Method, device and application of pyrometallurgical lead and zinc smelting

Abstract

The present invention provides a method for pyrometallurgical lead and zinc smelting, comprising the steps of: mixing lead-zinc materials with flux to obtain a mixed material; using a first oxygen-rich gas as a carrier gas to spray the mixed material into an oxidation stage furnace chamber, the mixed material falls into an oxidation stage molten pool, oxidatively desulfurizes to obtain a high-zinc melt, and the high-zinc melt flows into a reduction stage molten pool; mixing a lead-zinc oxide material with a first reducing agent and then putting it into a reduction stage furnace chamber to form a bed material; spraying a second oxygen-rich gas below the bed material, reducing the metal oxides in the bed material to obtain a reduction residue, the reduction residue merges into the high-zinc melt to form a melt to be reduced, spraying a second reducing agent and a third oxygen-rich gas into the melt to be reduced to obtain a reaction gas; capturing and recovering the first zinc-containing gas and the second zinc-containing gas to obtain zinc metal. The present invention can recover lead and zinc in a short process and with low energy consumption, with a high recovery rate, and is worthy of promotion.

Description

Technical Field

[0001] The invention belongs to the technical field of lead and zinc refining and comprehensive resource utilization, and specifically relates to a method and device for pyrometallurgical lead and zinc smelting and application thereof. Background Art

[0002] Lead and zinc smelting is mainly divided into two processes: pyrometallurgy and hydrometallurgy. The hydrometallurgy process has the disadvantages of single raw material type, large amount of wastewater and hazardous waste, while the pyrometallurgy has the advantages of wide raw material adaptability, less hazardous waste production and discharge, and short process, which is more suitable for processing complex materials such as smelting solid waste and urban minerals. At present, the pyrometallurgy of lead mainly adopts the traditional sintering-blast furnace reduction method, flash smelting methods such as Kifuset and Outokumpu, and oxygen-enriched smelting methods such as QSL, SKS, and three-continuous furnace. The pyrometallurgy of lead cannot process materials with high zinc content (Zn>15wt.%). The pyrometallurgy of zinc mainly adopts the sintering-sealed blast furnace method, which has the advantages of simultaneous smelting and production of lead and zinc metals, but its disadvantages are also very obvious, including the atmospheric pollution caused by the unorganized emission of SO2 flue gas during the sintering process, the difficulty of acid production by recovering low-concentration SO2, and the energy loss and carbon consumption increase caused by the reheating of the cooled sintered blocks by blast reduction. The traditional pyrometallurgy of zinc has reached the threshold of self-innovation.

[0003] Compared with the sintering-blast furnace smelting process, the molten pool smelting has low energy consumption, high efficiency and short process, which meets the low-carbon development needs of the metallurgical industry. Oxygen-enriched molten pool blowing has a higher desulfurization efficiency. Compared with the unorganized emission of SO2 flue gas in the sintering process, its flue gas is collected through the flue port, which can greatly reduce the environmental pollution load of the desulfurization process. The slag after oxidative desulfurization can directly flow into the reduction section for metal recovery, avoiding the reheating process of the cold material, which can greatly reduce the energy consumption of the smelting process. At present, the Kifusate process, "three-furnace" lead smelting, QSL lead smelting and other processes in lead smelting all adopt the molten pool smelting method or ideas to achieve good production efficiency, lead recovery rate and low energy consumption cost. However, molten pool lead and zinc smelting are all aimed at the smelting of high-lead materials, and there are no reports on engineering cases of molten pool smelting of high-zinc materials (such as Zn content ≥ 25%). The reason is that the ZnO in zinc-based solid waste has a high melting point (1975°C), which is difficult to melt and flow at conventional smelting temperatures (1150-1300°C). Large-scale matching can easily lead to deterioration of smelting conditions. Therefore, the existing lead smelting processes such as Kifset and three-continuous furnaces need to strictly limit the zinc content in the feed to no more than 8%.

[0004] In the existing lead-zinc material molten pool smelting process, zinc is mainly recovered in the form of zinc oxide dust, and further leaching-electrolysis is required to recover metallic zinc. The process is long and energy-intensive, and it cannot meet the requirements of low-carbon recycling. For example, the Ausmelt top-blown submerged injection direct zinc smelting technology (TSL) reduces volatile zinc from the molten pool, with a total zinc recovery rate of 99%, but zinc is recovered in the form of ZnO; a large number of engineering practices have proved that zinc in the molten pool can be reduced to metallic zinc, but metallic zinc is easily secondary oxidized in the ascending flue, resulting in the inability to directly recover metallic zinc.

[0005] In addition, the boiling points of ZnS and PbS in the sulfide raw materials are low, and there is a serious volatilization loss problem under conventional smelting temperatures. The mass transfer process of lead-zinc sulfides in contact with oxygen in the molten pool is slow, and the oxidation desulfurization rate cannot keep up with its volatilization rate, which ultimately leads to the volatilization of lead-zinc materials in the molten pool process and an increase in the smoke rate. Summary of the invention

[0006] In order to solve the technical problems existing in the prior art of high-zinc materials causing deterioration of smelting conditions, low direct recovery rate of metallic zinc and volatilization loss of lead-zinc sulfides, the present invention provides a method for pyrometallurgical lead-zinc smelting, comprising the steps of:

[0007] Mixing the lead-zinc material with a flux to obtain a mixed material; wherein the mass fraction of zinc in the lead-zinc material is greater than 25%;

[0008] The mixed material is sprayed into the oxidation stage furnace chamber with the first oxygen-rich gas as a carrier gas, and the mixed material falls into the oxidation stage molten pool, and is oxidized and desulfurized to obtain a high-zinc melt, and the high-zinc melt flows into the reduction stage molten pool; wherein the particle size of the mixed material is less than 3 mm;

[0009] The lead-zinc oxide material is mixed with the first reducing agent and then put into the reduction stage furnace chamber to form a bed material; a second oxygen-rich gas is sprayed below the bed material to reduce the metal oxides in the bed material to obtain a first zinc-containing gas and a reduction residue, wherein the reduction residue includes liquid lead metal and unreduced oxides and gangue;

[0010] The reduction residue is merged into the high-zinc melt to form a melt to be reduced, and a second reducing agent and a third oxygen-rich gas are sprayed into the melt to be reduced to obtain a reaction gas; wherein the reaction gas includes CO, CO2 and zinc-containing vapor;

[0011] The first zinc-containing gas and the second zinc-containing gas are captured and recovered to obtain zinc metal, and the second zinc-containing gas is formed when the reaction gas rises and passes through the bed material.

