lambda (“A”) or lambda value refers to the very useful parameter often used in relation to burners and combustible fuels, especially in combustion engines, where that parameter represents the ratio of the current air flow in the counter. to fuel ratio and in the denominator the air to fuel ratio of the same fuel in stoichiometric ratio. so if an air-fuel mixture is in stoichiometric ratio, its lambda value is 1.0. Applicants apply that first lambda parameter to any gaseous mixture in which oxygen is present together with another substance which can readily react with oxygen, such as a combustible substance, the other substance being a gas or liquid, or a combination thereof. . The applicants have found that, if no solid reducing agent is used in the process, controlling the first lambda of the additional gas injected through the at least one second injector is a very practical means of controlling the atmosphere. in the furnace, setting whether the atmosphere is neutral, oxidizing or reducing, as well as the degree of oxidation or reduction. Applicants have found that the additional reducing agent feed point in the device according to the present invention is very versatile and the control of the first lambda, and/or the second lambda as described below, in the additional gas to be injected is a provides a very practical method for controlling the redox conditions in the furnace, and thereby directing the chemical reactions that take place in the furnace. The applicants have found that the combination of the injection of additional gas with the injection of first hot gases from the plasma generator(s) allows for a wide range of redox conditions, whereby the redox conditions can be adjusted almost independently of the heat input to the furnace. are set, as opposed to the more conventional heating means such as using natural gas burners. The applicants also consider a second lambda which takes into account all combustibles used in the process and added in the additional gas, i.e. including any solid combustibles such as most of the reducing agents listed above in this document are described. In an embodiment of the method according to the present invention, the additional gas injected via the at least one second injector has a second lambda of less than 0.6, preferably at most 0.5, more preferably at most 0.4 even more preferably at most 0.3, even more preferably at most 0.2. The applicants have found that such low values for the second lambda are very conducive to fumigation of metals from metallurgical slag, such as zinc.
    In one embodiment of the method of the present invention, the additional gas injected through the at least one second injector is combustible and the additional gas in the at least one second injector reaches a velocity that is higher than the flame propagation rate of the additional gas. Applicants have found that additional heat input into the furnace can be obtained by injecting, as part of the supplemental gas, a gaseous or liquid fuel, preferably when the supplemental gas further comprises oxygen. Typically, the temperature of the liquid bath in the furnace is above the temperature at which the fuel and oxygen in the additional gas begin to react, even without an ignition source. The applicants have found that such a reaction can travel upstream, against the direction of flow of the additional gas in the lines leading to the at least one second injector, and also in the second injector itself. Such a
    “back-back” phenomenon can lead to the release of heat in that injector line, thereby increasing the temperature of the additional gas upstream and/or in the injector. The applicants have found that the risk of damage to equipment due to such heating in or upstream of the injector can be easily reduced or even eliminated if the additional gas in the injector or other location upstream reaches a velocity that is higher than the flame propagation rate in the additional gas.
    In an embodiment of the method according to the present invention, the at least one vaporizable metal or the at least one vaporizable metal compound is a metal in its elemental form or a vaporizable compound containing a metal, the metal preferably being selected from the group consisting of consists of zinc, lead, tin, bismuth, cadmium, indium, germanium, and combinations thereof, wherein the vaporizable compound may be, for example, an oxide, a sulfide, a chloride, or a combination thereof. The applicants have found that the method according to the present invention is extremely suitable for the removal by evaporation of a metal or metal-containing compound selected from the given list. Applicants have found that this process offers a very competitive alternative for recovering any of the indicated metals from metallurgical charges.
    In an embodiment of the method according to the present invention, a metal that is less noble than the metal in the vaporizable metal or in the vaporizable metal compound is added in the furnace, preferably iron and/or aluminum, the less noble metal being preferably added added in the form of particulate matter, wherein the particulate matter more preferably has an average particle diameter of at most 5, 4, 3, 2 or 1 mm, preferably at most 500 µm, more preferably at most 250, 200, 150, 100 or even 50 µm, keeping the concentration of the less noble metal in the slag below its limit of solubility in the slag at process conditions. The applicants have found that this brings the advantage of improving the fluidity of a slag phase which may be present in the furnace as part of the liquid bath.
    However, the applicants have found that it is preferable to keep the concentration of those compounds below the solubility limit of the compound in the liquid bath because exceeding the solubility can lead to the formation of a separate phase of that particular compound in the oven. .
    Such a separate phase risks interfering with contact between the other liquid phase in the liquid bath with the injected additional gas and/or the first hot gas generated by the plasma torch and/or the additional first hot gases generated by the oxygas burner , if present, and thereby interfere with the chemical reactions desired in the furnace, leading in particular to poorer vaporization of the vaporizable metal or metal compound.
    In one embodiment of the method of the present invention, a second reducing agent is added to the first plasma-grade hot gases upstream of the at least one first injector.
    This entails the advantage that even more reducing agent is introduced into the furnace, in addition to the amount that can be introduced along with the additional gas.
    The amount of additional reducing agent that can be introduced through the at least one first injector is independent of the enthalpy input into the furnace.
    This method of introducing reducing agent is therefore extremely practical for controlling the redox property of the atmosphere in the furnace.
    An additional advantage is that the reducing agent introduced through the first injector is introduced along with the highest temperature enthalpy fed into the furnace.
    At a higher temperature, the equilibrium constant of the desired zinc fumigation reaction (I) favors the formation of zinc metal, which is a vaporizable metal or vaporizable metal compound.
    The effectiveness of the reducing agent introduced with the first hot gases from the plasma torch is therefore greater, and because this injection also takes place via a submerged injector, it is also very efficient due to the extremely intimate contact of the first hot gases with the liquid. in the liquid bath, i.e. only a little of this reducing agent can reach the surface of the liquid bath without coming into contact with liquid from the bath. In an embodiment of the method of the present invention utilizing the second reducing agent, the second reducing agent is selected from a gas, a liquid and a solid, and combinations thereof, wherein the second reducing agent is preferably selected from the group consisting of natural gas, gaseous and/or liquid hydrocarbon, fuel oil, charcoal or coke, and combinations thereof, and even more preferably is coke, even more preferably is petcoke, preferably in the form of solid particulate matter, wherein the particulate matter more preferably has an average particle diameter of at most 6 mm, even more preferably at most 5, 4, 3, 2 or 1 mm, even more preferably at most 500 µm, preferably at most 250, 200, 150, 100 or even 50 µm. The applicants have found that introducing the plasma through the first injector provides a very versatile option for introducing additional reducing agent, as it is very tolerant of the choice of reducing agent, especially with regard to its state of aggregation, but also in terms of the amount that can be introduced.
