A method and apparatus for complex zinc concentrate fire desulphurization

Abstract

The application belongs to the field of nonferrous metallurgy, and discloses a method and device for fire desulfurization of complex zinc concentrate. The method for fire desulfurization of complex zinc concentrate comprises the following steps: continuously feeding zinc-containing materials into a low-oxygen zone, heating the zinc-containing materials in the low-oxygen zone, and flowing the zinc-containing materials from the low-oxygen zone to an oxygen-rich zone, and obtaining fluidized materials after pre-oxidation during the flowing process; continuously flowing the fluidized materials into the oxygen-rich zone for further deep oxidation, and continuously flowing the materials to a discharge port to discharge the materials outside the furnace, and obtaining zinc oxide after cooling the discharged materials. The production method provided by the application completes the low-temperature pre-oxidation in the low-oxygen zone and the medium-temperature main reaction in the oxygen-rich zone, greatly improves the processing capacity of a single roasting furnace, significantly reduces the softening probability of material particles and the agglomeration rate of large particles in the furnace, effectively reduces the residual heat taken away by flue gas, improves the heat energy utilization efficiency, can efficiently process fine, wet, miscellaneous and poor complex zinc-containing materials, and balances the roasting efficiency, product quality and energy consumption control.

Description

Technical Field

[0001] This invention belongs to the field of non-ferrous metallurgy and relates to a zinc oxide process, specifically a method and apparatus for pyrometallurgical desulfurization of complex zinc concentrate. Background Technology

[0002] Pyrometallurgical desulfurization of complex zinc concentrate is a core step in the pretreatment of zinc smelting raw materials. The core objective is to oxidize zinc sulfide (ZnS) into zinc oxide (ZnO) or soluble zinc salts, achieve efficient desulfurization and resource-based acid production, and prepare qualified raw materials for subsequent hydrometallurgical zinc smelting.

[0003] Patent CN105603210A discloses a short-process pyrometallurgical zinc smelting method, which completely removes sulfur from powdered sulfide zinc concentrate through fluidized bed roasting, converting it into oxide roasted sand. The temperature of the fluidized bed reduction process is selected as 950℃~1250℃, and the particle size of the roasted sand is 1~3mm. This method has a large processing capacity, low cost, simple process, and short process.

[0004] However, with the development of the industry, the particle size of zinc concentrate fed into the furnace is getting smaller and smaller. Under the same operating parameters, fine-particle materials have a large specific surface area and are prone to melting and agglomeration at high temperatures due to reduced surface tension. When a continuous liquid phase layer forms on the particle surface, it can encapsulate unreacted ZnS nuclei, causing a "sintering lock-in" phenomenon. This leads to the obstruction of solid-gas interface reactions and the stagnation of desulfurization kinetics, ultimately resulting in a decrease in desulfurization rate and an abnormal increase in the content of insoluble sulfur in flue gas. In addition, when the content of impurity elements (such as lead, iron, vanadium, manganese, etc.) in the zinc concentrate fed into the furnace is high, fine-particle zinc concentrate is prone to forming agglomerates due to surface tension. This causes localized exothermic reactions, concentrated particle softening, and adhesion to the furnace bed. Under high temperature and high air-to-material ratio atmosphere, this can catalyze the conversion of SO2 to SO3, causing the SO3 concentration in the flue gas to rise continuously, exacerbating equipment corrosion and leakage risks, reducing sulfur recovery efficiency, and significantly increasing the load on waste acid treatment and overall operating costs.

[0005] The aforementioned problems have become key technological bottlenecks restricting the large-scale, green, and efficient development of the zinc smelting industry. Summary of the Invention

[0006] In view of the defects and deficiencies of the existing technology, the present invention provides, firstly, a method for pyrometallurgical desulfurization of complex zinc concentrate; and secondly, a production apparatus for pyrometallurgical desulfurization of complex zinc concentrate.

[0007] In a first aspect, the present invention provides a method for pyrometallurgical desulfurization of complex zinc concentrate, comprising: continuously feeding zinc-containing material into a low-oxygen zone, heating the zinc-containing material in the low-oxygen zone, flowing the zinc-containing material from the low-oxygen zone to an oxygen-rich zone, undergoing pre-oxidation during the flow process to obtain fluidized material; continuously flowing the fluidized material into an oxygen-rich zone for further deep oxidation, continuously flowing the fluidized material towards the discharge port and being discharged from the furnace body, and obtaining zinc oxide after cooling the discharged material; The zinc-containing material consists of 8 wt% to 12 wt% water, 1.5 wt% to 2.5 wt% lead, 44 wt% to 50 wt% zinc, and 23 to 25 wt% sulfur; The D50 of zinc-containing materials is 14.8~20μm.

[0008] Preferably, during the reaction process in the low-oxygen zone and the oxygen-enriched zone, the oxygen-containing stream is blown upwards from below the material, and the flow rates of the low-oxygen stream and the oxygen-enriched stream are the same, which are (5 × 10⁻⁶) / ( ... 4 )~(15×10 4 Nm 3 / h.

[0009] Preferably, the distance from the zinc-containing material feeding point to the inner wall of the reaction chamber is L, and the total length of the material flow path in the low-oxygen zone and the oxygen-rich zone is D, where L = (1 / 4~1 / 3)D.

[0010] Preferably, the reaction temperature in the low-oxygen zone is 800~850ºC, the reaction time is 1~1.5h, and the oxygen concentration in the low-oxygen zone is 20~22 vol%.

[0011] Preferably, the reaction temperature in the second oxygen-enriched zone is 900~1000℃, the reaction time is 1~1.5h, and the oxygen concentration in the second oxygen-enriched zone is 30~35vol.

[0012] Secondly, the present invention provides a production apparatus for pyrometallurgical desulfurization of complex zinc concentrate, comprising a furnace body, a wind box, an air inlet pipe, a pressure equalization and dispersion air distribution structure, and a partition plate, wherein the wind box is disposed at the bottom of the furnace body; The air inlet pipe is fixedly connected to the air box and extends out of the air box. The pressure equalization and dispersion air distribution structure is disposed on the air inlet pipe and is located inside the air box. The air inlet pipe is fixedly connected to the bottom of the air box; The partition plate is fixedly connected to the air box, and the partition plate divides the air box into a first low-oxygen zone and a first oxygen-rich zone; an oxygen pipe is fixedly connected to the air box, and the oxygen pipe is connected to the first oxygen-rich zone. The bellows blows low-oxygen flow and oxygen-rich flow into the reaction chamber of the furnace body from bottom to top, thereby forming a second low-oxygen zone and a second oxygen-rich zone in the reaction chamber of the furnace body. The pressure equalization and dispersion air distribution structure includes a pressure equalization pipe, which is fixedly connected to and communicates with the air inlet pipe. The pressure equalization pipe has multiple pressure equalization holes, which are evenly spaced along the circumferential direction of the pressure equalization pipe. The centerlines of the equalizing pipe, the partition plate, and the air box overlap.

