Method for pyrometallurgical smelting of metal-containing raw materials, waste materials and / or secondary waste materials

Abstract

To provide a method that enables better regulation of highly exothermic processes during pyrometallurgical smelting of metal-containing raw materials, waste materials and / or secondary waste materials.SOLUTION: The present disclosure relates to a method for the pyrometallurgical smelting of metal-containing raw materials, waste materials and / or secondary waste materials M, where the materials are fed in shredded form to a smelting unit 1 which includes a smelting zone 6 and main and secondary reaction zones 7, 8 and are smelted such that a liquid melt phase 9, a liquid slag phase 10 and a gas phase are formed. An oxidizing, reducing and / or inert gas and / or gas mixture G is supplied in compressed form via at least one injector 11 and expanded adiabatically within the smelting unit 1, and is then injected as adiabatically expanded gas and / or gas mixture into the liquid slag phase 10 so as to achieve a prescribed cooling effect.SELECTED DRAWING: Figure 1

Description

[Technical Field]

[0001] The present invention relates to a method for the pyrometallurgical melting of metal-containing raw materials, residual materials and / or secondary residual materials in the presence of an oxidizing, reducing and / or inert gas. [Background technology]

[0002] Methods for the pyrometallurgical melting of metal-containing raw materials, residue materials and / or secondary residue materials are basically known from the prior art.

[0003] The metal-containing raw materials, residue materials and / or secondary residue materials used herein usually have a significant proportion of hydrocarbons which, due to their large energy content, require intensive cooling of the melting process.

[0004] To cool the highly exothermic process, melting units with coolable reactor walls are known from the prior art. For example, Patent Document 1 discloses a method for recovering metals from secondary materials using a melt reactor. The melt reactor comprises a circular chamber defined by a coolable reactor wall. A number of oxygen lances are arranged in the reactor wall below the slag opening, offset from the center of the chamber at an angle of 5 to 60° to the horizontal, so that oxygen can be injected directly into the melt and the melt can be rotated within the circular chamber.

[0005] However, the external cooling means known from the prior art are difficult to control due to significant hysteresis and are technically very complex. [Prior art documents] [Patent documents]

[0006] [Patent Document 1] Chinese Patent Application Publication No. 104928493 [Patent Document 2] German Patent Application Publication No. 102011002616 Summary of the Invention [Problem to be solved by the invention]

[0007] The problem underlying the present invention is therefore to provide a method which allows for better control of the highly exothermic process during the pyrometallurgical melting of metal-containing raw materials, residual materials and / or secondary residual materials (M) in the presence of oxidizing, reducing and / or inert gases. [Means for solving the problem]

[0008] According to the invention, this problem is solved by a method having the features of claim 1.

[0009] In the method according to the invention for melting metal-containing raw materials, residue materials and / or secondary residue materials by pyrometallurgy, these materials are fed in pulverized form to a melting unit comprising a melting zone, a main reaction zone and a sub-reaction zone and melted in the presence of an oxidizing gas, a reducing gas and / or an inert gas and / or a gas mixture, so that a liquid molten phase, a liquid slag phase and a gas phase are formed.

[0010] The method comprises supplying an oxidizing gas, a reducing gas and / or an inert gas and / or a gas mixture under compression via at least one injector and adiabatically expanding the gas mixture in a melting unit, followed by a gas mixture under a pressure of preferably 10 J / Nm 3 The cooling effect of the present invention is achieved by injecting adiabatically expanded gas and / or gas mixture into the liquid slag phase.

[0011] The adiabatic expansion of the oxidizing, reducing and / or inert gases and / or gas mixtures or reactant gases creates a direct cooling effect inside the melting unit, which allows the energy / heat balance of the process to be controlled in a targeted manner. Thus, via adjustment of the pressure, flow and / or nozzle geometry of the injectors, preferably including Laval nozzles, a cooling effect of at least 10 J / Nm 3 cooling effect of at least 100 J / Nm 3 and even more preferably at least 1.0 kJ / Nm 3 cooling effect of at least 5.0 kJ / Nm 3 It is possible to set the adiabatic expansion of the reaction gases so that a cooling effect of 1000 kJ / s can be achieved.