    In an embodiment of the method of the present invention, the method comprises the step of adjusting the oxygen potential in the slag in the range of 10 to 10° Pa (i.e. 10% to 107% atm). Preferably, the oxygen potential in the slag is adjusted by addition of the first and/or the second reducing agent. Thanks to the use of a plasma torch, virtually any oxygen potential can be combined with any amount of generated heat. In combination with the recovery of the one or more vaporizable metals or metal compounds, other metals can also be extracted from the material introduced into the furnace. In one embodiment, the oxygen potential in the slag can be adapted to selectively reduce metal compounds in the slag to a molten metal phase. Typical examples of such metals that can be reduced from the slag are Cu, Ni, Sn, Pb, Ag, Au, Pt and Pd. The molten metal phase can then be collected in the bottom of the furnace. The molten metal phase can then be removed, continuously or intermittently, through an outlet. To this end, the oven can be provided with a refractory lining at the bottom. In another embodiment where the material introduced into the furnace, and thereby also comprises the slag, sulfur or sulfur compounds, a matte phase can also be obtained. The oxygen potential in the slag can then be adapted to prevent the sulfur from being oxidized. Metals can then be recovered in a molten matte phase. Examples of metals that can be recovered from the slag in a matte phase are Fe, Cu, Ni, Sn, Pb, Ag, Au, Pt and Pd. The molten matte phase can then also be collected in the bottom of the furnace. The molten matte phase can be removed, continuously or intermittently, through an outlet. In yet another embodiment, both a metal phase and a matte phase can be obtained by adequate adjustment of the oxygen potential and the sulfur content. As a non-limiting example, Au, Pt and Pd can be reduced to a metallic phase, while Cu and Ni can be made to form the matte phase. The matte phase usually appears on top of the metal phase because it usually has a lower density than the metal phase and because the two phases remain more or less undissolved in each other. The matte phase and the metal phase may be withdrawn from the furnace through separate outlets or through a common outlet. In one embodiment of the method according to the present invention, the post-combustion is performed in the single-chamber furnace. This has the advantage of representing a much more compact design of the equipment, and consequently lower investment costs.
    In one embodiment of the method according to the present invention, the post-combustion comprises introducing into the post-combustion zone an oxygen-containing gas, preferably selected from air, oxygen-enriched air and purified oxygen gas. The applicants have found that this option is a relatively simple option with low investment costs to achieve the function of the afterburner zone. Applicants prefer to simply use air, as explained above. In an embodiment of the method according to the present invention, the oxidized form of the at least one vaporizable metal or the at least one vaporizable metal compound is recovered from the gas as dust. Applicants have found that this option is much safer as compared to the alternative where the metal is condensed to form a liquid metal phase, for example as set forth in U.S. Patent No. 4,588,436, because the risk of spontaneous ignition and/or explosion of the exhaust gas from the furnace virtually terminates at the outlet of the afterburner zone. Applicants have also found that this option entails relatively low investment costs, for example compared to the alternative described in US 4,588,436.
    In an embodiment of the method according to the present invention, the recovery of the oxidized form of the at least one vaporizable metal or the at least one vaporizable metal compound from the gas comprises filtering the gas containing the oxidized form of the at least one vaporizable metal or the at least one vaporizable metal compound, using a filter, preferably a filter cloth. As set forth above, Applicants prefer to use filter sleeves made of polytetrafluoroethylene (PTFE) cloth. In such a gas filter the gas velocities can be very low locally. Still, oxygen is expected to be present. It is therefore important to the process of the present invention that substantially all of the reduced form of the metal or metal compound is oxidized to its oxidized form such that the risk of spontaneous ignition and/or explosion is acceptably low.
    In an embodiment of the method according to the present invention, the method further comprises a cooling step upstream of the recovery of the oxidized form of the at least one vaporizable metal or the at least one vaporizable metal compound from the gas. A variety of suitable cooling methods can be used, as set forth above.
    Typically, the last step in the gas processing sequence is a blower or fan that forces the gas from the recovery zone into the emission chimney, and also boosts the draft upstream by drawing gas through the sequence of afterburner zone, optional cooling zone, and recovery zone.
    In an embodiment of the method of the present invention, the method comprises forming a molten metal phase, the method further comprising the step of removing the molten metal phase from the furnace. Applicants have found that the process of the present invention can potentially lead to the formation of a separate molten liquid phase due to the reduction of less volatile metals to their elemental form. This can be a pure metal phase or a molten alloy. In such circumstances it is very practical to remove the separate molten metal phase from the furnace as a separate by-product. In the case of an alloy, it may be preferred to further process the alloy such that at least one of the metals in the alloy is recovered separately from some of the other metals in the alloy. Said further processing may comprise pyrometallurgical steps and/or electrolytic steps.
    In an embodiment of the method of the present invention wherein the metallurgical charge comprises a slag and wherein the slag comprises sulfur and/or sulfur compounds, the method further comprises the step of forming a molten matte phase and a further step of removing the molten matte phase from the oven. That is an option, possibly in addition to the recovery of a liquid molten metal or alloy from the process.
    In one embodiment of the method according to the present invention, the metallurgical charge is introduced into the furnace as a liquid. This entails the advantage that the metallurgical charge does not have to be melted and/or melted out as part of the process carried out in the plant and/or furnace, which is advantageous for the heat equilibrium of the furnace and therefore also for the productivity of the process and equipment, including the furnace itself.
    In one embodiment of the method of the present invention, the metallurgical charge is a metallurgical slag, wherein the metallurgical slag is preferably selected from a copper smelting slag, a copper refining slag, and combinations thereof, the process producing a second slag.
    Applicants have found that the method (and apparatus) of the present invention is highly suitable for treating the feed materials as indicated.
    In an embodiment of the method according to the present invention, the molten slag has an average temperature of less than 50 degrees Celsius above the liquidus temperature of the slag.
    This entails the advantage that the freeze liner of solid slag which forms against the internal surfaces of the furnace wall, and which protects the refractory lining, can be easily maintained at a sufficient thickness to provide adequate protection and heat retention. insulation.
    Such a freeze lining is very advantageous in terms of the thermal equilibrium of the furnace, since it acts as thermal insulation between the hot liquid slag in the furnace and the furnace wall, which is preferably cooled to protect its mechanical integrity.
    The freezer lining therefore reduces heat losses from the oven to the cooled wall.
    In one embodiment of the method according to the present invention, an oxide selected from CaO, Al:O3, and combinations thereof, is added to the slag in the fumigation furnace, preferably at a temperature of at least 1000°C, preferably at least 1050°C, more preferably about 1150°C.
    This feature entails the additional advantage that the final composition of the second slag after the fumigation step can be further optimized and stabilized, and that the slag is made more suitable for certain end uses by possibly also influencing the mineralogy.
    The applicants have found that the high temperature addition,
    as indicated, and in the molten state, is more effective to obtain the desired effects.
    In an embodiment of the method according to the present invention, the temperature of the slag in the furnace is at least at the temperature indicated in the preceding paragraph, more preferably still higher, such as at least 1200 or 1250 or 1300°C, and with more preferably about 1350°C. This entails the advantage of a more favorable equilibrium constant between the vaporizable metal or metal compound and its precursor in the liquid slag.
    An additional advantage of a higher temperature is that it facilitates the removal of the fumigated slag from the furnace, the so-called "draining", whether this is done by overflow or by tapping at the bottom through a bottom tap hole at a suitable location in the oven wall.
    In an embodiment of the method according to the present invention, the method further comprises the step of cooling the second slag to become a solid, wherein the second slag is preferably first removed from the furnace as a liquid. The advantage is that the fumigation furnace can be released for further slag treatment while the second slag cools. The slag can be cooled and/or cured by bringing the slag into contact with a cooling medium, such as air and/or water, possibly ambient air.