[0013] Preferably, the pressure equalization and dispersion air distribution structure includes two or more pressure equalization pipes, which are stacked and interconnected along the height direction away from the wind box, and the cross-section of the multiple pressure equalization pipes gradually decreases from bottom to top.

[0014] Preferably, the diameter of the equalizing holes on the plurality of equalizing pipes gradually increases from bottom to top.

[0015] Preferably, the furnace body is provided with a furnace opening device, an inspection window, a feed inlet, a discharge outlet, a heat dissipation device, an operating door, a smoke exhaust outlet, and a temperature detection device; the feed inlet and the discharge outlet are located at opposite ends of the material flow direction.

[0016] Preferably, the air box includes a box body and a gas distribution plate. The box body is inverted conical in shape, and the gas distribution plate is fixedly connected to the top of the box body. The gas distribution plate has a plurality of ventilation holes evenly spaced apart. The partition plate is fixedly connected to the box body and divides the box body into the first low-oxygen zone and the first oxygen-rich zone.

[0017] Compared with the prior art, one or more technical solutions provided by the present invention have at least one of the following beneficial effects: (1) This invention achieves zoned temperature control and on-demand oxygen supply through segmented reaction. The low-oxygen zone completes the low-temperature pre-oxidation and the oxygen-rich zone completes the medium-temperature main reaction roasting mode, which greatly improves the processing capacity of a single roasting furnace, making the bed capacity reach more than 8t / d·m2 and the annual processing scale of zinc-containing materials reach more than 550kt / a. It can also significantly reduce the probability of material particle softening and large particle agglomeration in the furnace, reduce the occurrence of "sintering lock-in" phenomenon, reduce the insoluble sulfur content of roasted sand to 0.16%, and control the SO3 content in flue gas to 0.05~0.07vol. At the same time, it effectively reduces the residual heat carried away by the flue gas, improves the thermal energy utilization efficiency, and can efficiently process complex zinc-containing materials that are fine, wet, mixed, and poor, taking into account roasting efficiency, product quality and energy consumption control.

[0018] (2) The present invention further optimizes the production device for pyrometallurgical desulfurization of complex zinc concentrate. By adopting a uniform pressure dispersion air distribution structure, the airflow is evenly distributed, effectively reducing the turbulence of high-speed airflow, and forming a uniform velocity field and pressure field in the air distribution area. This enhances the device's adaptability to fluctuations in raw material particle size and changes in operating conditions. Furthermore, the dispersion air distribution effect can be adapted to the roasting operation of fine-particle zinc-containing materials, significantly reducing the smoke dust rate of the roasting furnace to below 40%, while controlling the insoluble sulfur content of the smoke dust to below 0.3wt%. The furnace opening, heat dissipation, detection, and material discharge devices on the furnace body further ensure the stable operation of the roasting operation.

[0019] (3) This device adopts a pressure equalization and dispersion air distribution structure with uniform pressure equalization holes in the circumferential direction, which can make the airflow uniformly dispersed and sprayed out, forming a stable and uniform velocity field and pressure field in the wind box. It can effectively adapt to the fluctuation of raw material particle size and heat load changes in the furnace, and avoid sudden changes in local air pressure and fluidization disorder. At the same time, the furnace is divided into low oxygen zone and oxygen rich zone by the partition plate and the oxygen concentration in each zone is precisely controlled, so that the oxidation exothermic reaction of zinc-containing materials can proceed smoothly in stages, avoiding excessive heat load in the furnace bed caused by excessive reaction concentration, and reducing the risk of coking in the bed from the source. This air distribution structure can also avoid the generation of dust-containing airflow in the wind box, alleviate the problem of air inlet channel blockage, and, together with the furnace body matching furnace start-up, heat exhaust, detection and material discharge device, comprehensively improve the long-term operational stability of the whole device. Attached Figure Description

[0020] Figure 1 This is a schematic diagram of the overall structure of the pyrometallurgical desulfurization production device for complex zinc concentrate provided in Embodiment 1 of the present invention. Figure 2 This is a schematic diagram of the internal structure of the bellows in Embodiment 1 of the present invention; Figure 3 This is a schematic diagram of the gas distribution plate in Embodiment 1 of the present invention.

[0021] Attached Figure Descriptions: 1. Furnace body; 101. Furnace top; 102. Upper straight section; 103. Conical section; 104. Lower straight section; 2. Wind box; 201. Box body; 202. Gas distribution plate; 3. Air inlet pipe; 4. Pressure equalization pipe; 5. Pressure equalization hole; 6. Divider plate; 7. Flue gas outlet; 8. Furnace start-up device; 9. Inspection window; 10. Feed inlet; 11. Discharge outlet; 12. Heat dissipation device; 13. Temperature detection device; 14. Operating door. Detailed Implementation

[0022] The present invention provides the following specific technical solutions.

[0023] In a first aspect, the present invention provides a method for pyrometallurgical desulfurization of complex zinc concentrate, comprising: continuously feeding zinc-containing material into a low-oxygen zone, heating the zinc-containing material in the low-oxygen zone, flowing the zinc-containing material from the low-oxygen zone to an oxygen-rich zone, undergoing pre-oxidation during the flow to obtain fluidized material; continuously flowing the fluidized material into an oxygen-rich zone for further deep oxidation, continuously flowing the fluidized material towards the discharge port and being discharged from the furnace body, and obtaining zinc oxide after cooling the discharged material; and the high-temperature flue gas after the reaction in the second low-oxygen zone and the second oxygen-rich zone being drawn into the subsequent process section through the negative pressure of the flue gas discharge port. The zinc-containing material consists of 8 wt% to 12 wt% water, 1.5 wt% to 2.5 wt% lead, 44 wt% to 50 wt% zinc, and 23 to 25 wt% sulfur; The D50 of zinc-containing materials is 14.8~20μm.