[0012] Regarding the output value, this is the normal lube (Nm 3 )

[0013] The maximum achievable cooling effect is essentially physically limited by the Joule-Thomson effect, so it is possible to achieve a maximum of 100 kJ / Nm through adjustment of the injector pressure, flow and / or nozzle geometry, preferably including a Laval nozzle. 3 cooling effect, preferably up to 90kJ / Nm 3 cooling effect of 80 kJ / Nm 3 cooling effect, most preferably up to 70kJ / Nm 3 It is possible to set the adiabatic expansion of the reaction gases so that a cooling effect of 1000 kJ / s can be achieved.

[0014] It should be noted that the cooling effect described here can only be achieved with gases and / or gas mixtures that have a positive Joule-Thomson coefficient μ.

[0015] Direct cooling within the melting unit using the reaction gas, which is also used as the cooling medium, advantageously allows the extension of external cooling measures, which are usually carried out using cooling panels and / or cooling channels, thereby substantially simplifying and improving the overall cooling management. Direct cooling also allows the life of the refractory lining of the melting unit to be extended, which has a favorable effect on the operating economy of the melting unit.

[0016] Advantageous further embodiments of the invention are set forth in the respective dependent claims. The features individually recited in the independent claims can be combined with one another in any technically meaningful manner to define further embodiments of the invention. Furthermore, the features recited in the respective claims are defined and explained in detail in this specification, and further preferred embodiments of the invention are shown.

[0017] Basically, the reaction gas injected via at least one injector can be fed directly into the liquid slag phase by immersing the injector in the liquid slag phase.

[0018] However, preferably, the reactive gas is blown into the liquid slag phase through at least one injector positioned above but not in contact with the liquid slag phase in the melting unit and oriented at an angle of 5 to 85°, more preferably at an angle of 15 to 80°, even more preferably at an angle of 25 to 75°, and most preferably at an angle of 35 to 70° relative to the horizontal, so that the reactive gas is adiabatically expanded in the main reaction zone and / or sub-reaction zone of the melting unit.

[0019] This injection of the reactant gases subjects the liquid slag phase to intense turbulence, as the turbulent flow is injected into the gas phase in the sub-reaction zone located above the liquid slag phase. Surprisingly, this process achieves a surface area that is at least a factor of 5, preferably at least a factor of 6, more preferably at least a factor of 7, and most preferably at least a factor of 8, larger than the liquid slag phase, resulting in particularly intensive contact with the gas phase in the sub-reaction zone located above the liquid slag phase and greater mass and energy transfer. By positioning at least one injector at a specific angle relative to the horizontal, the liquid slag phase is subjected to additional rotation, resulting in the formation of vortices in both the main reaction zone and the sub-reaction zone, which further enhance the turbulence. This allows for a maximally turbulent environment in the melting unit, which is particularly conducive to efficient metallurgical reactions. The adiabatic expansion of the reacting gases in the melting unit again enhances the formation of a large specific surface of the liquid slag phase, which ultimately leads to particularly intensive contact with the surrounding gas atmosphere and enhances the chemical reaction and its reaction rate.

[0020] The term "non-contact" in the sense of the present invention is understood to mean that the at least one injector capable of injecting the oxidizing, reducing and / or inert gas and / or gas mixture into the melting unit is not in continuous contact with the liquid slag phase during the injection and in the process steps therebetween, but is positioned at a specific distance from the liquid slag phase and thus above the bath level throughout the process. The exception to this is the temporary contact of individual droplets of the liquid slag phase and / or the liquid melt phase, which occurs during the process depending on the strong turbulence and is therefore unavoidable.

[0021] The term "injector" is understood within the context of the present invention, unless otherwise specified, as a lance or an injection pipe formed by an essentially hollow cylindrical element.