    In an embodiment of the method according to the present invention in which the second slag is cooled, the cooling is performed by contacting the liquid second slag with water. Applicants have found that water cooling is very effective and can be performed in many different ways, resulting in relatively well controlled cooling rates.
    In an embodiment of the method according to the present invention wherein the second slag is cooled, the second slag is cooled at a rate of at least 30 degrees Celsius per second, preferably at least 40 degrees Celsius per second, more preferably at least 50 degrees Celsius per second. or 60 degrees Celsius per second. The applicants have found that at the higher cooling rate, as indicated, a higher amorphous content of the slag can be obtained, which is important for certain end uses, such as when the slag is intended for use as a binder in the construction industry.
    In an embodiment of the method according to the present invention wherein the second slag is cooled, the method further comprises the step of grinding the solid second slag, preferably grinding the second slag into powder.
    In an embodiment of the method according to the present invention wherein the second slag is cooled, the second slag is cooled at a rate of less than 40 degrees Celsius per second, preferably at most 30 degrees Celsius per second, more preferably at most 20 degrees Celsius per second. degrees Celsius per second. The applicants have found that at the lower cooling rate, as indicated, a lower amorphous content of the slag can be obtained, and thus a more crystalline character, which is important for certain end uses, such as when the slag is intended for use as aggregate or for decorative purposes.
    In an embodiment of the method according to the present invention, wherein a second slag is formed by the method, the method further comprises the step of adding the second slag as a binder or as an aggregate during the production of an article for the construction industry. The applicants have found that the second slag can be used as a binder for aggregates, preferably as an active binder, preferably as a binder with pozzolanic effect. Applicants have found that the slag can act as a cement replacement binder, for example when used as a partial cement replacement, such as Portland cement, but also as a binder for producing geopolymer compositions.
    In an embodiment of the method according to the present invention, wherein the slag is used as a binder during the production of an article for the construction industry, the article further comprises an aggregate, the aggregate preferably comprising sand and/or the second slag.
    In an embodiment of the method according to the present invention, wherein the slag is used as a binder during the production of an article for the construction industry and the article further comprises an aggregate, the method further comprises the step of adding an activator during the production of the object. The applicants have found that the second slag can act as an active binder, which is able to react with a suitable activator and thereby exhibits strong binding properties for aggregates. The second slag can therefore be used as a substitute for Portland cement, or as the sole binder in an article, in which case it is considered to be a “geopolymer”, substances which, for example, impart fire and heat resistance properties to coatings, adhesives, composites and so on.
    In an embodiment of the method of the present invention using an activator, the activator is selected from the group consisting of sodium hydroxide, NaOH, potassium hydroxide, KOH, sodium silicate, Na2SiO3, potassium silicate, K2SiO3, and combinations thereof, wherein the activator is preferred is NaOH.
    In an embodiment of the method according to the present invention in which an article for the construction industry is formed, the article for the construction industry is a building element.
    In an embodiment of the method according to the present invention in which a building element is formed, the building element is selected from the list consisting of a tile, a paving stone, a block, a concrete block, and combinations thereof.
    In an embodiment of the method according to the present invention in which a construction industry article is formed, the construction industry article has a foamed structure.
    In one embodiment of the use of the present invention, the metallurgical charge is selected from a copper smelting slag and a copper refining slag, and combinations thereof.
    In one embodiment of the use of the present invention, the vaporizable metal or metal compound is selected from zinc, lead, tin, bismuth, cadmium, indium, germanium, and combinations thereof.
    In an embodiment of the method according to the present invention, at least part of the method is monitored and/or controlled electronically, preferably by a computer program. Applicants have found that electronically controlling steps of the method according to the present invention, preferably by a computer program, brings the advantage of much better processing, with results that are much more predictable and closer to the process objectives. For example, based on temperature measurements, and if desired also measurements of pressure and/or content, and/or in combination with the results of chemical analyzes of samples taken from process streams and/or analytical results obtained in online , controlling the equipment with regard to the supply or withdrawal of electrical energy, the supply of heat or of a cooling medium, regulation of flow and/or pressure. The applicants have found that such monitoring or control is particularly advantageous for steps performed in continuous mode, but may also be advantageous for steps performed in batch or semi-batch mode. In addition, the monitoring results obtained during or after performing steps in the method according to the present invention are preferably also useful for monitoring and/or controlling other steps as part of the method according to the present invention, and/or of processes carried out upstream or downstream of the process of the present invention, as part of an overall process of which the process of the present invention is only a part. Preferably, the entire process as a whole is monitored electronically, more preferably by at least one computer program. Preferably, the method as a whole is electronically controlled as much as possible. Applicants prefer that the computer controller also provides for data and instructions to be passed from one computer or computer program to at least one other computer or other computer program or other module of the same computer program, for monitoring and/or controlling other processes, including, but not limited to, the methods described herein.
    EXAMPLE 1 In this example 1, an oven equipped with 3 plasma generators was used. The furnace, also referred to as “the device”, “the reactor” or “the fumigation installation”, had a total height from the bottom to the inlet opening at the top of approximately 7.34m. The top of the furnace was formed by a dome enclosing the top inlet and the exhaust gas discharge line. Below the upper dome, which was 1.09 m high, the furnace comprised an upper section, which was cylindrical about a vertical axis, approximately 3.00 m high and 5.50 m in outer diameter. that upper section tapped the furnace downwards for a distance in height of about 1.66 m, terminating in a lower cylindrical section with a diameter of about 3.19 m and a height of 1.00 m. dome had a height of 0.60m. The lower cylindrical section had a height of 1.00 m, and the tapered section a height of 1.66 m. During operation, the furnace was expected to contain a molten liquid bath to at least above the highest opening of the access points of the furnace. Plasma grade first hot gases and the extra hot gases. To this end, Applicants prefer to maintain a liquid level in the furnace that is at least as high as the bottom of the tapered section. More preferably, the liquid level is held slightly higher, somewhere near the tapered section. If necessary, the level can be allowed to rise above the tapered section, but it should remain below the level where the static pressure becomes too great a burden for the introduction of the first hot gases and/or the additional gases, such that the agitation of the bath would suffer as a result.
    The furnace housing was a double-walled, water-cooled alloy steel construction, except for areas well protected by a refractory lining, and the space within the double walls was supplied with running cooling water during operation as part of a circulating pump circuit. This cooling is provided to protect the structural integrity, in particular the mechanical strength, of the reactor wall. The cooling also causes part of the liquid slag in the furnace to solidify against a wall in a so-called "freeze lining", below the liquid level, but also against the majority of the furnace wall above the liquid level due to splashing. This solid freeze coating protects the walls against many forms of chemical and mechanical wear. It also provides thermal insulation, thus reducing the amount of heat that can be lost from the furnace contents to the cooling water. Since a molten metal phase can also be formed during the process, the lower cylindrical section and lower dome were coated with a suitable refractory material, in this case a combination of insulating blocks, wear lining and refractory concrete. Most of those sections were not included in the water cooling system.