[0024] Research has revealed that existing traditional fluidized bed roasting processes have stringent requirements for the conditions of the materials fed into the furnace. They can typically only process zinc-containing materials with low moisture content, low lead content, and high sulfur content. This is because high moisture content in the material easily leads to particle agglomeration and accumulation, resulting in poor fluidization characteristics. High lead content will form a low-melting-point phase at high temperatures, exacerbating material agglomeration and blocking the gas channels on the gas distribution plate, causing turbulent flow and furnace condition fluctuations. When the sulfur content is low, the oxidation heat release is insufficient, making it difficult to maintain a stable furnace temperature. In addition, the traditional air distribution structure cannot adaptively compensate, which easily leads to problems such as low temperature zones, incomplete reactions, and excessive insoluble sulfur. Therefore, it is difficult to adapt to complex fine-grained zinc-containing materials with high moisture content, high lead content, and low sulfur content, making large-scale stable operation difficult.

[0025] Through the above-mentioned production process, a segmented roasting method of pre-oxidation in a low-oxygen zone and main reaction in an oxygen-enriched zone can be adopted. This allows for precise control of the temperature and oxygen concentration in each reaction zone, ensuring a gentle initial oxidation reaction. This avoids the melting and softening of fine-particle materials due to a sudden drop in surface tension caused by localized concentrated heat release, resulting in porous and loose zinc oxide particles and reducing the occurrence of "lock-in phenomenon." Furthermore, it ensures efficient diffusion of oxygen into the particle interior in the subsequent oxygen-enriched zone, achieving full oxidation and desulfurization of zinc sulfide. At the same time, the gentle reaction environment in the low-oxygen pre-oxidation stage reduces the activation of impurity elements (lead, iron, vanadium, manganese, etc.), and the precise optimization of oxygen concentration in the oxygen-enriched zone significantly inhibits the catalytic effect of impurity elements on the conversion of sulfur dioxide to sulfur trioxide, greatly reducing the concentration of sulfur trioxide in the flue gas. This reduces the risk of equipment corrosion and leakage, improves sulfur recovery efficiency, and reduces the load on waste acid treatment and overall operating costs. Ultimately, this achieves efficient, stable, and green roasting of complex zinc-containing materials that are fine, wet, mixed, and lean, ensuring high-scale continuous production of high-quality zinc oxide from a single unit.

[0026] That is, the preferred process provided by the present invention can stably process the fluidized bed roasting of complex zinc-containing materials that are fine (14.8~20μm), wet (the water content of the material to be treated increases from 8wt% to 12wt%), impure (the lead content of the material to be treated increases from 1.5wt% to 2.5wt%), and poor (the sulfur content of the material to be treated decreases from 30wt% to 23wt%). The insoluble sulfur content of the roasted sand is reduced to 0.16%, the dust rate is reduced from 50% to below 40%, the insoluble sulfur content of the dust is less than 0.3%, and the scale of zinc-containing material processing reaches more than 550kt / a.

[0027] Research has shown that this technology is suitable for the roasting requirements of complex zinc-containing materials, including fine, wet, mixed, and lean materials. It effectively reduces the probability of material particle softening and agglomeration, and promotes the full oxidation and desulfurization of materials such as zinc sulfide (ZnS). This significantly improves the production efficiency and product quality of zinc oxide, while reducing the loss of waste heat from flue gas and improving the efficiency of thermal energy utilization, enabling high-scale and highly stable continuous production of zinc oxide with a single unit.

[0028] Preferably, during the reaction process in the low-oxygen zone and the oxygen-enriched zone, the oxygen-containing stream is blown upwards from below the material, and the flow rates of the low-oxygen stream and the oxygen-enriched stream are the same, which are (5 × 10⁻⁶) / ( ... 4 )~(15×10 4 Nm 3 / h.

[0029] Preferably, the distance from the zinc-containing material feeding point to the inner wall of the reaction chamber is L, and the total length of the material flow path in the low-oxygen zone and the oxygen-rich zone is D, where L = (1 / 4~1 / 3)D.

[0030] Research has shown that setting the feeding point at (1 / 4 to 1 / 3) D from the inner wall of the reaction chamber allows zinc-containing materials to fall precisely into the core reaction area of ​​the second low-oxygen zone. This enables the materials to quickly come into contact with the uniform airflow in the low-oxygen zone, forming a stable fluidized state. This prevents the materials from accumulating on the wall or directly entering the oxygen-rich zone, ensuring sufficient time for low-temperature pre-oxidation reaction. At the same time, it lays the foundation for the orderly flow of materials to the oxygen-rich zone, improving the continuity and stability of the overall roasting reaction.

[0031] Preferably, the reaction temperature in the low-oxygen zone is 800~850ºC, the reaction time is 1~1.5h, and the oxygen concentration in the low-oxygen zone is 20~22 vol%.

[0032] Research has shown that the above-mentioned optimized reaction conditions are suitable for the requirements of low-temperature pre-oxidation reaction. They can not only enable zinc-containing materials to complete the initial oxidation to generate loose and porous zinc oxide, increasing the gas-solid contact area of ​​subsequent reactions, but also prevent fine-particle materials from melting and agglomerating due to violent oxidation and exothermic reactions caused by excessively high temperature and high oxygen concentration. At the same time, the activation degree of impurity metals is low under these conditions, which is compatible with low oxygen flow and reduces the loss of fine particles by flue gas, ensuring that the pre-oxidation reaction is sufficient and stable.

[0033] Preferably, the reaction temperature in the second oxygen-enriched zone is 900~1000℃, the reaction time is 1~1.5h, and the oxygen concentration in the second oxygen-enriched zone is 30~35vol.

[0034] Preferably, the negative pressure at the exhaust port is (-100) to (-50) Pa.

[0035] Research has shown that the above-mentioned optimized reaction conditions are suitable for the medium-temperature main reaction requirements, providing sufficient oxygen content and reaction temperature for the complete oxidation of complex zinc-containing materials, promoting their full conversion into zinc oxide. At the same time, these conditions can prevent gas diffusion from being hindered in the particle pores, prevent low-melting-point phases such as zinc ferrite from agglomerating and settling due to liquid-phase bridging, ensure stable fluidization, effectively reduce the insoluble sulfur content of calcined sand, and improve the quality of zinc oxide products.