[0022] The term "melting unit" in the sense of the present invention is understood to mean a conventional melting unit comprising a hollow cylinder, hollow cone or hollow cube standing on a circular or square base, the height of which is several times the length and width of the hollow cylinder, hollow cone or hollow cube. Preferably, therefore, the main reaction zone of the melting unit, located above the melting zone, is configured with an essentially circular and / or ellipsoidal cross section.

[0023] Other melting units known to the person skilled in the art from the prior art, such as electric arc furnaces (EAF), submerged arc furnaces (SAF) or induction furnaces, are not included in the present invention.

[0024] Advantageously, at least one injector, which injects reactive gases into the liquid slag phase without contact, has a minimum distance of 0.10 m, preferably 0.15 m, more preferably 0.20 m, even more preferably 0.25 m, and most preferably 0.30 m, from the surface of the liquid slag phase. In addition to the stirring and turbulent mixing of the liquid slag phase with the adjacent gas phase, which results in a particularly effective metallurgical reaction, the spaced apart arrangement from the liquid slag phase also results in a significant reduction in injector wear. This effectively prevents injector clogging, which requires significant and costly maintenance efforts with the solutions known from the prior art.

[0025] However, the at least one injector for injecting the reactive gas into the liquid slag phase without contact should not exceed the maximum distance from the surface of the liquid slag phase, so that advantageously the at least one injector has a maximum distance of 2.50 m, preferably 2.0 m, more preferably 1.50 m, even more preferably 1.0 m, and most preferably 0.80 m, from the injector tip to the surface of the liquid slag phase.

[0026] In this connection, the bath level of the liquid slag phase does not have a static bath level or slag level throughout the process, but rather can vary depending on the different process stages. Therefore, it is particularly advantageous that at least one injector for non-contact injection of the reaction gas into the liquid slag phase is positioned in such a way that a distance in the range of 0.30 to 2.0 m, particularly preferably in the range of 0.50 to 1.70 m, is ensured relative to the surface of the liquid slag phase.

[0027] Preferably, the reactive gas is injected into the liquid slag phase so that the gas penetrates the liquid slag phase to a minimum depth of 1 / 4, preferably 1 / 3, more preferably 2 / 4, even more preferably 2 / 3, and most preferably 3 / 4. By specifically setting the velocity of the injected reactive gas and the gas flow pulse, the penetration depth can be adjusted as needed, and depending on both parameters, penetration into the liquid slag phase can also be achieved. Therefore, if necessary, the metal-containing molten phase located below the liquid slag phase can also be manipulated. In addition, the gas jet briefly generates cavitation in the liquid slag phase, and the metal-containing raw material, residual material, and / or secondary residual material can be entrained in the cavitation and better decomposed within the slag phase.

[0028] In one advantageous embodiment, the reaction gases injected into the liquid slag phase via at least one injector (11) are injected at a velocity of at least 50 m / s, preferably at least 100 m / s, more preferably at least 150 m / s, even more preferably at least 200 m / s, even more preferably at least 250 m / s, and most preferably at least 300 m / s, the velocity values ​​mentioned being the exit velocities of the respective gases as they leave the injector, i.e., at its tip.

[0029] With respect to maximum velocity, it is preferred that the reaction gas is injected into the liquid slag phase at a velocity of at most 1000 m / s, more preferably at a velocity of at most 800 m / s, even more preferably at a velocity of at most 600 m / s, even more preferably at a velocity of at most 550 m / s, and most preferably at a velocity of at most 450 m / s.

[0030] In this connection, it is particularly preferred that at least one injector comprises a Laval nozzle for injecting the reactant gas into the liquid slug phase. The Laval nozzle is characterized by having a convergent section and a divergent section adjacent to each other at the nozzle throat. The radius of the narrowest cross section, the outlet radius, and the nozzle length may vary depending on the respective design. Such a Laval nozzle is known from US Pat. No. 5,623,499, which is incorporated herein by reference and is hereby incorporated by reference into the disclosure of the present invention.