    In the wall of the lower cylindrical section, and thus below the liquid level during operation, three (3) plasma generators (PG) were provided along the periphery at the same height and approximately equal distances for injecting their hot gases into the oven via blowpipes in a direction perpendicular to the oven wall.
    A plasma generator is a device that produces very hot gas, which is at least partially transformed into plasma. Typical gas temperatures are 3500-5000°C. This gas is heated by electrical energy. A high voltage difference across two electrodes creates an electric arc between the electrodes. In this reactor, air was blown through the arc during operation and heated by the energy of the arc. As the electric current is increased, more air can be heated and more power can be transferred to the air. The power of the PG (W — expressed in watts) is defined as voltage (V — volts) * electric current (A — amps). In the operation of this type of plasma, there is a proportionality between the rated power of the PG and the amount of air that can be blown through the PG.
    The three plasma generators of the reactor in the example had a nominal power of 3 MW, and during the operation of the furnace, each of them was supplied with an amount of compressed air in the range of 300-900 Nm#/hr. At the reference enthalpy of 3.5 kWh/Nm3 for the gas produced, the plasma generators were each capable of handling 857 Nm of such plasma-grade hot gases as “primary gas”.
    The PGs were not mounted directly in the reactor wall. They blew their first hot gases (plasma-driven and plasma-grade) into the furnace through a blowpipe. The blowpipe is a nozzle that forms an opening in the reactor through which the hot gases in the reactor can be fed. This blowpipe can further be used to mix secondary volumes of natural gas and/or additional air into the hot gases from the PG, if necessary. Preferably, Applicants maintain a significant volume of secondary gases through the blowpipe at all times when a hot liquid bath is present in the furnace.
    The purpose of this is that, even if the PG should be turned off and/or removed, sufficient gas remains through the blowpipe to prevent the hot liquid from entering the blowpipe, and to avoid the risk of liquid would flow upstream into the blowpipe, where it would be cooled and cured, creating a significant burden because it must be removed before the blowpipe is fully fit for its intended use.
    During operation, an additional 90-200 Nm#/hr of natural gas was added to the first hot gases from each PG through holes in the corresponding blowpipe. Also, additional air was usually added, at a flow rate in the range of 100-250 Nm 2 /h, through each of the blowpipes. These volumes therefore count as secondary gas volumes.
    The natural gas used in this example comprised 84.206 volume % methane, 3.646 volume % ethane, 0.572 volume %
    propane and 9.966 volume % nitrogen. The remaining <1% by volume consisted of higher alkanes, mainly butanes and pentanes.
    Opposite each combination of plasma generator and blowpipe, an additional blowpipe was provided for injecting additional gas into the furnace, so also 3 for the entire furnace. Those additional blowpipes or injectors are the second submerged injectors according to the present invention. They were also arranged to inject their additional gases in a direction perpendicular to the furnace wall, but a change of the preferred option for injecting at an upward angle is planned. in the bath.
    The second submerged injectors were made using a blowpipe of the same type that was also used downstream of the plasma generators. These blowpipes, and therefore also the blowpipes downstream of the PGs, are water-cooled, they are cylindrical, double-walled, and protrude through the furnace wall into the furnace space below the level of the liquid bath expected in the furnace during operation. The blowpipes are designed for injecting secondary gases into the double wall of the blowpipe. The inner cylinder of the blower pipe is provided with a plurality of holes that allow the secondary gases to penetrate into the central volume of the blower pipe through which the primary gases flow, which in the case of an upstream PG are the plasma grade hot gases contained in the PG. are generated by themselves. The holes are preferably provided as spouts to give the gas additional velocity to promote mixing of the secondary gases with the primary gases flowing through the blowpipe. In the second submerged injectors, the PG was replaced by a simple pipe extending through the blowpipe toward the liquid bath, preferably extending as far as the blowpipe extended into the furnace. The primary gas, such as compressed air, could be forced through that pipe, possibly supplemented with a quantity of natural gas. An amount of additional reducing agent, such as coal in the form of fine powder, may be admixed into the primary gas or one of its components.
    During operation, each of the three additional injectors was supplied with a quantity of the total primary and secondary gases of 300-600 Nm /h of compressed air in which a quantity of 30-60 Nm /h of natural gas was mixed and, if applicable , about 150-200 kg/h of coal powder as an additional reducing agent. The coal powder had an average particle size of 120 µm. The gas pressure upstream of the additional blowpipe was 6bar gauge. The gas velocity in the additional blowpipe was generally higher than 330 m/s during operation. A double pressurized barrel system was used to inject the coal powder. The top vessel acted as a pressure lock: it remained at atmospheric pressure while being filled from a hopper located on top of the pressure vessel, usually via a dump valve. The hopper was filled by means of mechanical transport, usually with the aid of a feed belt or screw, but possibly also by unloading large bags. After filling, this vessel was pressurized to the injection pressure. Subsequently, the lower vessel, which is kept at the injection pressure, could be filled by pouring contents of the upper vessel into the lower vessel. A weight controlled feed system was provided to feed the coal powder from the lower vessel into the injection air. Air and coal powder were then pressure transported to the additional injectors and into the liquid slag. The advantage of the double vessel system is that the inflow of reducing agent into the reactor could be arranged to be uninterrupted. The blowpipes, plasma generators and injectors were all water cooled.
    A radiant water cooler was provided on top of the furnace, in the form of a double-walled metal cylinder in which the exhaust gases from the furnace flow through the center of the cylinder, and cooling water is forced through the wall of the cylinder.
    Ambient air is admitted between the top of the furnace and the radiant water cooler to mix with the furnace exhaust. The vaporized zinc and CO present in the gas come into contact with the oxygen in the air; at the high temperature of the gas, these substances ignite spontaneously and form an afterburning zone. Due to the significant draft in the furnace and water cooler, the exhaust gases flow at a high speed. The ambient air is let in through specially designed openings in such a way that the air mixes quickly and intensively with the exhaust gases. As a result, a stable flame front is formed within the radiant water cooler and some of its radiant heat is radiated back down from the post-combustion zone into the furnace onto the liquid bath in the furnace. The top of the furnace and radiant water cooler are also provided with a plurality of injection points through which pressurized air can be injected into the furnace exhaust. That capability can be used simultaneously with the entry of ambient air through the openings. Preferably, however, the openings to admit the ambient air are substantially closed, and substantially all of the necessary oxygen is introduced through the injection points. This mode of operation is preferred because the oxygen supply is more stable and controllable than the alternatives in which draft air is admitted.
    In the afterburner zone, the gas reaches temperatures of up to 1500°C.
    The gas leaving the post-combustion zone was at a temperature of about 1200°C. Downstream of the radiant water cooler, about 6-7000 liters/hour of water was injected into the gas stream. This spray cooling step lowers the temperature of the gas to about 220°C.
    The wet gas from the spray cooling step was passed to a gas filter in which porous sleeves in PTFE are provided over cylindrical stubs, and the sleeves retain the dust generated by the oxidized form of the vaporizable metal or the vaporizable metal compound formed in the post-combustion zone. .
    Downstream of the gas filter is a fan which provides the exhaust from the furnace and which blows the filtered gas into the emission chimney.