[0012] Furthermore, the flux includes a slag-forming agent, which includes one or more of quartz sand, quicklime, and calcium carbonate. The sum of the mass fractions of CaO, SiO2, and Fe in the mixture is 25-35%, the SiO2 / Fe in the mixture is 1.8-2.4, and the CaO / SiO2 in the mixture is 0.3-0.5.

[0013] Furthermore, a fluxing agent is added to the mixed material, and the fluxing agent includes a manganese-containing material and / or a copper-containing material.

[0014] Furthermore, the oxygen concentration in the oxidation stage furnace chamber is 30-95%, and the oxygen-to-material ratio in the oxidation stage furnace chamber to the mixed material is 200-500 Nm 3 / t, the temperature range of the oxidation stage furnace chamber is 1150-1300°C.

[0015] Furthermore, the method of using the first oxygen-rich gas as a carrier gas to spray the mixed material into the oxidation stage furnace chamber, the mixed material falling into the oxidation stage molten pool, being oxidized and desulfurized to obtain a high-zinc melt, and the high-zinc melt flowing into the reduction stage molten pool also includes: the high-zinc melt flows into the reduction stage molten pool via a supplementary heat tank, the supplementary heat method of the supplementary heat tank includes bottom and / or annular electromagnetic heat, and the inflow method includes height difference inflow and / or external power transmission method.

[0016] Furthermore, the amount of the first reducing agent added is 0.7-1.8 times the theoretical amount required to reduce all the metal oxides in the lead-zinc oxide material to a metallic state; the amount of the second reducing agent added is 0.8-2.0 times the theoretical amount required to reduce all the metal oxides in the melt to be reduced to a metallic state.

[0017] Furthermore, the temperature of the tuyere zone where the second oxygen-rich gas is injected is 1100-1400°C, and the temperature inside the melt to be reduced is 1100-1350°C.

[0018] Furthermore, the reaction products of the reaction of spraying the second reducing agent and the third oxygen-rich gas into the melt to be reduced also include crude lead alloy and slag. The crude lead alloy is allowed to settle and separate after standing for 1 to 4 hours; the iron-silicon ratio of the slag is 0.4 to 1.5, and the calcium-silicon ratio of the slag is 0.8 to 2.0.

[0019] The present invention also provides a pyrometallurgical lead and zinc smelting device, which is applied to any one of the pyrometallurgical lead and zinc smelting methods described above, and comprises an oxidation section, a supplementary heat tank and a reduction section, wherein the oxidation section comprises an oxidation section furnace chamber and an oxidation section molten pool which are connected from top to bottom, and the reduction section comprises a reduction section furnace chamber and a reduction section molten pool which are connected from top to bottom;

[0020] The top of the furnace chamber of the oxidation stage is fixedly connected with a feeder and a flue;

[0021] An oxidation section molten pool for carrying high-zinc melt, wherein the oxidation section molten pool is provided with a nozzle;

[0022] A supplementary heat tank is in the shape of a hollow tube, and the supplementary heat tank is connected to the oxidation section molten pool and the reduction section molten pool, so as to pass the high-zinc melt into the reduction section molten pool;

[0023] The reduction section furnace chamber is provided with a material cup, a smoke exhaust port and an air supply port in sequence from top to bottom; wherein the material cup is fixedly installed on the top of the reduction section furnace chamber to put lead-zinc oxide material and the first reducing agent into the reduction section furnace chamber; the smoke exhaust port is fixedly installed on the upper part of the reduction section furnace chamber to discharge the first zinc-containing gas and the second zinc-containing gas; the air supply port is fixedly installed on the lower part of the reduction section furnace chamber to spray the second oxygen-rich gas into the reduction section furnace chamber;

[0024] The reduction section molten pool is used to carry the molten material to be reduced; a nozzle is provided through the outer wall of the reduction section molten pool to spray the second reducing agent and the third oxygen-rich gas into the molten material to be reduced; the reduction section molten pool is also provided with a slag discharge port and a siphon port in sequence from top to bottom.

[0025] The present invention also provides an application of the above-mentioned pyrometallurgical lead-zinc smelting device in pyrometallurgical lead-zinc-copper smelting.

[0026] Compared with the prior art, the present invention has at least the following advantages:

[0027] 1. The present invention combines the oxidation section with the reduction section to coordinately process the high-zinc mixed material. By using oxygen-rich gas as a carrier gas to spray materials into the oxidation section furnace chamber, the volatilization loss of lead-zinc sulfides can be effectively reduced. The high-zinc mixed material is melted into a high-zinc melt after efficient oxidation and desulfurization in the oxidation section furnace chamber, and the high-zinc melt flows into the reduction section furnace chamber to coordinate with the lead-zinc oxide material. The high-zinc oxide material is fully melted in the short process section after oxidation and desulfurization into a high-zinc melt, which ensures the smooth operation of the working conditions and saves the energy consumption of remelting the high-zinc melt after cooling and consolidation.

[0028] 2. The present invention synergistically processes high-zinc melt and lead-zinc oxide materials in the reduction section, and vertically couples the bed materials with the reduction section molten pool, thereby enhancing the material processing capacity and efficiency of the present invention. On the one hand, the bed can control the reducing atmosphere to inhibit the oxidation of zinc vapor, and can filter the furnace gas and dust generated by the smelting in the reduction section molten pool, so that the rising first zinc-containing gas and the second zinc-containing gas are purer. On the other hand, the materials in the bed are fully reacted under a closed reducing atmosphere, including: the first reductant is burned under the injection of the second oxygen-rich gas to provide a reducing atmosphere; the unreduced oxides in the bed drip into the molten pool and are reduced under the injection of the second reductant and the third oxygen-rich gas; the CO generated by the reduction in the reduction section molten pool rises into the bed to further reduce the bed materials. The high-zinc melt and the lead-zinc oxide materials are further recovered as metallic zinc in the form of pure zinc vapor under the above-mentioned triple reduction conditions, effectively improving the direct recovery rate of metallic zinc. BRIEF DESCRIPTION OF THE DRAWINGS

[0029] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on the structures shown in these drawings without paying creative work.

[0030] Figure 1 The present invention is a flow chart of pyrometallurgical lead and zinc smelting in one embodiment of the present invention.

[0031] Figure 2 The figure is a schematic diagram of the structure of a device for pyrometallurgical lead and zinc smelting in one embodiment of the present invention.