[0031] In another advantageous embodiment, the Laval nozzle further comprises a coaxial nozzle or a ring gap nozzle, through which a second oxidizing gas, reducing gas, and / or inert gas and / or gas mixture can be injected into the slag phase. The first oxidizing gas, reducing gas, and / or inert gas and / or gas mixture is injected into the liquid slag phase using an injector, preferably a supersonic Laval nozzle, so as to penetrate the liquid slag phase. The second oxidizing gas, reducing gas, and / or inert gas and / or gas mixture is simply injected into the slag phase through the ring gap nozzle, without penetrating the slag phase. Therefore, the second oxidizing gas, reducing gas, and / or inert gas and / or gas mixture is referred to as a "sheath gas" within the meaning of the present invention.

[0032] The first and / or second oxidizing gas, reducing gas and / or inert gas and / or gas mixture are preferably selected from the group comprising oxygen, air and / or oxygen-enriched air. The first and / or second oxidizing gas, reducing gas and / or inert gas and / or gas mixture are preferably selected from the group comprising natural gas, in particular methane, carbon monoxide, water vapor, hydrogen, in particular green hydrogen and / or gas mixtures thereof. The first and / or second oxidizing gas, reducing gas and / or inert gas and / or gas mixture are preferably selected from the group comprising nitrogen, argon, carbon dioxide and / or gas mixtures thereof.

[0033] The term green hydrogen is understood in the context of the present invention to be produced by electrolytic decomposition of water into oxygen and hydrogen, the current required for the electrolysis coming from renewable energies such as wind, hydropower and / or solar power.

[0034] The option of introducing reactive and / or inert sheath gases and / or sheath gas mixtures into the melting unit in addition to the reaction gases advantageously allows for the control of the chemical potential and the adjustment of the oxygen partial pressure in the liquid slag and gas phases, where the chemical potential of the gas phase is formed in a reaction with the raw material, residual material and / or secondary residual material containing the metal to be melted, in a reaction with the reaction gas introduced via the injector, in a reaction with the resulting reaction gas blown into the liquid molten and slag phases, and in a reaction with the supplied sheath gas.

[0035] In a preferred embodiment, the composition of the reactant gases injected into the liquid slag phase can be kept constant, while the composition of the sheath gas can be tailored depending on the requirements for optimal control of the chemical potential of the gas atmosphere.

[0036] Additionally or alternatively, in another preferred embodiment, the composition of the sheath gas injected into the slag phase can be kept constant, while the composition of the reactant gas or reactant gas mixture supplied to the liquid slag phase can be tailored depending on the requirements for optimal control of the chemical potential.

[0037] The preferred flow rate at which the reaction gas is injected into the liquid slag phase is at least 300 Nm 3 / h, preferably at least 350 Nm 3 / h, more preferably at least 400 Nm 3 / h, even more preferably at least 450 Nm 3 / h, most preferably at least 500 Nm 3 / h. Since flow rate is a standard dependent quantity, flow rates can be higher depending on the unit size.

[0038] As already mentioned above, the liquid slag phase is subjected to rotation by arranging at least one injector at a specific angle to the horizontal, so that a vortex is formed both in the main reaction zone and in the sub-reaction zone. In order to obtain a particularly efficient vortex in the liquid slag phase, which also acts advantageously with respect to the addition of raw materials containing ground metal, residual materials and / or secondary residual materials, the reaction gas is preferably injected into the slag phase via at least one injector tangentially to an imaginary flow ring, the flow ring corresponding to 0.1 to 0.9 times the inner diameter of the main reaction zone, more preferably 0.1 to 0.8 times the inner diameter, even more preferably 0.2 to 0.7 times the inner diameter, and most preferably 0.2 to 0.6 times the inner diameter. It has been found that, advantageously, at the specific rotation speed of the liquid slag phase, a vortex can be formed in its center, via which the raw material containing the ground metal, the residual material and / or the secondary residual material can be introduced directly into the liquid slag phase and / or at least directly accepted by the liquid slag phase, and thus can be decomposed substantially more quickly in the process. In contrast to processes known from the prior art, the decomposition process takes place in the desired main reaction zone or in the liquid slag phase, and not at its surface.