    The fumigation process and the oven were used in batch mode. The workloads reported below consisted of a precisely defined sequence of distinguishable process steps. During the various process steps, more or less electrical power, coal powder, air and natural gas was fed into the reactor, depending on the desired effect. The operation of the PGs, blowpipes and additional injectors — or blowpipes — varied according to the process step. The different steps are now described in detail.
    First Process Step: Filling the Furnace with Liquid: At the start of the charge, 76900 kg of liquid slag from the upstream copper smelter was fed into 4 slag pots with a net weight of about 19 tons each, measured by the weighing device on the bridge crane transferring the slag pots between different furnaces.
    In the upstream copper smelter, the slag is well mixed before being poured out of the smelting furnace. The slag composition can therefore be considered homogeneous. The composition of most metals in the slag was measured by inductively coupled plasma atomic emission spectroscopy (ICP-AES), also called inductively coupled optical emission spectrometry (ICP-OES), and sometimes simply ICP, and for SiO2 by X-ray diffraction (X-ray). diffraction, XRF). The XRD technique used was quantitative X-ray diffraction analysis using Topas Academic software V5, with Al»Os as internal standard.
    Table I: Composition of feed slag | Qu | 080 | |. PM 046 | SO 000 | LA | 000 | LB | 000 | |. MB | 000 | |. 8b | 000 | For this process step, the PGs were set at a power level of 1400 kW each, and an average airflow of about 437 Nm 3 /h per PG as primary gas.
    In addition, the following secondary gases were used.
    The flow of natural gas through the blowpipe was set at 125 Nm®/h.
    The air flow through the blower pipe was set at a level of 100 Nm 3 /h.
    The total flow of primary and secondary gases through the additional injectors as the second submerged injectors was set per injector at 380 Nm 3 /h air, natural gas was added at a flow rate of 44 Nm 3 /h.
    The injection of coal powder has not yet been activated in this process step.
    Second method step: fumigation step After filling the liquid slag, the fumigation step was started.
    In that step, the input of energy and reducing agent was increased to promote the volatilization of zinc as a vapor.
    The PGs were set at a power level of 2500 kW each, and an average primary airflow of 714 Nm#/h per PG. In addition, the following secondary gases were used. Natural gas was added to each of the blowpipes downstream of the PGs at a flow rate of 148 Nm#/hr. The additional airflow through the blowpipe was set at 100 Nm#/h.
    The total flow of primary and secondary gases through the additional injectors was fed with air at 380 Nm#/h per injector. Natural gas was added to each injector at 44 Nm#/hr. The injection of coal powder to each injector was set at 180 kg/hr.
    The supply of energy and reducing agent resulted in fumigation of volatile compounds from the liquid slag. The most volatile element was Zn. It was present in the slag as zinc oxide (ZnO). The temperature in the reactor was maintained in the range of 1180-1250°C, which kept the slag flowing. Thanks to the various reducing agents, i.e. the coal powder and the various feeds of natural gas, ZnO was reduced to metallic zinc (Zn). At atmospheric pressure, Zn can be vaporized at a temperature above 906°C. Thus, Zn evaporated from the slag bath and was transported as part of the furnace process gases to the furnace exhaust gas treatment equipment.
    Large amounts of air were mixed with the process gases in the reactor waste gas discharge line, resulting in complete post-combustion of the process gases. Any remaining CO, Zn, Hz was completely oxidized in that step. The zinc in vapor form oxidizes to ZnO and forms a solid particle. This ZnO thus formed a substance in the incinerated process waste gas stream. This post-combustion or post-combustion step is followed by a cooling step. At the exit of the cooling step, the temperature of the process gases was less than 220°C. The process gases were then filtered in a bag filter with PTFE cloths. After the filtration, the process gases were vented to the atmosphere through a chimney. The ZnO dust particles were recovered in the filter, cooled and stored in a dust silo. From the silo, the Zn-rich dust product could be dumped into silo trucks for sale.
    Samples were taken during fumigation and analyzed with the fast but slightly less accurate method XRF. When the desired level of Zn in the slag in the furnace was reached, the fumigation was stopped and the trimming step was started.
    Third Process Step: Trimming The purpose of this step was to oxidize the last remaining coal powder in the furnace charge and to heat the slag to a more appropriate tapping temperature. The target temperature was 1220-1250°C.
    The PGs were operated at a power level of 2500 kW each, and with an average primary airflow of 714 Nm#h per PG. In addition, the following secondary gases were used. The flow of natural gas through the blowpipe was set at 102 Nm 3 h. The airflow through the blowpipe was set at 100 Nm#/h.
    As the total flow of primary and secondary gases through the additional injectors, these second submerged injectors were each fed with 380 Nm 3 /h air and 44 Nm 3 /h natural gas. The injection of coal powder was interrupted during this trimming step. No slag sample was taken after the completion of the trimming step. Draining was immediately started. Fourth process step: tapping and pelletizing the slag The aim of this step is to extract the liquid slag from the reactor. The tap hole located in the side of the reactor was opened by drilling and the liquid slag was allowed to flow out of the reactor in a flume. From that flume, the slag product was pelletized by means of a water pelletizing system, in which a large volume of water was sprayed into the falling slag stream, whereby the liquid slag solidified and the solid formed disintegrated into particles of +1 mm. The PGs continued to operate at a power level of 2000 kW each during this tapping and pelletizing step, with an average primary airflow of 606 Nm#/hr per PG. As secondary gases, a flow of natural gas to the blower pipe of 128 Nm 3 /h was set, and then an air flow directly to the blower pipe was set at 100 Nm 3 /h.
    The additional injectors also continued to operate with air at a flow rate of 380 Nm#/h per injector and natural gas at 44 Nmÿ/h in total for primary plus secondary gases. The injection of coal powder was interrupted.
    Samples were taken of the final product after pelletizing. The composition is considered to be close to the composition of the slag immediately after the fumigation step.
    Additional operating parameters for the PGs in each process step are shown in Table II, in which the “Enthalpy” is calculated based on the power supplied to the PG and the airflow supplied to the PG.
    Table II: PG operating parameters air/natural gas KWh/Nm | Trimming | 8 | 35 | The evolution of the slag composition during loading is illustrated by Table III, which shows the results of analyzes of slag samples taken after each step: Table III: Evolution of the slag composition Filling Fumigation processed e= | 06 | 057 | 0 | 0%. CU ® | 06 | 04 | 008 | 0025. Output material composition This batch yielded approximately 10500 kg of filter dust, having a composition as shown in Table IV, the result of an ICP analysis of a representative sample:
    Table IV: Composition of filter dust product cu | 0 | [Sn | 0m [ ®% | 28 N [000 ou | 0 | [as | 000 | ss» | 00 [ @ | 00
    For comparison, a second batch was processed during which the additional blowpipes had not yet been installed. To provide an equal amount of reducing agent during the fumigation step, the same amount of carbon was added by introducing coarse petcoke with a particle size in the range of 6 mm through the feed opening.
    The amount and composition of liquid slag feed is very similar to the first charge, as is the time of feeding, trimming and draining. It was mainly the duration of the fumigation that differed.