[0032] Description of the drawings: 1. Oxidation section furnace chamber; 2. Flue; 3. Oxidation section molten pool; 4. Feeder; 5. Supplementary heat tank; 6. Reduction section molten pool; 7. External melt inlet; 8. Nozzle; 9. Supplementary air port; 10. Reduction section furnace chamber; 11. Slag discharge port; 12. Siphon port; 13. Smoke exhaust port; 14. Material cup. DETAILED DESCRIPTION

[0033] The technical solutions in the embodiments of the present invention will be described clearly and completely below in conjunction with the accompanying drawings. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0034] Furthermore, the technical solutions between the various embodiments of the present invention may be combined with each other, but this must be based on the fact that they can be implemented by ordinary technicians in the field. When the combination of technical solutions is mutually contradictory or cannot be implemented, it should be deemed that such combination of technical solutions does not exist and is not within the scope of protection required by the present invention.

[0035] When numerical ranges are given in the embodiments, it should be understood that, unless otherwise specified in the present invention, both endpoints of each numerical range and any value between the two endpoints can be selected. Unless otherwise defined, all technical and scientific terms used in the present invention are familiar to those skilled in the art and the description of the present invention, and any methods, equipment and materials of the prior art similar or equivalent to the methods, equipment and materials described in the embodiments of the present invention can also be used to implement the present invention.

[0036] like Figure 1 As shown, the present invention provides a method for pyrometallurgical lead and zinc smelting, comprising the steps of:

[0037] S1. Mixing a lead-zinc material with a flux to obtain a mixed material; wherein the mass fraction of zinc in the lead-zinc material is greater than 25%.

[0038] Lead-zinc materials may include mixed concentrates such as zinc concentrate and lead concentrate.

[0039] In some embodiments, the flux may include a slag-forming agent, which may include one or more of quartz sand, quicklime, and calcium carbonate, and mainly plays a role in adjusting the slag type.

[0040] The lead-zinc materials and flux are mixed in proportion, and the sum of the mass fractions of CaO, SiO2 and Fe in the mixed material is adjusted to be 25-35%, SiO2 / Fe is 1.8-2.4, and CaO / SiO2 is 0.3-0.5. The mixed material utilizes the synergistic mutual melting between the components to form a low melting point and low viscosity mixed material that can be melted at a lower temperature.

[0041] In other embodiments, a fluxing agent may be added to the mixed material, the fluxing agent mainly comprising a manganese-containing material and / or a copper-containing material, wherein the manganese or copper in the fluxing agent can promote the melting of the high-zinc mixed material by destroying the crystal structure of the refractory phase (such as a refractory zinc-containing compound).

[0042] For example, manganese-containing materials may include industrial manganese dioxide, manganese carbonate, manganese concentrate, etc.; copper-containing materials may include industrial copper oxide, copper powder, scrap copper, copper concentrate, matte, etc.

[0043] As another example, the fluxing agent can be added after the slag-forming agent is added and the components of the mixed material are adjusted, so as to enhance the effect of the fluxing agent and further optimize the fluxing effect by coordinating the adjustment effect of the slag-forming agent.

[0044] S2. The mixed material is sprayed into the oxidation stage furnace chamber 1 with the first oxygen-rich gas as the carrier gas, and the mixed material falls into the oxidation stage molten pool 3, and is oxidized and desulfurized to obtain a high-zinc melt, and the high-zinc melt flows into the reduction stage molten pool 6; the particle size of the mixed material is less than 3 mm.

[0045] In some embodiments, the first oxygen-rich gas may be pure oxygen or oxygen-enriched air to coordinately adjust the oxygen concentration, oxygen-to-fuel ratio, and furnace temperature of the oxidation stage furnace chamber 1 .

[0046] Compared with existing technology:

[0047] 1) The present invention utilizes oxygen-enriched molten pool oxidation desulfurization: The commonly used technology usually uses the sintering-sealed blast furnace method, which has the advantage of simultaneous smelting and producing lead and zinc metals, but its disadvantages are also very obvious. The unorganized emission of SO2 flue gas during the sintering process causes air pollution, the recovery of low-concentration SO2 to produce acid is difficult, and the reheating of the cooled sintered blocks in the reduction stage causes energy loss and increased carbon consumption.

[0048] The oxygen-enriched molten pool oxidation desulfurization has a higher desulfurization efficiency. Compared with the unorganized emission of SO2 flue gas in the sintering process, its flue gas can be collected through the flue 2, which can greatly reduce the environmental pollution load of the desulfurization process. The melt after oxidation desulfurization can directly flow into the reduction section for the recovery of metals such as lead and zinc, avoiding the reheating of cold materials and greatly reducing the energy consumption of the smelting process.

[0049] 2) The present invention regulates the particle size of the mixed material and the feeding method: Since the boiling point of ZnS in the sulfide raw material is only 1185°C, the common technology usually still has the problem of large-scale volatilization of ZnS materials under conventional smelting temperatures. Considering that ZnS has a high melting point (1700°C), its mass transfer with the oxidation desulfurization process in the oxidation stage molten pool 3 is slow, and the oxidation desulfurization rate is difficult to keep up with its volatilization rate, which ultimately leads to the volatilization of the mixed material and the increase of smoke rate.

[0050] In the present invention, the above-mentioned mixed material can be finely processed by crushing-ball milling to make the particle size of the mixed material less than 3 mm. The small particles of the mixed material can slowly fall in the process of descending to the oxidation stage molten pool 3, and closely contact with the first oxygen-rich gas, thereby accelerating the process of the initial desulfurization oxidation reaction, and forming an oxide layer on the surface of the mixed material, reducing the volatilization loss rate of lead-zinc sulfides.

[0051] In addition, the feeding method of the mixed material may include feeding in a spiral manner at the furnace top or spraying into the furnace with an oxygen-rich load. By utilizing this suspended blowing method, the mixed material can be fed into the furnace in a slow and uniform manner, thereby enhancing the effect of oxidative desulfurization.

[0052] In some embodiments, the oxygen concentration, oxygen-to-material ratio and temperature in the oxidation furnace chamber 1 can be adjusted by blowing the oxidation furnace molten pool 3; wherein the oxygen concentration can be 30-95%, and the oxygen-to-material ratio of the oxygen in the oxidation furnace chamber to the mixed material can be 200-500Nm 3 / t, the temperature in the oxidation stage furnace chamber 1 can range from 1150 to 1300°C, thereby promoting the conversion of sulfides and further enhancing the initial desulfurization and oxidation effect.