[0039] Therefore, in one particularly advantageous embodiment, the metal-containing raw material, residue material and / or secondary residue material is provided in a targeted manner in the center of the slag phase through an opening in a melting unit arranged above the liquid slag phase.

[0040] This effect is particularly advantageous when the reactive gas is injected into the liquid slag phase via at least two, more preferably at least three, even more preferably at least four, and most preferably at least five injectors arranged in the wall of the melting unit, the injectors being particularly advantageously arranged at equal intervals along the periphery of the melting unit.

[0041] Additionally and / or alternatively, pulverized and / or optionally powdered metal-containing raw material, residual material, and / or by-product residual material can be added to the liquid slag phase via at least one, preferably at least two, and more preferably at least three injector lances located in the region of at least one injector. The pulverized and / or optionally powdered material can be injected via at least one, preferably multiple, injection lances directly into the liquid slag phase, more preferably directly into the cavitation in the liquid slag phase generated by at least one injector, and / or directly into the gas jet of the injector, whereby the pulverized and / or powdered metal-containing raw material, residual material, and / or by-product residual material subsequently passes into the liquid slag phase. Thus, these materials can be efficiently processed with minimal losses. Particularly effective processing is achieved if the materials have an average particle size of 0.01 to 5.0 mm, preferably less than 3.5 mm, more preferably less than 3.0 mm.

[0042] In another preferred embodiment, the reactive gases injected into the slag phase via at least one injector can be pulsed.

[0043] The method according to the invention is essentially designed for the pyrometallurgical melting of metal-containing raw, residual and / or secondary residual materials, in particular raw, residual and / or secondary residual materials containing antimony, bismuth, lead, iron, gallium, gold, indium, copper, nickel, palladium, platinum, rhodium, ruthenium, silver, zinc and / or tin, such as, in particular, organic scrap.

[0044] In the context of the present invention, scrap containing organic components is understood as organic scrap. Preferred organic scrap is selected from the group comprising electronic scrap, automobile shredder scrap and / or transformer shredder scrap, in particular light shredder fraction.

[0045] The term "electronic scrap" in the context of the present invention is understood to mean old electronic equipment as defined in accordance with EU guideline 2002 / 96 / EC. The equipment categories covered by said guideline relate to: large household appliances; small household appliances; IT and telecommunications equipment; entertainment electronics; lighting equipment; electric and electronic tools (excluding fixed industrial tools); electric toys, sports and leisure equipment; medical devices (excluding implants and all contaminated products); monitoring and control equipment and automated output devices. For individual products that fit into the corresponding equipment categories, reference is made to Annex IB of the guideline.

[0046] The present invention and its technical aspects will be described in detail below with reference to the drawings. It should be noted that the present invention should not be limited by the illustrated embodiments. In particular, unless otherwise specified, it is also possible to extract a partial sun of the matters described in the drawings and combine them with other components and understandings based on this specification and / or the drawings. In particular, it should be noted that the size ratios of each drawing and particularly the drawings are merely schematic. Since the same reference numerals represent the same objects, in some cases, explanations based on other drawings can be taken into consideration as a supplement. [Brief explanation of the drawings]

[0047] [Figure 1] 1 is a schematic cross-sectional view of an embodiment of a melting unit according to the invention for carrying out the method according to the invention; [Figure 2] FIG. 2 shows the melting unit along the section line AA. DETAILED DESCRIPTION OF THE INVENTION

[0048] 1 shows a schematic representation of an embodiment of a melting unit 1 according to the invention, which is provided for the pyrometallurgical melting of metal-containing raw materials, residual materials and / or secondary residual materials, hereinafter referred to as material to be melted M, in the presence of an oxidizing, reducing and / or inert gas and / or gas mixture G. The oxidizing, reducing and / or inert gas and / or gas mixture G will hereinafter be referred to as reaction gas G.