[0036] Secondly, the present invention provides a production apparatus for pyrometallurgical desulfurization of complex zinc concentrate, comprising a furnace body, a wind box, an air inlet pipe, a pressure equalization and dispersion air distribution structure, and a partition plate, wherein the wind box is disposed at the bottom of the furnace body; The air inlet pipe is fixedly connected to the air box and extends out of the air box. The pressure equalization and dispersion air distribution structure is disposed on the air inlet pipe and is located inside the air box. The air inlet pipe is fixedly connected to the bottom of the air box; The partition plate is fixedly connected to the air box, and the partition plate divides the air box into a first low-oxygen zone and a first oxygen-rich zone; an oxygen pipe is fixedly connected to the air box, and the oxygen pipe is connected to the first oxygen-rich zone. The bellows blows low-oxygen flow and oxygen-rich flow into the reaction chamber of the furnace body from bottom to top, thereby forming a second low-oxygen zone and a second oxygen-rich zone in the reaction chamber of the furnace body. The pressure equalization and dispersion air distribution structure includes a pressure equalization pipe, which is fixedly connected to and communicates with the air inlet pipe. The pressure equalization pipe has multiple pressure equalization holes, which are evenly spaced along the circumferential direction of the pressure equalization pipe. The centerlines of the equalizing pipe, the partition plate, and the air box overlap.

[0037] Research revealed that the overlapping of the equalizing pipe, partition plate, and centerline of the wind box creates a coaxial symmetrical design. This design allows the airflow from the inlet pipe to be evenly distributed throughout the wind box via the equalizing pipe, effectively reducing the turbulence of the high-speed airflow and creating a uniform velocity and pressure field in the wind box distribution area. This avoids localized sintering and channeling phenomena in the fluidized layer caused by uneven air distribution, improves the roasting capacity for fine-particle zinc-containing materials, reduces the dust rate to below 40%, and reduces the insoluble sulfur content in the dust to below 0.3 wt%. Furthermore, it enhances the device's adaptability to fluctuations in raw material particle size and changes in operating conditions, enabling stable processing of complex zinc-containing materials that are fine, wet, mixed, and lean.

[0038] The partition plate divides the air box into a first low-oxygen zone and a first oxygen-rich zone, and the furnace reaction chamber corresponds to a second low-oxygen zone and a second oxygen-rich zone. The oxygen pipe is only connected to the first oxygen-rich zone. This structure allows the low-oxygen and oxygen-rich airflows to be accurately delivered to the corresponding reaction zones of the fluidized bed in the furnace, realizing zoned temperature control and on-demand oxygen distribution of the fluidized bed during the roasting process. It can accurately control the oxygen concentration in the oxygen-rich zone, which not only meets the segmented process requirements of pre-oxidation in the low-oxygen zone and main reaction in the oxygen-rich zone, but also reduces the amount of flue gas and improves the thermal energy utilization efficiency. The partitioned structure of the bellows and furnace body creates a flow field and oxygen concentration field suitable for segmented roasting. Combined with uniform air distribution, this effectively reduces the probability of material particle softening and the agglomeration rate of large particles within the furnace, preventing material blockage of airflow channels and ensuring stable and efficient operation of the roasting furnace. This increases the capacity of a single hearth to 8 t / d·m. 2The annual processing capacity of zinc-containing materials reaches over 550 kt / a, while reducing the insoluble sulfur content of calcined sand to 0.16 wt% and controlling the SO3 content in flue gas to 0.05~0.07 vol%, significantly improving the quality of roasted products.

[0039] This invention precisely divides the airbox into a first low-oxygen zone and a first oxygen-rich zone with equal areas by setting up a partition plate and a pressure-equalizing dispersion air distribution structure, and ensures that the total air intake flow rate of the two zones is consistent, thereby achieving equal gas flow velocities entering the second low-oxygen zone and the second oxygen-rich zone. Based on this, a stable and continuous transition zone naturally forms between the second low-oxygen zone and the second oxygen-rich zone within the furnace. Within the reaction chamber, materials migrate directionally from the second low-oxygen zone to the second oxygen-rich zone; simultaneously, during the reaction process, the materials undergo up-and-down tumbling motion within the chamber, and their directional flow significantly impedes the upward airflow, further strengthening and stabilizing this transition zone.

[0040] This transition zone, serving as a crucial coupling section between low-oxygen weak reaction and oxygen-rich strong oxidation, serves two main purposes. First, it effectively avoids the instantaneous and intense exothermic reaction and localized hot spots caused by sudden changes in oxygen concentration at the interface between the two zones. It also prevents sudden changes in oxygen content from leading to a surge in local reaction rates and heat accumulation, reducing the likelihood of particle melting, agglomeration, or even fluidization instability. Second, the gradient oxygen concentration field can orderly regulate the oxidation atmosphere within the furnace, allowing the material to gradually increase its reaction intensity and enhance desulfurization, ensuring sufficient reaction and stable fluidization throughout the entire process, thereby improving roasting efficiency and product quality consistency.

[0041] Preferably, the pressure equalization and dispersion air distribution structure includes two or more pressure equalization pipes, which are stacked and interconnected along the height direction away from the wind box, and the cross-section of the multiple pressure equalization pipes gradually decreases from bottom to top.

[0042] Research has shown that stacking multiple pressure equalizing pipes along the height direction with a gradually decreasing cross-section from bottom to top allows for a gradual and uniform distribution of airflow within the bellows, further optimizing the spatial uniformity of air distribution and avoiding significant local velocity differences that can occur with a single pressure equalizing pipe. Simultaneously, the gradual flow distribution continuously reduces airflow turbulence, creating a more stable velocity and pressure field within the bellows. This ensures a uniform and stable fluidization state of the material within the furnace, meeting the roasting requirements of fine-particle zinc-containing materials, effectively reducing dust entrainment, and improving roasting efficiency.

[0043] Preferably, the diameter of the equalizing holes on the plurality of equalizing pipes gradually increases from bottom to top.

[0044] Research has shown that the gradually increasing aperture of the equalizing pipe from bottom to top makes the air outlet resistance of the upper layer lower than that of the lower layer. Combined with the multi-layer equalizing pipe with progressively smaller cross-sections, this achieves a balance of air outlet resistance along the height direction within the wind box, allowing for a more reasonable distribution of air volume in each layer of equalizing pipe and a more uniform airflow output. This avoids excessively fast or slow air outlets in certain areas, further optimizing the stability of the velocity and pressure fields within the wind box, ensuring uniform fluidization of materials throughout the furnace, and meeting the roasting requirements of fine-particle zinc-containing materials.