[0053] Exemplarily, the above-mentioned molten pool blowing method may include separate side blowing, separate bottom blowing, or a mixed method of side blowing and bottom blowing, which can adjust the process parameters and reaction conditions in the oxidation section while promoting heat and mass transfer and accelerating the oxidation desulfurization reaction.

[0054] As another example, the refined mixed material is dried to facilitate the mixed material to enter the furnace.

[0055] When the mixed material after refinement and drying falls into the oxidation section molten pool 3, it is subjected to secondary desulfurization and oxidation (the initial desulfurization and oxidation is the process of the mixed material falling in the oxidation section cavity), in combination with the low melting point and low viscosity characteristics after the above-mentioned adjusted ratio, to melt and form a high-zinc melt with good fluidity.

[0056] The high-zinc melt can flow from the heat supplement tank 5 (i.e., the liquid chute) into the reduction stage furnace chamber 10. To ensure the smooth inflow of the high-zinc melt and avoid cooling and pipe blockage of the high-zinc melt and energy consumption of re-melting, the heat supplement method of the heat supplement tank 5 may include bottom and / or annular electromagnetic heat supplement, and the inflow method includes height difference inflow and / or external power transmission method; in further detail, the external power transmission method may include positive pressure transmission or gas injection.

[0057] S3. Mix the lead-zinc oxide material with the first reducing agent and put it into the reduction stage furnace chamber 10 to form a bed material; spray a second oxygen-rich gas under the bed material to reduce the metal oxides in the bed material to obtain a first zinc-containing gas and a reduction residue, wherein the reduction residue includes liquid lead metal and unreduced oxides and gangue.

[0058] Lead-zinc oxide materials may include secondary materials such as return powder, specifically lead / zinc oxide ore, lead-silver slag from hydrometallurgical zinc smelting system, zinc leaching slag, lead-containing smoke, zinc oxide soot, lead-zinc smelting dust removal sludge, copper-containing electroplating sludge, galvanizing sludge, zinc-containing soot from steel mills, hot-dip galvanizing process dust, zinc powder replacement of precious metal sludge, waste zinc-manganese batteries and other lead-zinc materials that do not require oxidative desulfurization.

[0059] In some embodiments, the mass fraction ratio of lead, zinc and copper in the lead-zinc oxide material can be 5-40:10-70:0-10, and the content of other metal elements can be flexibly adjusted according to the smelting conditions.

[0060] The first reducing agent may include solid reducing agents such as pulverized coal, coke, and lump coal. The amount of the first reducing agent added is 0.7-1.8 times the mass of the first reducing agent required to reduce all the metal oxides in the lead-zinc oxide material to a metallic state.

[0061] For example, the lead-zinc oxide material and the first reducing agent can be firstly formed into blocks by hot pressing, sintering or the like, and then put into the reduction stage furnace chamber 10 by adding materials through a material cup 14 or continuously and hermetically adding materials.

[0062] As another example, the desulfurization product from the oxidation stage can be cooled and crushed into a suitable size and then mixed with the reducing agent in a proportion and fed into the furnace.

[0063] The second oxygen-enriched gas may be pure oxygen or oxygen-enriched air with an oxygen concentration greater than 20%.

[0064] The injection of the second oxygen-rich gas regulates the temperature of the tuyere zone within the range of 1100-1400°C. While the second oxygen-rich gas participates in the reduction reaction of the bed material, the reducing agent such as coke continuously burns at high temperature to further provide energy for the above reduction, thereby improving the reduction efficiency of the metal oxide to be reduced.

[0065] After the above reduction reaction, the metal oxides in the bed material are reduced to obtain a reduction residue, including the first zinc-containing gas, liquid lead metal, and unreduced oxides and gangue.

[0066] S4. The reduction residue is merged into the high-zinc melt to form a melt to be reduced, and a second reducing agent, a third oxygen-rich gas and a second flux are sprayed into the melt to be reduced to obtain a reaction gas; wherein the reaction gas includes CO, CO2 and zinc-containing vapor.

[0067] The second reducing agent may include coke powder, anthracite, pulverized coal, natural gas and spent carbonaceous electrode rods / powder.

[0068] The amount of the second reducing agent added is 0.8-2.0 times the mass of the second reducing agent required to reduce all the metal oxides in the melt to be reduced to a metallic state.

[0069] The third oxygen-enriched gas may be pure oxygen or oxygen-enriched air with an oxygen concentration greater than 20%. The third oxygen-enriched gas may also include fluxes such as slag type regulators to adjust the iron-silicon ratio and calcium-silicon ratio of the slag in the melt to be reduced to be within the range of 0.8-2 and 0.4-1.5, respectively, so that the slag of the melt to be reduced presents a high-quality slag shape with high fluidity, low melting point and low viscosity, thereby facilitating the separation of slag and gold and facilitating slag discharge.

[0070] The second reducing agent and the third oxygen-rich gas are sprayed into the melt to be reduced to fully stir the molten pool, promote heat and mass transfer, and advance the reduction reaction process.

[0071] In some embodiments, the reaction products of spraying the second reducing agent and the third oxygen-rich gas into the melt to be reduced also include crude lead alloy and slag, and the crude lead alloy is allowed to settle and separate after standing for 1 to 4 hours. The crude lead alloy and the slag can be discharged separately from the siphon port 12 or the slag discharge port 11, or they can be discharged together to the electric heating front bed for further clarification and separation.

[0072] In other embodiments, the slag disposal method may be, but is not limited to, water quenching, sending to a fuming furnace, an iron-enriching furnace, etc. The crude lead alloy may be further refined to recover valuable metals such as gold and silver.

[0073] S5. Capture and recover the first zinc-containing gas and the second zinc-containing gas to obtain zinc metal, wherein the second zinc-containing gas is formed when the reaction gas rises and passes through the bed material.

[0074] In some embodiments, metallic zinc can be captured and recovered by a capture device, wherein the capture device can include a zinc rain condensation device, etc.

[0075] As can be seen from the above, compared with the commonly used technology, the present invention combines the oxidation section with the reduction section to coordinate the treatment of high-zinc mixed materials. By using suspended blowing, the high-zinc mixed materials are melted into high-zinc melts after efficient oxidation and desulfurization in the oxidation section furnace chamber 1, and the high-zinc melts flow into the reduction section furnace chamber 10 for coordinated treatment with the lead-zinc oxide materials. By adjusting the composition of the mixed materials, the slag type of the high-zinc melt, and the slag type of the slag, the coordinated section deployment is achieved, and the high-zinc oxide materials are oxidized and desulfurized into high-zinc melts. The full melting state between the short process sections is achieved, which ensures the smooth operation of the working conditions and saves the energy consumption of remelting after the high-zinc melt is cooled and solidified.