    The amounts and compositions of the product after pelletizing and of the filter fabric were comparable.
    The time required for the fumigation step to obtain a very similar Zn content in the final slag was significantly longer in this comparative batch compared to the batch according to the invention described above. That is, the comparative charge had a significantly lower zinc fumigation rate compared to the working example, and thus the present invention significantly increased the zinc fumigation rate during the fumigation step.
    EXAMPLE 2 In this Example 2, the same furnace was used as in Example 1, but with a different configuration with respect to the second submerged gas injection. The natural gas supply was the same, as was its quality.
    At the same level or height as the three plasma generator blowpipe combinations, only one additional injector blowpipe combination was provided this time, as a single second submerged injector for injecting additional gas and fine coke into the furnace. The blowpipe was cooled with water and a constant flow rate of 350-400 Nm 3 /h of air was injected through the blowpipe and then through the holes in the inner wall of the blowpipe. The natural gas supply was not used in this example.
    The injector in the additional injector-blast tube combination fed additional gases into the liquid slag bath in a direction perpendicular to the furnace wall. During operation, an amount of 100-400 Nm·h of compressed air was supplied as primary gases to the additional injector, in which, if applicable, an amount of about 100-700 kg/h of coal powder was admixed as additional reducing agent. The coal powder had an average particle size of 120 µm. The pressure of the compressed gas upstream of the second submerged injector assembly was 6 bar gauge.
    The gas velocity in the additional injector-blast nozzle combination was usually higher than 150 m/s during operation. First Process Step: Filling the Furnace with Liquid: The same procedure, grades and amounts were used as in the corresponding step as part of Example 1, with the following exceptions.
    The flow of secondary gases through the one additional blowpipe as part of the one additional injector-blowpipe combination was set at 350 Nm 3 /h air, and no natural gas was added. The flow of primary gases through the additional injector as part of the one additional injector-blast nozzle combination was set at 200 Nm#/h air. The fine coke injection was not yet activated in this process step.
    Second Process Step: Fumigation Step The same procedure as in Example 1 was used.
    The PGs were reset to a power level of 2500 kW each, and an average primary airflow of 714 Nm#h per PG. In addition, the following secondary gases were used. Natural gas was added to each of the blowpipes downstream of the PGs at a flow rate of 148 Nm 3 /h. The additional airflow through the blowpipe was set at 100 Nm#/h.
    The secondary gas flow through the additional blowpipe as part of the one additional injector-blowpipe combination was 350 Nm#/h air, to which no natural gas was added. As the primary gas, the flow through the additional injector as part of the additional injector-blowing tube combination was set at 200 Nm 3 /h air. The fine coke injection was set at 700 kg/hr in this process step.
    The temperature in the reactor was maintained in the range of 1180-1250°C, which kept the slag flowing. Thanks to the various reducing agents, i.e. the coal powder and the various feeds of natural gas, ZnO was reduced to metallic zinc (Zn). Thus, Zn evaporated from the slag bath and was transported as part of the furnace process gases to the furnace exhaust gas treatment equipment.
    Samples were taken during fumigation and analyzed with the fast but slightly less accurate method XRF. When the desired level of Zn in the slag in the furnace was reached, the fumigation was stopped and the trimming step was started.
    Third method step: trimming The target temperature was again 1220-1250°C.
    The PGs were operated at a power level of 2500 kW each, and with an average airflow of 714Nm3%h per PG. In addition, the following secondary gases were used. The flow of natural gas through the blowpipe was set at 102 Nm#/h. The airflow through the blowpipe was set at 100 Nm#/h.
    The secondary gas flow through the additional blowpipe as part of the one additional injector-blowpipe combination was set at 350 Nm#h air, and no natural gas was added. The primary gas flow through the additional injector as part of the one additional injector-blast nozzle combination was set at 200 Nm#/h air. The fine coke injection was not yet activated in this process step.
    No slag sample was taken after the completion of the trimming step. Draining was immediately started. Fourth process step: tapping and pelletizing the slag The same procedure as in Example 1 was used.
    The PGs continued to operate at a power level of 2000 kW each during this tapping and pelletizing step, with an average primary airflow of 606 Nm#/h per PG. As secondary gases, a flow of natural gas to the blowpipe of 128 Nm#h, and an air flow directly to the blowpipe of 100 Nm#/h were used.
    The flow of secondary gases through the additional blowpipe as part of the one additional injector-blowpipe combination was 350 Nm 3 h air, and no natural gas was added. The primary gas flow through the additional injector as part of the one additional injector-blast nozzle combination was set at 200 Nm#/h air. The fine coke injection was not yet activated in this process step.
    Samples were taken of the final product after pelletizing. The composition is considered to be close to the composition of the slag immediately after the fumigation step.
    The additional operating parameters for the PGs in each method step were the same as those shown in Table | as part of Example 1.
    The final results of this example were very close to those of Example 1, only this time they were again obtained in a shorter time than with the batch processed as part of Example 1 for comparison.
    Applicants determined that a significant increase in production rate could be obtained with the embodiments of the present invention, also with Example 2. Applicants believe that this effect is due to a combination of (|) stronger agitation of the bath, ( ii) more stripping gas, (iii) more reducing agent, and, probably most importantly, (iv) using a solid form reducing agent with a much smaller particle size such that the reducing agent is much more reactive. This effect makes it possible to achieve the intended fumigation conditions much more quickly than with the coarse petcoke. The combination of the beneficial effects allowed the fumigation step to go into full effect much more quickly, as evidenced by the much faster increase in heat to be dissipated from the post-combustion zone, and also that the duration of the trim step was very could be shortened, almost an order of magnitude, because the time it took could be shortened from about a quarter of an hour to just 2-3 minutes. The fumigator with the second submerged injector(s) was able to operate more stably, at a higher throughput, and closer to the maximum of its power.
    Having fully described the present invention, it will be apparent to those skilled in the art that the invention can be practiced with a wide range of parameters within the scope of the claims, without departing from the scope of the invention as defined by the claims.
    权利要求:
    Claims (71)
    [1]
    A single-chamber furnace for fumigating at least one vaporizable metal or metal compound from a metallurgical charge, comprising a bath furnace capable of containing a molten charge to a certain level, the furnace being equipped with at least one plasma torch with non-transferring arc for generating first hot gases of plasma quality and having at least one first submerged injector for injecting the first hot gases from the plasma torch below the determined level, the furnace further comprising an afterburning zone for oxidizing said at least one vaporizable metal or the at least one vaporizable metal compound in the flue gas to generate an oxidized form of the at least one vaporizable metal or the at least one vaporizable metal compound, and a recovery zone for recovering the oxidized form of the at least one vaporizable metal or the at least one vaporizable metal compound from the gas formed in the post-combustion zone, characterized in that the furnace is further provided with at least one second submerged injector different from the first submerged injector for injecting additional gas into the furnace below the determined level.
    [2]
    The furnace of claim 1 wherein the apparatus is arranged to inject, through the at least one second injector, a total amount of additional gas which is at least 10% of the amount of first hot gases that can be generated by the one element of the at least one highest power plasma torch when that torch delivers first hot gases with an enthalpy content of at least 3.5 kWh/Nm3, expressed in volumetric units under normal conditions.