[0049] The melting unit 1 shown here is configured in the form of a conventional bath melting unit and comprises in its lower region a base surface 2 and an essentially cylindrically shaped reactor wall 3 extending perpendicularly from the base surface 2, the reactor wall comprising a first conically shaped region 4 and a second conically shaped region 5. The melting unit 1 comprises a melting zone 6, a main reaction zone 7 and a sub-reaction zone 8.

[0050] The conical first section 4 of the melting unit 1 is configured to include a melting zone 6 and a main reaction zone 7. A sub-reaction zone 8 extends above the main reaction zone 7.

[0051] In the conical first region 4, the comminuted material to be melted M is melted in the presence of a reactive gas G so that a liquid melt phase 9 and a liquid slag phase 10 are formed.

[0052] 1, the reaction gas G is injected into the melting unit 1 via an injector 11 arranged in the reactor wall 3. The injector 11 is arranged between the first conical region 4 and the second conical region 5 in a ring element 12, which includes a specially formed, water-cooled port 13 in which the injector 11 is suitably positioned.

[0053] In the embodiment shown here, the reaction gas G is injected into the slag phase 10 via an injector 11 located above the liquid slag phase 10 or in the sub-reaction zone 8 of the melting unit 1. As can be seen, the injector 11 is oriented at a specific angle and is located above the liquid slag phase 10. The angle can be, for example, in the range of 5 to 85° with respect to the horizontal line H.

[0054] Each injector 11 is equipped with a Laval nozzle 14, through which the reaction gas G can be injected at supersonic speed into the slag phase 10. Preferably, the reaction gas G is compressed and supplied to the melting unit 1 via the injectors 11, each of which includes a Laval nozzle 14, and is adiabatically expanded in the melting unit 1. Particularly preferably, the reaction gas G is adiabatically expanded and injected into the liquid slag phase 10 so that the heat required for the strongly exothermic reaction process can be removed.

[0055] Furthermore, each injector 11 includes an outer coaxial nozzle 15 through which a sheath gas (not shown) can be sprayed into the liquid slag phase 10 .

[0056] 2 shows a view of the melting unit 1 according to the section line AA. As can be seen, here there are in particular three injectors 11 arranged at equal intervals from one another, through which the reaction gas G is injected into the liquid slag phase 10 tangentially to an imaginary flow ring 16, which may encompass a diameter corresponding to 0.1 to 0.9 times the inner diameter of the main reaction zone 7.

[0057] The material M to be melted can be provided to the center of the slag phase 10 through an opening 17 of the melting unit 1 arranged above the slag phase 10. Additionally or alternatively, the material to be melted can also be fed into the liquid slag phase 10 via an injection lance 18 arranged in the region of the injector 11. [Explanation of symbols]

[0058] 1 Melting Unit 2 Base surface 3. Reactor wall 4. Conical first region 5 Conical second range 6. Melting Zone 7 Main Reaction Zone 8 Sub-reaction zone 9. Molten Phase 10 Slag phase 11 Injector 12 Ring Elements 13 ports 14 Laval nozzle 15 Coaxial Nozzle 16 Virtual Flow Ring 17 Opening / Supply System 18 Injection Lance M Material to be melted H horizontal line G Reactant gas

Claims

1. 1. A method for melting metal-containing raw materials, residual materials and / or secondary residual materials (M) by pyrometallurgical methods, wherein the materials are fed in pulverized form to a melting unit (1) comprising a melting zone (6), a main reaction zone and sub-reaction zones (7, 8) and melted in the presence of an oxidizing gas, a reducing gas and / or an inert gas and / or a gas mixture, so that a liquid molten phase (9), a liquid slag phase (10) and a gas phase are formed, Oxidizing gas, reducing gas and / or inert gas and / or gas mixture (G) is supplied compressed via at least one injector (11) and is adiabatically expanded in the melting unit (1) and then preferably at a pressure of 10 J / Nm ３ adiabatically expanded gas and / or gas mixture is injected into the liquid slag phase (10) so as to achieve a cooling effect of