[0076] The present invention synergistically processes high-zinc melt and lead-zinc oxide material in the reduction section, and vertically couples the bed material with the reduction section molten pool 6, thereby enhancing the material processing capacity and efficiency of the present invention. On the one hand, the bed can realize the control of the reducing atmosphere to inhibit the oxidation of zinc vapor, and can filter the furnace gas and dust generated by the smelting of the reduction section molten pool 6, so that the rising first zinc-containing gas and the second zinc-containing gas are purer. On the other hand, the materials in the bed are fully reacted under the closed reducing atmosphere, including: the first reductant is burned under the injection of the second oxygen-rich gas to provide a reducing atmosphere; the unreduced oxides in the bed drip into the reduction section molten pool 6 and are reduced under the injection of the second reductant and the third oxygen-rich gas; the CO generated by the reduction in the reduction section molten pool 6 rises into the bed to further reduce the bed material. The high-zinc melt and the lead-zinc oxide material are further recovered as pure zinc vapor under the above-mentioned triple reduction conditions to obtain metallic zinc, which effectively improves the direct recovery rate of metallic zinc.

[0077] In some embodiments, the first oxygen-rich gas is used as a carrier gas to spray the mixed material into the oxidation stage furnace chamber 1, the mixed material falls into the oxidation stage molten pool 3, and is oxidized and desulfurized to obtain a high-zinc melt, and the high-zinc melt flows into the reduction stage molten pool 6, which also includes: the high-zinc melt flows into the reduction stage molten pool 6 via a supplementary heat tank 5, the supplementary heat method of the supplementary heat tank 5 includes bottom and / or annular electromagnetic heat, and the inflow method includes height difference inflow and / or external power transmission method.

[0078] In some embodiments, the amount of the first reducing agent added is 0.7-1.8 times the theoretical amount required to reduce all the metal oxides in the lead-zinc oxide material to a metallic state; the amount of the second reducing agent added is 0.8-2.0 times the theoretical amount required to reduce all the metal oxides in the melt to be reduced to a metallic state.

[0079] In some embodiments, the temperature of the tuyere zone where the second oxygen-rich gas is injected is 1100-1400°C, and the temperature inside the melt to be reduced is 1100-1350°C.

[0080] The temperature of the tuyere zone is the furnace temperature of the air supply port 9 area in the reduction stage furnace chamber 10 described below; the air supply port 9 is fixedly installed at the lower part of the reduction stage furnace chamber 10 to spray the second oxygen-rich gas into the reduction stage furnace chamber 10.

[0081] In some embodiments, the reaction products of the reaction of spraying the second reducing agent and the second oxygen-rich gas into the melt to be reduced also include crude lead alloy and slag. The crude lead alloy is allowed to settle and separate after standing for 1 to 4 hours; the iron-silicon ratio of the slag is 0.4 to 1.5, and the calcium-silicon ratio of the slag is 0.8 to 2.0.

[0082] like Figure 2 As shown, the present invention also provides a pyrometallurgical lead and zinc smelting device, which is applied to the pyrometallurgical lead and zinc smelting method as described in any one of the above, comprising an oxidation section, a supplementary heat tank 5 and a reduction section, wherein the oxidation section comprises an oxidation section furnace chamber 1 and an oxidation section molten pool 3 which are connected from top to bottom, and the reduction section comprises a reduction section furnace chamber 10 and a reduction section molten pool 6 which are connected from top to bottom;

[0083] The top of the oxidation stage furnace chamber 1 is fixedly connected with a feeder 4 and a flue 2;

[0084] An oxidation section molten pool 3 is used to carry the high-zinc melt, and the oxidation section molten pool 3 is provided with a nozzle 8;

[0085] The supplementary heat tank 5 is in the shape of a hollow tube, and the supplementary heat tank 5 is connected to the oxidation section molten pool 3 and the reduction section molten pool 6, so as to pass the high-zinc melt into the reduction section molten pool 6;

[0086] The reduction stage furnace chamber 10 is provided with a material cup 14, a smoke exhaust port 13 and an air supply port 9 in order from top to bottom; wherein the material cup 14 is fixedly installed at the top of the reduction stage furnace chamber 10 to put the lead-zinc oxide material and the first reducing agent into the reduction stage furnace chamber 10; the smoke exhaust port 13 is fixedly installed at the upper part of the reduction stage furnace chamber 10 to discharge the first zinc-containing gas and the second zinc-containing gas; the air supply port 9 is fixedly installed at the lower part of the reduction stage furnace chamber 10 to spray the second oxygen-rich gas into the reduction stage furnace chamber 10;

[0087] The reduction section molten pool 6 is used to carry the molten material to be reduced; a nozzle 8 is provided through the outer wall of the reduction section molten pool 6 to spray the second reducing agent and the third oxygen-rich gas into the molten material to be reduced; the reduction section molten pool 6 is also provided with a slag discharge port 11 and a siphon port 12 from top to bottom.

[0088] The present invention also provides an application of the above-mentioned pyrometallurgical lead-zinc smelting device in pyrometallurgical lead-zinc-copper smelting.

[0089] In order to facilitate those skilled in the art to further understand the present invention, examples are given below:

[0090] Example 1

[0091] S1. Using a mixed concentrate of zinc concentrate and lead concentrate (whose element composition and mass fraction include: Zn 27.5wt.%, Pb16.0wt.%, Cu 1.2wt.%, Fe 9.5wt.%, S 22.3wt.%, SiO2 5.6wt.%, CaO 3.9wt.%, Cd1.3wt.%) as raw material, quartz sand and quicklime are added, and the contents of CaO, SiO2 and Fe in the mixed material are adjusted to 33wt.%, and the ratios of SiO2 / Fe and CaO / SiO2 are 1.80 and 0.37 respectively.

[0092] Add fluxing agent lead matte (main components: Cu 70wt.%, Pb 20wt.%) to the mixed material, the amount of lead matte added is 6% of the mass fraction of the mixed material. Dry the mixed material after adding the fluxing agent.