[0045] Preferably, the furnace body is provided with a furnace opening device, an inspection window, a feed inlet, a discharge outlet, a heat dissipation device, an operating door, a smoke exhaust outlet, and a temperature detection device; the feed inlet and the discharge outlet are located at opposite ends of the material flow direction.

[0046] Preferably, the air box includes a box body and a gas distribution plate. The box body is inverted conical in shape, and the gas distribution plate is fixedly connected to the top of the box body. The gas distribution plate has a plurality of ventilation holes evenly spaced apart. The partition plate is fixedly connected to the box body and divides the box body into the first low-oxygen zone and the first oxygen-rich zone.

[0047] To make the technical problems, technical solutions and technical advantages of the present invention clearer, a detailed description will be given below with reference to specific examples. However, the scope of protection of the present invention is not limited to the following specific embodiments.

[0048] Unless otherwise defined, all technical terms used herein have the same meaning as commonly understood by those skilled in the art. The technical terms used herein are for the purpose of describing particular embodiments only and are not intended to limit the scope of the invention.

[0049] Unless otherwise specified, all raw materials, reagents, instruments and equipment used in this invention can be purchased from the market or prepared by existing methods.

[0050] Example 1: A production apparatus for pyrometallurgical desulfurization of complex zinc concentrate, referring to Figure 1 It includes a furnace body 1, a wind box 2, an air inlet pipe 3, a pressure equalization and dispersion air distribution structure and a partition plate 6. The wind box 2 is located at the bottom of the furnace body 1 and is connected to the furnace body 1. The pressure equalization and dispersion air distribution structure and the partition plate 6 are both located in the wind box 2. The air inlet pipe 3 is fixedly connected to the wind box 2 and the air inlet pipe 3 extends out of the wind box 2.

[0051] The furnace body 1 includes a furnace top 101, an upper straight section 102, a conical section 103, and a lower straight section 104, arranged sequentially from top to bottom. The furnace top 101 is arc-shaped, with the convex surface facing outwards. An exhaust port 7 is provided on the upper straight section 102. The exhaust port 7 generates negative pressure through the induced draft fan of the subsequent process section. In practical applications, the negative pressure device can be a commonly used exhaust device such as a negative pressure induced draft fan. This device can actively draw air to create a stable negative pressure in the exhaust pipe, achieving smooth and controllable exhaust of the flue gas. The exhaust flow rate inside the furnace can be adjusted. Conical section 103 is an expanded-diameter conical section with a smaller bottom and a larger top, which can gradually increase the cross-sectional area of ​​the airflow in the furnace and steadily reduce the exhaust gas velocity. This can not only prevent fine particles from being entrained by a large amount of high-speed airflow and reduce the dust rate, but also allow the material to form a stable fluidized transition zone above the bed, reducing particle backmixing and short-circuit flow. At the same time, in conjunction with the zoned reaction conditions, the gas-solid contact is more sufficient, improving the roasting reaction efficiency and operational stability.

[0052] The lower straight section 104 is the main reaction chamber. The lower straight section 104 is equipped with a furnace opening device 8, an inspection window 9, a feed port 10, a discharge port 11, a heat dissipation device 12, an operating door 14, a flue gas outlet 7, and a temperature detection device 13. The feed port 10 and the discharge port 11 are located at both ends of the lower straight section 104. In a specific embodiment of the present invention, there are two feed ports 10 arranged side by side.

[0053] Multiple furnace opening devices 8 are provided, and the multiple furnace opening devices 8 are distributed at intervals along the circumferential direction of the lower straight section 104. The number of furnace opening devices 8 is selected according to the size of the lower straight section 104, and usually 4 to 10 furnace opening devices 8 are provided. In this specific embodiment, 4 furnace opening devices 8 are provided.

[0054] Multiple inspection windows 9 are provided, and the multiple inspection windows 9 are distributed at intervals along the circumferential direction of the lower straight section 104; the inspection windows 9 and the furnace opening device 8 are located on the same horizontal line; the number of inspection windows 9 is selected according to the size of the lower straight section 104, and usually 2 to 4 inspection windows 9 are provided. In this specific embodiment, 4 inspection windows 9 are provided.

[0055] Multiple heat dissipation devices 12 are provided, and the multiple heat dissipation devices 12 are distributed at intervals along the axial direction of the lower straight section 104. The heat dissipation devices 12 are usually located below the inspection window 9 and on both sides of the inspection window 9. In actual application, the number of heat dissipation devices 12 is selected according to the size of the lower straight section 104.

[0056] Multiple operating doors 14 are provided, and the multiple operating doors 14 are distributed at intervals along the circumferential direction of the lower straight section 104; there are usually 2 to 4 operating doors 14, and in this specific embodiment, there are 4 operating doors 14.

[0057] Multiple sets of temperature detection devices 13 are provided, and these sets are spaced apart along the circumferential direction of the lower straight section 104. Each set of temperature detection devices 13 has multiple devices, and these multiple devices are spaced 250mm to 500mm apart along the height direction of the lower straight section 104, so as to monitor the material temperature in real time and comprehensively. The number of temperature detection devices 13 is selected according to the size of the lower straight section 104, usually 4 to 24 sets, with 3 to 5 devices in each set.

[0058] The air box 2 is located below the lower straight section 104. The air box 2 includes a box body 201 and a gas distribution plate 202. The box body 201 is inverted conical in shape. The gas distribution plate 202 is fixedly connected to the top of the box body 201, and multiple ventilation holes are evenly and spaced on the gas distribution plate 202. A partition plate 6 is fixedly connected to the box body 201, dividing the box body 201 into a first low-oxygen zone and a first oxygen-rich zone. An air inlet pipe 3 is fixedly connected to the bottom of the box body 201 and is used to supply air to the air box 2. In this specific embodiment, the air inlet pipe 3 is arranged horizontally and extends out of the box body 201. An air outlet is opened on the air inlet pipe 3, and a uniform air distribution structure is arranged on the air outlet.