2. 2. The method according to claim 1, wherein the at least one injector (11) comprises a Laval nozzle (14) for injecting an oxidizing, reducing and / or inert gas and / or gas mixture (G) into the liquid slag phase (10), and preferably also a coaxial nozzle (15) for injecting a second oxidizing, reducing and / or inert gas and / or gas mixture (G) into the liquid slag phase (10).

3. 3. The method according to claim 1, wherein the oxidizing, reducing and / or inert gas and / or gas mixture (G) is injected into the liquid slag phase (10) in the melting unit (1) through an injector (11) arranged above the liquid slag phase (10) without contacting the liquid slag phase and oriented at an angle of 5 to 85° to the horizontal.

4. 4. The method according to claim 3, characterized in that the at least three injectors (11) for injecting the oxidizing, reducing and / or inert gas and / or gas mixture (G) into the liquid slag phase (10) without contact have a minimum spacing of 0.10 m, preferably a minimum spacing of 0.15 m, more preferably a minimum spacing of 0.20 m, even more preferably a minimum spacing of 0.25 m, most preferably a minimum spacing of 0.30 m relative to the surface of the slag phase (10).

5. 5. The method according to claim 1, wherein the oxidizing gas and / or gas mixture (G) is selected from the group comprising oxygen, air and / or oxygen-enriched air, the reducing gas and / or gas mixture is selected from the group comprising natural gas, in particular methane, carbon monoxide, water vapor, hydrogen, in particular green hydrogen and / or gas mixtures thereof, and the inert gas and / or gas mixture is selected from the group comprising nitrogen, argon, carbon dioxide and / or gas mixtures thereof.

6. 6. The method according to any one of claims 1 to 5, characterized in that the oxidizing, reducing and / or inert gas and / or gas mixture (G) injected via at least one injector (11) into the liquid slag phase (10) is injected at a velocity of at least 50 m / s, preferably at least 100 m / s, more preferably at least 150 m / s, even more preferably at least 200 m / s, even more preferably at least 250 m / s and most preferably at least 300 m / s.

7. The first oxidizing gas, reducing gas and / or inert gas and / or gas mixture (G) has a flow rate of at least 300 Nm ３ / h, preferably at least 350 Nm ３ / h, more preferably at least 400 Nm ３ / h, and even more preferably at least 450 Nm ３ / h, most preferably at least 500 Nm ３ 7. The method according to claim 1, wherein the slag phase (10) is injected at a flow rate of 1000 kJ / h.

8. 8. The method according to claim 1, wherein the first oxidizing, reducing and / or inert gas and / or gas mixture (G) is injected into the liquid slag phase (10) via at least one injector (11) tangentially to a virtual flow ring (16), the flow ring (16) enclosing a diameter corresponding to 0.1 to 0.9 times the inner diameter of the main reaction zone (7) of the melting unit (1).

9. 9. The method according to claim 1, wherein the first oxidizing, reducing and / or inert gas and / or gas mixture (G) injected into the liquid slag phase (10) via at least one injector (11) is pulsed.

10. 10. The method according to claim 1, wherein the metal-containing raw material, residue material and / or secondary residue material is provided to the center of the liquid slag phase (10) through an opening (17) arranged above the liquid slag phase (10).

11. 11. The method according to claim 1, wherein metal-containing raw materials, residue materials and / or secondary residue materials are optionally additionally injected into the liquid slag phase (10) through at least one injection lance (18) arranged in the wall (3) of the melting unit (1).

12. 12. The method according to claim 11, characterized in that at least one injection lance (18) is arranged in the region of at least one injector (11).

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