[0093] S2. Using the first oxygen-rich gas as the carrier gas, wherein the oxygen concentration is 70%, the mixed material with the fluxing agent added is sprayed into the oxidation section molten pool 3 from the spray gun device of the oxidation section furnace chamber 1, and enters the oxidation section molten pool 3 after preliminary oxidation desulfurization; further oxidation desulfurization blowing is performed in the oxidation section molten pool 3, using the side blowing form, adjusting the blowing oxygen concentration to 60%, and the oxygen-to-material ratio to 300Nm 3 / t, the temperature in the furnace is controlled to be in the range of 1200-1250°C, the mixed material is further oxidized and desulfurized in the oxidation section molten pool 3, and the melting and slagging are completed to form a high-zinc melt.

[0094] S3. The high-zinc melt flows into the reduction stage molten pool 6 through the supplementary heat tank 5. After the return powder of the lead-zinc ISP process is agglomerated, the lead-zinc-copper ratio in the lead-zinc oxide material is 32:67:1. The lead-zinc oxide material and the reducing agent coke are matched at an excess coefficient of 0.9, and are added to the material column from the material cup 14 at the upper end of the reduction stage furnace chamber 10. The material column is continuously sprayed with a second oxygen-rich gas with an oxygen concentration of 30% through the lower tuyere, and the blast volume is adjusted to control the temperature of the tuyere area to be maintained at about 1250-1300°C. The first reducing agent is burned to provide a reducing atmosphere, so that the metal oxides in the material are reduced to obtain a first zinc-containing gas and a reduction residue, wherein the reduction residue includes liquid lead metal and unreduced oxides and gangue.

[0095] S4. The reduction residue drips or falls into the molten pool below the reduction furnace, and gathers with the high-zinc melt to form a melt to be reduced; the melt to be reduced is sprayed with a suitable proportion of the second reducing agent (pulverized coal) and slag type regulator (calcium oxide) through the spray guns on both sides with a 60% concentration of the third oxygen-enriched gas as the carrier gas to control the slag iron-silicon ratio and calcium-silicon ratio in the melt to be reduced to 0.6 and 1.0 respectively. The second reducing agent and slag type regulator strongly stir the molten pool, adjust the blast volume to control the temperature of the melt to be reduced to 1200-1250°C, and continue to reduce the unreduced metal oxides such as lead, zinc, and copper in the reduction stage molten pool 6 with the help of heat release and the provision of a reducing atmosphere, and at the same time complete the slag-making reaction, and the reduced lead, copper, and cadmium liquid metals in the reduction stage molten pool 6 settle in the furnace below the reduction furnace to enrich into crude lead alloys, and separate from the slag. Finally, reaction gas, crude lead alloy, and slag are obtained.

[0096] S5. The reaction gas is filtered through the upper material column to reduce the dust particle content in the gas phase to obtain the second zinc-containing gas. The first zinc-containing gas and the second zinc-containing gas are then collected in the zinc rain or lead rain condenser to obtain metallic zinc. The crude lead alloy and slag in the reduction stage molten pool 6 are discharged, clarified in the electric heating front bed for 4 hours, and the crude lead alloy is discharged from the siphon port 12 to the refining workshop to obtain valuable metals, and the slag is sent to the fuming furnace through the slag discharge port.

[0097] According to the analysis, the recovery rate of metallic zinc was 91%, and the recovery rate of metallic lead was 95%; the volatilization loss rates of lead and zinc were 17.8wt.% and 8.5wt.% respectively.

[0098] Example 2

[0099] S1. Using mixed concentrate (whose element composition and mass fraction include: Zn 26.2wt.%, Pb 19.3wt.%, Cu0.9wt.%, Fe 8.1wt.%, S 21.2wt.%, SiO2 6.1wt.%, CaO 4.2wt.%, Cd 0.9wt.%) as raw material, quartz sand and quicklime are added, the contents of CaO, SiO2 and Fe in the mixed material are adjusted to 33wt.%, and the ratios of SiO2 / Fe and CaO / SiO2 are 2.2 and 0.38 respectively, and the mixed material is dried.

[0100] S2. Using the first oxygen-rich gas as the carrier gas, wherein the oxygen concentration is 65%, the mixed material is sprayed into the oxidation section molten pool 3 through the spray gun device of the oxidation section furnace chamber 1, and enters the oxidation section molten pool 3 after preliminary oxidation desulfurization; further oxidation desulfurization and blowing are carried out in the oxidation section molten pool 3, and the side blowing form is adopted, and the blowing oxygen concentration is adjusted to 70%, the oxygen-to-material ratio is 350Nm3 / t, and the temperature range in the furnace is controlled to be 1200-1250℃, the mixed material is further oxidized and desulfurized in the oxidation section molten pool 3, and the melting and slag formation is completed to form a high-zinc melt.

[0101] S3. The high-zinc melt flows into the reduction stage molten pool 6 through the supplementary heat tank 5. The lead-zinc oxide ore is combined with zinc oxide fly ash for agglomeration to obtain a lead-zinc oxide material, and the lead-zinc-copper ratio in the lead-zinc oxide material is 30:69:1. The lead-zinc oxide material and the reducing agent coke are combined at an excess coefficient of 1.0, and are added to the material column from the material cup 14 at the upper end of the reduction stage furnace chamber 10. The material column is continuously sprayed with a second oxygen-rich gas with an oxygen concentration of 30% through the lower tuyere, and the blast volume is adjusted to control the temperature of the tuyere area to be maintained at about 1250-1300°C. The first reducing agent is burned to provide a reducing atmosphere, so that the metal oxides in the material are reduced to obtain a first zinc-containing gas and a reduction residue, wherein the reduction residue includes liquid lead metal and unreduced oxides and gangue.

[0102] S4. The reduction residue drips or falls into the molten pool below the reduction furnace, and gathers with the high-zinc melt to form a melt to be reduced; the melt to be reduced is sprayed with a suitable proportion of the second reducing agent (pulverized coal) and slag type regulator (calcium oxide) through the spray guns on both sides with a 50% concentration of the third oxygen-enriched carrier gas to control the slag iron-silicon ratio and calcium-silicon ratio in the melt to be reduced to 0.45 and 1.0 respectively. The second reducing agent and slag type regulator strongly stir the molten pool, adjust the blast volume to control the temperature of the melt to be reduced to 1200-1250°C, and continue to reduce the unreduced metal oxides such as lead, zinc, and copper in the reduction stage molten pool 6 with the help of heat release and the provision of a reducing atmosphere, and at the same time complete the slag-making reaction, and the reduced lead, copper, and cadmium liquid metals in the reduction stage molten pool 6 settle in the furnace below the reduction furnace to enrich into crude lead alloys, and separate from the slag. Finally, reaction gas, crude lead alloy, and slag are obtained.