[0059] Reference Figure 2 A pressure equalization and dispersion air distribution structure is installed in the box 201. The pressure equalization and dispersion air distribution structure includes pressure equalization pipes 4, which are fixedly connected to and communicate with the outlet end of the air inlet pipe 3. The pressure equalization and dispersion air distribution structure includes two or more pressure equalization pipes 4, which are stacked and interconnected along the height direction away from the air box 2. The cross-section of the multiple pressure equalization pipes 4 gradually decreases from bottom to top, and the aperture of the pressure equalization holes 5 on the multiple pressure equalization pipes 4 gradually increases from bottom to top. This pressure equalization and dispersion air distribution structure adopts a multi-layered arrangement of pressure equalization pipes 4 stacked and interconnected along the height direction. With the design of gradually decreasing cross-section and gradually increasing aperture of the pressure equalization holes 5 from bottom to top, it can achieve balanced air outlet resistance and gradual airflow distribution along the height direction, effectively reduce gas swirling and entrainment in the air box, stabilize the velocity field and pressure field in the air box 2, make the air distribution more uniform, ensure the stability of the fluidization state of the material in the furnace, reduce dust entrainment, and improve the roasting efficiency of fine particulate zinc-containing materials.

[0060] In practical applications, the uppermost equalizing pipe 4 in the equalizing dispersion air distribution structure can be set in an open or closed manner, with a closed manner being preferred.

[0061] In this specific embodiment, the pressure equalization and dispersion air distribution structure is provided with two layers of pressure equalization pipes 4. The top end of the top pressure equalization pipe 4 is closed, and in order to reduce the air outlet resistance of the bottom pressure equalization pipe 4, the air outlet pipe is hollowed out. Adjacent pressure equalization holes 5 are separated by a columnar structure. The air outlet volume of the bottom pressure equalization hole 5 is controlled to be ≥50%, and the air outlet velocity of the top pressure equalization hole 5 is controlled to be 10~25m / s.

[0062] The centerlines of the equalizing pipe 4, the partition plate 6 and the air box 2 overlap, which can make the airflow symmetrically distributed along the center, avoid the flow deviation and eddies, ensure uniform and symmetrical air distribution and stable pressure field, further improve the fluidization uniformity of materials, and ensure the stable and efficient roasting process.

[0063] Because the airflow blown into the furnace body 1 by the bellows 2 includes both low-oxygen and high-oxygen flows, a second low-oxygen zone and a second high-oxygen zone are formed in the reaction chamber within the furnace body 1. The second low-oxygen zone is located above the first low-oxygen zone, and the second high-oxygen zone is located above the first high-oxygen zone. An oxygen pipe is fixedly connected to the bellows 2, and the oxygen pipe is connected to the first high-oxygen zone. In actual production, the gas in the second low-oxygen zone comes from the first low-oxygen zone, and the gas in the second high-oxygen zone comes from the first high-oxygen zone. When the bellows 2 introduces gas into the reaction chamber, a transition zone is formed between the second low-oxygen zone and the second high-oxygen zone. The transition zone is formed by the convergence of the gases ejected from the first low-oxygen zone and the first high-oxygen zone. The oxygen concentration in this transition zone changes in a gradient, which can effectively control the oxidation atmosphere in different areas of the furnace, ensuring that the material is heated evenly and reacts fully and stably within the reaction chamber.

[0064] The flue gas outlet 7 is located above the second oxygen-enriched zone. Its negative pressure draws in a large amount of flue gas generated in the upper part of the fluidized layer, and timely controls the residence time of the flue gas to ensure that the materials entrained in the flue gas react fully and reduce the non-melting sulfur in the flue gas dust.

[0065] Example 2: A method for pyrometallurgical desulfurization of complex zinc concentrate includes the following steps: Step 1: The zinc-containing material consists of 8 wt% water, 2.5 wt% lead, 44 wt% zinc, and 23 wt% sulfur. The zinc-containing material, with a particle size of 15-20 μm, is fed into the second low-oxygen zone of the pyrometallurgical desulfurization production unit for complex zinc concentrate described in Example 1 through the feed inlet. The airflow from the wind box is controlled at 10 × 10⁻⁶. 4 Nm 3 / h. During feeding, the distance between the landing point of the zinc-containing material and the furnace wall is controlled to be 1 / 4D (the total length of the material flow path in the low-oxygen zone and the oxygen-rich zone is D). The oxygen concentration in the second low-oxygen zone is 21 vol%, the reaction temperature is 830℃, and the flue gas velocity in the second low-oxygen zone is 0.45 m / s. The zinc-containing material flows from the second low-oxygen zone to the second oxygen-rich zone, reacts in the second low-oxygen zone for 1.5 hours, and then enters the second oxygen-rich zone to obtain fluidized material.

[0066] Step 2: The oxygen concentration in the second oxygen-enriched zone is 33 vol%, the reaction temperature is 980℃, and the exhaust gas velocity in the second oxygen-enriched zone is 0.55 m / s. After 1.5 h, the fluidized material flows from the second oxygen-enriched zone to the discharge port, and the oxidized material is discharged from the discharge port, thus obtaining zinc oxide calcined sand. After exhaust gas, dust is collected, and the resulting particles are zinc oxide calcination dust.

[0067] Example 3: A method for pyrometallurgical desulfurization of complex zinc concentrate includes the following steps: Step 1: The zinc-containing material consists of 10 wt% water, 2.1 wt% lead, 48 wt% zinc, and 24 wt% sulfur. The zinc-containing material, with a particle size of 15-20 μm, is fed into the second low-oxygen zone of the pyrometallurgical desulfurization production unit for complex zinc concentrate described in Example 1 through the feed inlet. The air outlet volume of the wind box is 5 × 10⁻⁶. 4 Nm 3 / h. During feeding, the distance between the zinc-containing material's landing point and the furnace wall is controlled to be 1 / 3D. The oxygen concentration in the second low-oxygen zone is 21 vol%, the reaction temperature is 850℃, and the flue gas velocity in the second low-oxygen zone is 0.4 m / s. The zinc-containing material flows from the second low-oxygen zone to the second oxygen-enriched zone, reacts in the second low-oxygen zone for 1.2 hours, and then enters the second oxygen-enriched zone to obtain fluidized material for 1.2 hours.

[0068] Step 2: The oxygen concentration in the second oxygen-enriched zone is 30 vol%, the reaction temperature is 985℃, the flue gas velocity is 0.5 m / s, and the flue gas velocity in the second oxygen-enriched zone is 0.55 m / s. After 1.2 hours, the fluidized material flows from the second oxygen-enriched zone to the discharge port, and the oxidized material is discharged from the discharge port, thus obtaining zinc oxide calcined sand. After the flue gas is discharged, dust is collected, and the obtained particles are zinc oxide calcination dust.