    [3]
    The furnace of claim 1 or 2 comprising a plurality of second injectors, each injector being arranged to inject, through each second injector, an amount of additional gas which is at least 10% of the amount of first hot gases which can generated by the one element of the at least one highest power plasma torch when that torch delivers first hot gases with an enthalpy content of at least 3.5 kWh/Nm3, expressed in volumetric units under normal conditions.
    [4]
    The furnace according to any one of the preceding claims, connected to at least one compressed gas supply and/or equipped with a compressor for supplying compressed gas to the at least one second injector.
    [5]
    The furnace of any preceding claim wherein the additional gas supply source for the device comprises a source of a gas selected from the group consisting of hydrogen, nitrogen, air, carbon dioxide, argon, neon, helium, methane, ethane, propane, butane and combinations thereof, preferably nitrogen or air, more preferably air, even more preferably compressed air.
    [6]
    The furnace of any preceding claim comprising means for thermally treating the additional gas upstream of the at least one second injector to alter its enthalpy content, the means for thermally treating the additional gas preferably comprises at least one heat exchanger.
    [7]
    The furnace of any preceding claim, further comprising means for incorporating a reducing agent into the additional gas upstream of the at least one second injector.
    [8]
    The furnace of the preceding claim wherein the reducing agent to be introduced may be selected from a gas, a liquid, a solid, and combinations thereof.
    [9]
    The furnace according to any one of the preceding claims, comprising means for controlling the lambda value of the additional gas to be injected into the bath by the second injector.
    [10]
    The furnace according to any one of the preceding claims, which is equipped to inject, as part of the supplemental gas, oxygen and a gaseous or liquid fuel, and to allow the velocity of the supplemental gas in the at least one second injector, or at some other location upstream thereof, exceeds the flame propagation rate of the fuel as part of the additional gas.
    [11]
    The furnace of the preceding claim, further being equipped to limit the amount of fuel injected such that combustion of the injected fuel under the intended operating conditions for the furnace causes an increase in the enthalpy of the additional gas such that the additional gas at the injection point in the bath is at a temperature not exceeding the temperature of the molten charge intended to be in the furnace during operation.
    [12]
    The furnace according to any one of the preceding claims, wherein the at least one second injector directs its additional gas to a second volume, as part of the interior space of the furnace below the predetermined level, which is different from the first volume in which the at least one first injector directs the first plasma grade hot gases.
    [13]
    The furnace of any preceding claim wherein the at least one first injector is located in the side wall of the furnace, the at least one second injector is located in the furnace wall opposite the at least one first injector, at preferably along the horizontal outer edge of the furnace, extending substantially the same height as the at least one first injector.
    [14]
    The furnace according to any one of the preceding claims comprising at least two and preferably at least three first injectors distributed along a horizontal outer edge of the side wall of the furnace, the at least one second submerged injector being additional gas directed to a volume as part of the interior space of the furnace below the predetermined level, approximately close to the vertical axis of the furnace, and/or the at least one second submerged injector is located along the side wall of the furnace at approximately equal distance between the locations of the two nearest of the at least two first injectors.
    [15]
    The furnace of any preceding claim, further being equipped for introducing a reducing agent into the first hot gases upstream of the at least one first injector.
    [16]
    The furnace of the preceding claim wherein the reducing agent to be introduced upstream of the at least one first injector may be selected from a gas, a liquid, a solid, and combinations thereof.
    [17]
    The furnace of any preceding claim, further comprising at least one oxygas burner for generating additional first hot gases in addition to the amount of plasma grade first hot gases from the at least one plasma torch.
    [18]
    The furnace of the preceding claim, further comprising at least one submerged third injector for injecting the additional first hot gases below the determined level.
    [19]
    The furnace of the preceding claim wherein the at least one oxygas burner is below the determined level.
    [20]
    The furnace of any preceding claim wherein the plasma torch is below the determined level.
    [21]
    The furnace according to any one of the preceding claims, wherein the post-combustion zone is provided above the determined level as part of the single chamber furnace.
    [22]
    The furnace according to any one of the preceding claims, wherein the post-combustion zone comprises connection to a supply source of an oxygen-containing gas, preferably selected from air, oxygen-enriched air and purified oxygen gas.
    [23]
    The furnace of any preceding claim, further comprising a cooling zone for cooling the gas generated in the post-combustion zone upstream of the recovery zone.
    [24]
    The furnace of any preceding claim wherein the recovery zone comprises a gas filter zone,
    wherein the gas filter zone preferably comprises at least one gas filter cloth.
    [25]
    The furnace according to any one of the preceding claims, wherein the furnace has a generally cylindrical shape, the furnace preferably also having a conical lower portion which tapers to a cylindrical lower portion of a smaller diameter, wherein the cylindrical shape of the furnace has a largest internal diameter d and the furnace has an overall internal height h, from bottom to top, the ratio of h to d being at least 0.75.
    [26]
    The furnace of the preceding claim wherein the furnace includes the conical lower portion and wherein the defined level is approximately at the level where the cylindrical shape merges into the conical lower portion.
    [27]
    The furnace of any preceding claim wherein the furnace is provided with an internal refractory lining.
    [28]
    The furnace of any preceding claim wherein the outer walls of the furnace are water cooled.
    [29]
    A method of fumigating at least one vaporizable metal or vaporizable metal compound from a metallurgical charge using the furnace according to any one of the preceding claims, comprising the steps of: introducing the metallurgical charge containing it at least one vaporizable metal or the at least one vaporizable metal compound contained in the furnace and forming a bath of molten charge to the determined level; fumigating an amount of at least one vaporizable metal or metal compound from the bath using the plasma-grade hot gases from the at least one plasma torch and at least one reducing agent to produce flue gas containing the vaporizable metal or metal compound;
    ° post-combustion of the flue gas in the post-combustion zone to oxidize the at least one vaporizable metal or metal compound to an oxidized form of the at least one vaporizable metal or metal compound, ° extract from the furnace of the gas generated in the furnace and recovering the oxidized form of the at least one vaporizable metal or the at least one vaporizable metal compound from the gas generated in the post-combustion step; characterized in that, during at least part of the fumigation step, additional gas is injected through the at least one second injector into the bath and below the determined level, thereby increasing the amount of flue gases comprising the vaporizable metal or metal compound .
    [30]
    The method of the preceding claim wherein the amount of additional gas injected via the at least one second injector is at least 10% of the amount of first hot gases that can be generated by the one element of the at least one plasma torch with the highest power when that torch delivers first hot gases with an enthalpy content of at least 3.5 kWh/Nm3, expressed in volumetric units under normal conditions.
    [31]
    The method of any of claims 29-30, wherein the furnace comprises a plurality of second injectors, and wherein the amount of additional gas injected through each second injector is at least 10% of the amount of first hot gases emitted. may be generated by the one element of the at least one highest power plasma torch when that torch delivers first hot gases with an enthalpy content of at least 3.5 kWh/Nm3, expressed in volumetric units under normal conditions.