[0103] S5. The reaction gas is filtered through the upper material column to reduce the dust particle content in the gas phase to obtain the second zinc-containing gas. The first zinc-containing gas and the second zinc-containing gas are then collected in the zinc rain or lead rain condenser to obtain metallic zinc. The crude lead alloy and slag in the reduction stage molten pool 6 are discharged, clarified in the electric heating front bed for 4 hours, and the crude lead alloy is discharged from the siphon port 12 to the refining workshop to obtain valuable metals, and the slag is sent to the fuming furnace through the slag discharge port.

[0104] The analysis showed that the recovery rate of metallic zinc was 90% and the recovery rate of metallic lead was 94%.

[0105] Example 3

[0106] S1. Take mixed concentrate (whose element composition and mass fraction include: Zn 28.8wt.%, Pb 15.1wt.%, Cu1.1wt.%, Fe 8.2wt.%, S 20.9wt.%, SiO2 6.6wt.%, CaO 4.2wt.%) as raw material, add quartz sand and quicklime, adjust the content of CaO, SiO2 and Fe in the mixed material to 33.1wt.%, and the ratio of SiO2 / Fe and CaO / SiO2 are 2.20 and 0.39 respectively.

[0107] Add fluxing agent lead matte (main components Cu 70wt.%, Pb 20wt.%) to the mixed material, the amount of lead matte added is 4% of the mass fraction of the mixed material, ball mill the mixed material after adding fluxing agent, control the particle size to 2mm, and dry it.

[0108] S2. The first oxygen-rich gas is used as the carrier gas, wherein the oxygen concentration is 75%, and the mixed material is sprayed into the oxidation section molten pool 3 by the spray gun device of the oxidation section furnace chamber 1, and enters the oxidation section molten pool 3 after preliminary oxidation desulfurization; the oxidation section molten pool 3 is further oxidized and desulfurized and blown, using the side blowing form, adjusting the blowing oxygen concentration to 80%, and the oxygen-to-material ratio to 350Nm 3 / t, the temperature in the furnace is controlled to be in the range of 1200-1250°C, the mixed material is further oxidized and desulfurized in the oxidation section molten pool 3, and the melting and slagging are completed to form a high-zinc melt.

[0109] S3. The high-zinc melt flows into the reduction stage molten pool 6 through the supplementary heat tank 5. The zinc oxide ash, lead-containing electrostatic dust ash, and sintering return powder are agglomerated to obtain lead-zinc oxide material, and the lead-zinc-copper ratio in the lead-zinc oxide material is 29:70:1. The lead-zinc oxide material and the reducing agent coke are matched with an excess coefficient of 1.0, and are added to the material column from the material cup 14 at the upper end of the reduction stage furnace chamber 10. The material column is continuously sprayed with a second oxygen-rich gas with an oxygen concentration of 30% through the lower tuyere, and the blast volume is adjusted to control the temperature of the tuyere area to be maintained at about 1300-1350°C. The first reducing agent is burned to provide a reducing atmosphere, so that the metal oxides in the material are reduced to obtain a first zinc-containing gas and a reduction residue, wherein the reduction residue includes liquid lead metal and unreduced oxides and gangue.

[0110] S4. The reduction residue drips or falls into the molten pool below the reduction furnace, and gathers with the high-zinc melt to form a melt to be reduced; the melt to be reduced is sprayed with a suitable proportion of the second reducing agent (pulverized coal) and slag type regulator (calcium oxide) through the spray guns on both sides with a third oxygen-rich gas of 45% concentration as the carrier gas to control the slag iron-silicon ratio and calcium-silicon ratio in the melt to be reduced to 0.5 and 1.2 respectively. The second reducing agent and slag type regulator strongly stir the molten pool, adjust the blast volume to control the temperature of the melt to be reduced to 1200-1250°C, and continue to reduce the unreduced metal oxides such as lead, zinc, and copper in the reduction stage molten pool 6 with the help of heat release and the provision of a reducing atmosphere, and at the same time complete the slag-making reaction, and the reduced lead, copper, and cadmium liquid metals in the reduction stage molten pool 6 settle in the furnace below the reduction furnace to enrich into crude lead alloys, and separate from the slag. Finally, reaction gas, crude lead alloy, and slag are obtained.

[0111] S5. The reaction gas is filtered through the upper material column to reduce the dust particle content in the gas phase to obtain the second zinc-containing gas. The first zinc-containing gas and the second zinc-containing gas are then collected in the zinc rain or lead rain condenser to obtain metallic zinc. The crude lead alloy and slag in the reduction stage molten pool 6 are discharged, clarified in the electric heating front bed for 4 hours, and the crude lead alloy is discharged from the siphon port 12 to the refining workshop to obtain valuable metals, and the slag is sent to the fuming furnace through the slag discharge port.

[0112] The analysis showed that the recovery rates of metallic zinc were 92% and that of metallic lead were 94%.

[0113] Example 4

[0114] The mixed material in Example 1 was blown with oxygen at 1250°C, with an oxygen concentration of 60% and an oxygen-to-material ratio of 300 Nm 3 / t, the SO2 content was reduced to 20mg / m 3 When about , the blowing is stopped and the desulfurization product is discharged. It can be seen that the desulfurization product has good fluidity.

[0115] The desulfurization product was measured by a nitrogen-sulfur analyzer, and its S content was found to be 0.5wt%. The melting point and high-temperature viscosity tests showed that the full melting temperature of the batching system was 1210°C, and the high-temperature viscosity value was 0.180Pa·S, which met the subsequent lead-zinc joint smelting requirements and could obtain metallic lead and metallic zinc.

[0116] Comparative Example 1

[0117] This comparative example is a comparative example of Example 1. Different from Example 1, the mixed material does not go through a process of being fully contacted with the first oxygen-rich gas, but is directly put into the oxidation stage molten pool 3 for oxidative desulfurization. The specific process is as follows: a mixed concentrate of zinc concentrate and lead concentrate (whose element composition and mass fraction include: Zn 27.5wt.%, Pb 16.0wt.%, Cu1.2wt.%, Fe 9.5wt.%, S 22.3wt.%, SiO2 5.6wt.%, CaO 3.9wt.%, Cd 1.3wt.%) is mixed with a flux, and then the mixed material is directly put into the oxidation stage molten pool 3, and oxidative desulfurization is carried out in the oxidation stage molten pool 3, wherein the temperature of the oxidation stage molten pool 3 is about 1200-1250°C.