[0069] Example 4: A method for pyrometallurgical desulfurization of complex zinc concentrate includes the following steps: Step 1: The zinc-containing material consists of 12 wt% water, 2 wt% lead, 50 wt% zinc, and 25 wt% sulfur. The zinc-containing material, with a particle size of 15-20 μm, is fed into the second low-oxygen zone of the pyrometallurgical desulfurization production unit for complex zinc concentrate described in Example 1 through the feed inlet. The air outlet volume of the wind box is 15 × 10⁻⁶. 4 Nm 3 / h. During feeding, the distance between the zinc-containing material's landing point and the furnace wall is controlled to be 1 / 4D. The oxygen concentration in the second low-oxygen zone is 21 vol%, the reaction temperature is 850℃, and the flue gas velocity in the second low-oxygen zone is 0.5 m / s. The zinc-containing material flows from the second low-oxygen zone to the second oxygen-enriched zone, reacts in the second low-oxygen zone for 1.5 hours, and then enters the second oxygen-enriched zone to obtain fluidized material.

[0070] Step 2: The oxygen concentration in the second oxygen-enriched zone is 35 vol%, the reaction temperature is 1000℃, and the exhaust gas velocity in the second oxygen-enriched zone is 0.6 m / s. After 1.5 h, the fluidized material flows from the second oxygen-enriched zone to the discharge port, and the oxidized material is discharged from the discharge port, thus obtaining zinc oxide calcined sand. After exhausting the flue gas, dust is collected, and the resulting particles are zinc oxide calcination dust.

[0071] Comparative Example 1: A production device for pyrometallurgical desulfurization of complex zinc concentrate differs from Example 1 in that it does not have a pressure equalization and dispersion air distribution structure, and multiple air outlets are opened on the air inlet pipe.

[0072] A method for pyrometallurgical desulfurization of complex zinc concentrate is provided, which uses the above-mentioned pyrometallurgical desulfurization production equipment for complex zinc concentrate. Steps 1 and 2 are the same as in Example 2, the flow rates of the air inlet pipe and oxygen pipe are kept constant, and the temperatures of the second low-oxygen zone and the second oxygen-rich zone are controlled to be the same as in Example 1.

[0073] During the production process, it was found that when the air intake volume of the air intake duct was 100,000 Nm³, 3 When the flow rate is / h, the bellows vibrates, air flows between the bellows and the furnace body, and channeling and dead zones appear in the fluidized bed, making stable production impossible.

[0074] Comparative Example 2: A method for pyrometallurgical desulfurization of complex zinc concentrate is disclosed, which uses the aforementioned pyrometallurgical desulfurization production equipment for complex zinc concentrate. The difference from Example 2 is that the distance between the landing point of the zinc-containing material and the furnace wall is controlled to be 1 / 5D. The process parameters of other steps 1 to 2 are the same as those in Example 2.

[0075] During production, it was found that due to the increased residence time of materials in the low-temperature, low-oxygen zone, the temperature in the low-oxygen zone reached 950℃, rendering the effect of the oxygen-enriched zone insignificant. The calcining furnace's processing capacity was reduced to 7 t / d·m³. 2 .

[0076] Comparative Example 3: A method for pyrometallurgical desulfurization of complex zinc concentrate is disclosed, which uses the aforementioned pyrometallurgical desulfurization production equipment for complex zinc concentrate. The difference from Example 2 is that the distance between the landing point of the zinc-containing material and the furnace wall is controlled to be 1 / 2D. The process parameters of other steps 1 to 2 are the same as those in Example 2.

[0077] During production, it was found that the material was too concentrated in the oxygen-enriched zone, resulting in the lowest temperature in the low-temperature, low-oxygen zone being 750℃, leading to incomplete reaction. Meanwhile, large particles settled and blocked the air or oxygen-enriched air channels on the gas distribution plate in the second oxygen-enriched zone, causing a significant increase in the air box pressure. The furnace needed to be shut down for cleaning.

[0078] Comparative Example 4: A method for pyrometallurgical desulfurization of complex zinc concentrate is disclosed, which uses the aforementioned pyrometallurgical desulfurization production apparatus for complex zinc concentrate. The difference from Example 2 is that the air box does not have zoned oxygen supply, and the oxygen concentration in both zones is 33 vol%. The process parameters for other steps 1 to 2 are the same as in Example 2.

[0079] During the production process, it was found that high oxygen enrichment caused violent reactions of materials per unit area, and even low melting point materials melted and wrapped around other materials. Large areas of sintering blockage occurred on the entire gas distribution plate, making normal production impossible.

[0080] Comparative Example 5: A method for pyrometallurgical desulfurization of complex zinc concentrate is disclosed, which uses the aforementioned pyrometallurgical desulfurization production apparatus for complex zinc concentrate. The difference from Example 2 is that the air box does not have zoned oxygen supply, and the oxygen concentration in both zones is 21 vol%. The process parameters for other steps 1 to 2 are the same as those in Example 2.

[0081] During production, it was found that the calcining furnace with the gas distribution plate had a low processing capacity of approximately 7 t / d·m. 2 To ensure the oxygen demand of the gas distribution plate reaction, a large amount of air is required, resulting in high flue gas velocity in the furnace, a dust rate of more than 45%, and high levels of insoluble sulfur in the dust.

[0082] The production capacity and dust rate (calcination dust mass: dry basis mass of raw materials fed into the furnace) of Examples 2-4 and Comparative Examples 1-5 were recorded, and the content of insoluble sulfur in zinc oxide calcined sand and calcination dust, and the content of SO3 in flue gas were tested. The data are shown in Table 1.

[0083] Table 1 Production parameters and product parameters of Examples 2-4 and Comparative Examples 1-5 As shown in Table 1, Examples 2-4 represent the optimal stable operating conditions of this invention. After minor fluctuations in material composition and fine-tuning of process parameters, the core indicators remained highly stable and exhibited excellent performance: the production capacity remained stable at 8.05-8.15 t / d·m³. 2 It has a strong unit furnace bed processing capacity; the dust rate is as low as 39.2~39.6wt%, which reduces the clogging and blockage of the subsequent cooling and dust removal section; the insoluble sulfur in the calcined sand is only 0.14~0.15wt% and the insoluble sulfur in the dust is 0.25~0.29wt%, which ensures thorough desulfurization and high product purity; the SO3 content in the flue gas is low (0.05~0.07wt%), which reduces environmental pressure and is suitable for large-scale industrial continuous mass production.