    [32]
    The method of any one of claims 29-31 wherein the additional gas injected through the at least one second injector comprises at least one gas selected from the group consisting of hydrogen, nitrogen, air, carbon dioxide , argon, neon,
    helium, methane, ethane, propane, butane and combinations thereof, preferably nitrogen or air, more preferably air, even more preferably compressed air.
    [33]
    The method of any of claims 29-32 wherein the additional gas injected through the at least one second injector is thermally treated upstream of the at least one second injector to alter its enthalpy content, wherein the thermal treatment of the additional gas is preferably carried out using at least one heat exchanger.
    [34]
    The method according to any one of claims 29-33, wherein the temperature of the additional gas entering the at least one second injector is at most equal to the temperature of the bath in the furnace, preferably at least 100 degrees. degrees Celsius below the temperature of the bath.
    [35]
    The method of any of claims 29-34 wherein the additional gas injected via the at least one second injector comprises at least one first reducing agent.
    [36]
    The method of the preceding claim wherein the first reducing agent is a solid.
    [37]
    The method of any of claims 29-36 wherein the additional gas injected through the at least one second injector further comprises oxygen and an amount of fuel suitable for combustion under the operating conditions in the furnace, contribute an enthalpy supply to the furnace that compensates for at least 50% of the cooling effect that the additional gas may have on the furnace in the event that the additional gas at the injection point is at a temperature lower than the temperature of the molten charge in the furnace.
    [38]
    The method of any of claims 29-37 wherein the additional gas injected through the at least one second injector has a lambda value of less than 1.0.
    [39]
    The method of any one of claims 29-38 wherein the additional gas injected through the at least one second injector is combustible and the additional gas in the at least one second injector reaches a velocity greater than the flame propagation rate of the additional gas.
    [40]
    The method of any one of claims 29-39 wherein the at least one vaporizable metal or the at least one vaporizable metal compound is a metal in its elemental form or is a vaporizable compound containing a metal, wherein the metal at is preferably selected from the group consisting of zinc, lead, tin, bismuth, cadmium, indium, germanium, and combinations thereof, and also the metallic compound is preferably selected from a chloride, an oxide, a sulfide, and combinations thereof.
    [41]
    The method according to the preceding claim wherein a metal which is less noble than the metal in the vaporizable metal or in the vaporizable metal compound is added in the furnace, preferably iron and/or aluminum.
    [42]
    The method of any one of claims 29 to 41 wherein a second reducing agent is added to the first plasma grade hot gases upstream of the at least one first injector.
    [43]
    The method of the preceding claim wherein the second reducing agent is selected from a gas, a liquid and a solid, and combinations thereof.
    [44]
    The method of any one of claims 29 to 43 comprising the step of adjusting the oxygen potential in the slag in the range of 10 to 10° Pa.
    [45]
    The method of any one of claims 29 to 44 wherein the post-combustion is performed in the single-chamber furnace.
    [46]
    The method according to any one of claims 29 to 45, wherein the post-combustion comprises introducing into the post-combustion zone an oxygen-containing gas, preferably selected from air, oxygen-enriched air and purified oxygen gas.
    [47]
    The method of any one of claims 29 to 45 wherein the oxidized form of the at least one vaporizable metal or the at least one vaporizable metal compound is recovered from the gas as dust.
    [48]
    The method of any one of claims 29 to 47, wherein the recovery of the oxidized form of the at least one vaporizable metal or the at least one vaporizable metal compound from the gas comprises filtering the gas containing the oxidized form of the at least one vaporizable metal or the at least one vaporizable metal compound, using a filter, preferably a filter cloth.
    [49]
    The method of any one of claims 29 to 48 further comprising a cooling step upstream of the recovery of the oxidized form of the at least one vaporizable metal or the at least one vaporizable metal compound from the gas.
    [50]
    The method of any one of claims 29 to 49 comprising forming a molten metal phase, the method further comprising the step of removing the molten metal phase from the furnace.
    [51]
    The method of any of claims 29 to 50 wherein the metallurgical charge comprises a slag and wherein the slag comprises sulfur and/or sulfur compounds, the method further comprising the step of forming a molten matte phase and a further step of removing the molten matte phase from the furnace.
    [52]
    The method of any one of claims 29 to 51 wherein the metallurgical charge is introduced into the furnace as a liquid.
    [53]
    The method of any one of claims 29 to 52 wherein the metallurgical charge is a metallurgical slag and wherein the method produces a second slag.
    [54]
    The method of the preceding claim wherein the molten slag has an average temperature of less than 50 degrees Celsius above the liquidus temperature of the slag.
    [55]
    The method of any one of claims 53 to 54, wherein an oxide selected from CaO, Al2O3, and combinations thereof is added to the bath in the furnace, preferably at a temperature in the bath of at least 1000°C, preferably about 1150°C.
    [56]
    The method of any one of claims 53-55 further comprising the step of cooling the second slag to become a solid, preferably first removing the second slag from the furnace as a liquid.
    [57]
    The method of the preceding claim wherein the cooling is performed by contacting the liquid second slag with water.
    [58]
    The method of any of claims 56-57 wherein the second slug is cooled at a rate of at least 30 degrees Celsius per second.
    [59]
    The method according to any one of claims 56-58 further comprising the step of grinding the solid second slag, preferably grinding the second slag into powder.
    [60]
    The method of any of claims 56-59 wherein the second slug is cooled at a rate of less than 40 degrees Celsius per second.
    [61]
    The method of any one of claims 56-60 further comprising the step of adding the second slag as a binder or aggregate during the production of an article for the construction industry.
    [62]
    The method of the preceding claim wherein the slag is used as a binder and the article further comprises an aggregate, the aggregate preferably comprising sand and/or the second slag.
    [63]
    The method of the preceding claim further comprising adding an activator during the production of the article.
    [64]
    The method of the preceding claim wherein the activator is selected from the group consisting of sodium hydroxide, NaOH, potassium hydroxide, KOH, sodium silicate, Na 2 SiO 3 , potassium silicate, K 2 SiO 3 , and combinations thereof.
    [65]
    The method of any one of claims 61-64 wherein the construction industry article is a building element.
    [66]
    The method of the preceding claim, wherein the building element is selected from the list of a tile, a paving stone, a block, a concrete block, and combinations thereof.
    [67]
    The method of any one of claims 61-66 wherein the construction industry article has a foamed structure.
    [68]
    Use of the furnace according to any one of claims 1 to 28 for fumigating at least one vaporizable metal or vaporizable metal compound from a metallurgical charge.
    [69]
    The use of the preceding claim wherein the metallurgical charge is selected from a copper smelting slag and a copper refining slag and combinations thereof.
    [70]
    The use of any one of claims 68-69 wherein the vaporizable metal or metal compound is selected from zinc, lead, tin, bismuth, cadmium, indium, germanium, and combinations thereof.
    [71]
    The method according to any one of claims 29-67, wherein at least part of the method is monitored and/or controlled electronically, preferably by a computer program.
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    同族专利:
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    BE1027793A1|2021-06-18|
    引用文献:
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    法律状态:
    2021-07-19| FG| Patent granted|Effective date: 20210623 |
    优先权:
    申请号 | 申请日 | 专利标题
    EP19210907|2019-11-22|
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