[0118] The first oxygen-rich gas is used for blowing in the form of side blowing; after deep oxidation desulfurization in the oxidation section molten pool 3 and product melting, it flows out and is discharged into the subsequent reduction section for treatment; through the analysis of the total amount and content of smoke dust, it can be obtained that the volatilization loss rates of lead and zinc are 39.2wt.% and 14.5wt.%, respectively, which are significantly higher than the volatilization loss rates of lead and zinc in Example 1.

[0119] The above technical solutions of the present invention are only preferred embodiments of the present invention, and the patent scope of the present invention is not limited thereto. All equivalent structural changes made by using the contents of the present invention specification and drawings under the technical concept of the present invention, or directly / indirectly applied in other related technical fields are included in the patent protection scope of the present invention.

Claims

1. A method for pyrometallurgical lead and zinc smelting, characterized in that: Includes steps: Mixing the lead-zinc material with a flux to obtain a mixed material; wherein the mass fraction of zinc in the lead-zinc material is greater than 25%; The mixed material is sprayed into the oxidation stage furnace chamber with the first oxygen-rich gas as the carrier gas, and the mixed material falls into the oxidation stage molten pool, and is oxidized and desulfurized to obtain a high-zinc melt, and the high-zinc melt flows into the reduction stage molten pool; wherein the particle size of the mixed material is less than 3 mm; the oxygen concentration in the oxidation stage furnace chamber is 30-95%, and the oxygen-to-material ratio of the oxygen in the oxidation stage furnace chamber to the mixed material is 200-500 Nm 3 / t, the temperature range of the oxidation stage furnace chamber is 1150-1300°C; The lead-zinc oxide material is mixed with the first reducing agent and then put into the reduction stage furnace chamber to form a bed material; a second oxygen-rich gas is sprayed below the bed material to reduce the metal oxides in the bed material to obtain a first zinc-containing gas and a reduction residue, wherein the reduction residue includes liquid lead metal and unreduced oxides and gangue; The reduction residue is merged into the high-zinc melt to form a melt to be reduced, and a second reducing agent and a third oxygen-rich gas are sprayed into the melt to be reduced to obtain a reaction gas; wherein the reaction gas includes CO, CO2 and zinc-containing vapor; The first zinc-containing gas and the second zinc-containing gas are captured and recovered to obtain zinc metal, and the second zinc-containing gas is formed when the reaction gas rises and passes through the bed material.

2. The method for pyrometallurgical lead and zinc smelting according to claim 1, characterized in that: The flux includes a slag-forming agent, which includes one or more of quartz sand, quicklime, and calcium carbonate. The sum of the mass fractions of CaO, SiO2, and Fe in the mixture is 25-35%, the SiO2 / Fe in the mixture is 1.8-2.4, and the CaO / SiO2 in the mixture is 0.3-0.

5.

3. The method for pyrometallurgical lead and zinc smelting according to claim 1, characterized in that: A fluxing agent is added to the mixed material, wherein the fluxing agent includes a manganese-containing material and / or a copper-containing material.

4. The method for pyrometallurgical lead and zinc smelting according to claim 1, characterized in that: The method of using the first oxygen-rich gas as a carrier gas to spray the mixed material into the oxidation stage furnace chamber, the mixed material falling into the oxidation stage molten pool, being oxidized and desulfurized to obtain a high-zinc melt, and the high-zinc melt flowing into the reduction stage molten pool also includes: the high-zinc melt flows into the reduction stage molten pool via a supplementary heat tank, the supplementary heat method of the supplementary heat tank includes bottom and / or annular electromagnetic heat, and the inflow method includes height difference inflow and / or external power transmission method.

5. The method for pyrometallurgical lead and zinc smelting according to claim 1, characterized in that: The amount of the first reducing agent added is 0.7-1.8 times the theoretical amount required to reduce all the metal oxides in the lead-zinc oxide material to a metallic state; the amount of the second reducing agent added is 0.8-2.0 times the theoretical amount required to reduce all the metal oxides in the melt to be reduced to a metallic state.

6. The method for pyrometallurgical lead and zinc smelting according to claim 1, characterized in that: The temperature of the tuyere area where the second oxygen-rich gas is injected is 1100-1400°C, and the temperature inside the melt to be reduced is 1100-1350°C.

7. The method for pyrometallurgical lead and zinc smelting according to claim 1, characterized in that: The reaction products of the reaction of spraying the second reducing agent and the third oxygen-rich gas into the melt to be reduced also include crude lead alloy and slag. The crude lead alloy is allowed to settle and separate after standing for 1 to 4 hours; the iron-silicon ratio of the slag is 0.4 to 1.5, and the calcium-silicon ratio of the slag is 0.8 to 2.

0.

8. A device for pyrometallurgical lead and zinc smelting, characterized in that: The method for pyrometallurgical lead and zinc smelting according to any one of claims 1 to 7 comprises an oxidation section, a supplementary heat tank and a reduction section, wherein the oxidation section comprises an oxidation section furnace chamber and an oxidation section molten pool connected from top to bottom, and the reduction section comprises a reduction section furnace chamber and a reduction section molten pool connected from top to bottom; The top of the oxidation section furnace chamber is fixedly connected with a feeder and a flue; An oxidation section molten pool for carrying high-zinc melt, wherein the oxidation section molten pool is provided with a nozzle; A supplementary heat tank is in the shape of a hollow tube, and the supplementary heat tank is connected to the oxidation section molten pool and the reduction section molten pool, so as to pass the high-zinc melt into the reduction section molten pool; The reduction section furnace chamber is provided with a material cup, a smoke exhaust port and an air supply port in sequence from top to bottom; wherein the material cup is fixedly installed on the top of the reduction section furnace chamber to put lead-zinc oxide material and the first reducing agent into the reduction section furnace chamber; the smoke exhaust port is fixedly installed on the upper part of the reduction section furnace chamber to discharge the first zinc-containing gas and the second zinc-containing gas; the air supply port is fixedly installed on the lower part of the reduction section furnace chamber to spray the second oxygen-rich gas into the reduction section furnace chamber; The reduction section molten pool is used to carry the molten material to be reduced; a nozzle is provided through the outer wall of the reduction section molten pool to spray the second reducing agent and the third oxygen-rich gas into the molten material to be reduced; the reduction section molten pool is also provided with a slag discharge port and a siphon port in sequence from top to bottom.

9. Use of the device for pyrometallurgical lead-zinc smelting as claimed in claim 8 in pyrometallurgical lead-zinc-copper smelting.

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