[0084] Compared with Example 2, which features a partition plate and a multi-layer pressure equalization and dispersion air distribution structure and can stably produce under high load, Comparative Example 1, which lacks a partition plate and pressure equalization and dispersion air distribution structure, experiences severe vibration of the air box and air leakage in the furnace body during high-flow air supply. The fluidized layer develops channels and dead zones, making stable mass production impossible. This fully demonstrates that the pressure equalization and dispersion air distribution structure and the partition plate are the core basic components for uniform air distribution, stable fluidization, and prevention of airflow turbulence in large roasting furnaces, and neither can be omitted.

[0085] Compared to Example 2, which precisely limits the distance between the material landing point and the furnace wall to 1 / 4D and achieves a balanced and efficient reaction, Comparative Example 2, where the landing point is too close to the furnace wall (1 / 5D), leads to excessive material retention in the low-oxygen zone, local overheating, ineffective oxygen-rich zone function, and reduced production capacity. Comparative Example 3, where the landing point is off-center from the furnace (1 / 2D), causes the material to skip the low-temperature preheating and flow directly into the oxygen-rich zone, resulting in insufficient reaction in the early stage and violent exothermic blockage and production stoppage in the later stage. It can be seen that the present invention, by controlling the material landing point and matching the oxygen concentration gradient transition zone in the furnace, avoids material deviation, retention, and overheating, ensures the gradual reaction of the material, and balances high production capacity and long-term stable operation.

[0086] Compared to Example 2, which uses a low-oxygen zone of 21 vol% combined with an oxygen-rich zone of 30-35 vol% for gradient oxygen supply, sintering prevention, and deep desulfurization, Comparative Example 4, with an overall oxygen concentration of 33 vol%, caused instantaneous and intense oxidation and exothermic reactions in the material, resulting in large-area sintering and caking that made production impossible. Comparative Example 5, with an overall oxygen concentration of 21 vol%, required a large flow of supplementary air for oxygen supply, leading to a surge in dust rate and low production capacity. This fully demonstrates the advantages of the present invention's zoning settings: weak reaction preheating in the low-oxygen zone to prevent thermal shock, gradient oxygen change in the transition zone to avoid local hot spot sintering, and high oxygen in the oxygen-rich zone to enhance deep desulfurization. It perfectly avoids the fatal defect of uniform oxygen throughout the entire area, achieving efficient, low-loss, and stable roasting.

[0087] The above-described embodiments are merely preferred embodiments of the present invention, but the scope of protection of the present invention is not limited thereto. Any equivalent substitutions or modifications made by those skilled in the art within the technical scope of the present invention, based on the technical solution and concept of the present invention, should be covered within the scope of protection of the present invention.

Claims

1. A method for pyrometallurgical desulfurization of complex zinc concentrate, characterized in that, include: Zinc-containing materials are continuously fed into a low-oxygen zone, where they are heated and flow into an oxygen-rich zone. During this flow, they undergo pre-oxidation to obtain fluidized material. The fluidized material then flows into an oxygen-rich zone for further deep oxidation and continues to flow out of the furnace through the discharge port. After cooling, the discharged material yields zinc oxide. The zinc-containing material contains 8wt%~12wt% water, 1.5wt%~2.5wt% lead, 44wt%~50wt% zinc and 23wt%~25wt% sulfur; The D50 of zinc-containing materials is 14.8~20μm; The oxygen concentration in the hypoxic zone is 20 vol%~22 vol%, the reaction temperature in the hypoxic zone is 800~850℃, and the reaction time is 1~1.5h. The oxygen concentration in the oxygen-enriched zone is 30 vol%~35 vol%, the reaction temperature in the oxygen-enriched zone is 900~1000℃, and the reaction time is 1~1.5h; Let L be the distance from the zinc-containing material feeding point to the inner wall of the reaction chamber, and D be the total length of the material flow path in the low-oxygen zone and the oxygen-rich zone. L = (1 / 4 ~ 1 / 3)D.

2. The method for pyrometallurgical desulfurization of complex zinc concentrate as described in claim 1, characterized in that, During the reaction in the low-oxygen zone and the oxygen-rich zone, the oxygen-containing gas stream is blown from the direction of the material downward, and the flow rate of the oxygen-containing gas is (5 x 10 4 )~(15 x 10 4 ) Nm 3 / h.

3. The method for pyrometallurgical desulfurization of complex zinc concentrate as described in claim 1, characterized in that, The exhaust gas velocity in the low-oxygen zone is 0.4~0.5 m / s.

4. The method for pyrometallurgical desulfurization of complex zinc concentrate as described in claim 1 or 3, characterized in that, The exhaust gas velocity in the oxygen-rich zone is 0.5~0.6m / s.

5. A production apparatus for pyrometallurgical desulfurization of complex zinc concentrate, characterized in that, It includes a furnace body (1), a wind box (2), an air inlet pipe (3), a pressure equalization and dispersion air distribution structure and a partition plate (6), wherein the wind box (2) is located at the bottom of the furnace body (1); The air inlet pipe (3) is fixedly connected to the air box (2) and extends out of the air box (2). The pressure equalization and dispersion air distribution structure is set on the air inlet pipe (3) and the pressure equalization and dispersion air distribution structure is located inside the air box (2). The air inlet pipe (3) is fixedly connected to the bottom of the air box (2); The partition plate (6) is fixedly connected to the bellows (2), and the partition plate (6) divides the bellows (2) into a first low-oxygen zone and a first oxygen-rich zone; an oxygen pipe is fixedly connected to the bellows (2), and the oxygen pipe is connected to the first oxygen-rich zone; The bellows (2) blows low-oxygen flow and oxygen-rich flow into the reaction chamber of the furnace body (1) from bottom to top, thereby forming a second low-oxygen zone and a second oxygen-rich zone in the reaction chamber of the furnace body (1). The pressure equalization and dispersion air distribution structure includes a pressure equalization pipe (4), which is fixedly connected to and communicates with the air inlet pipe (3). The pressure equalization pipe (4) has multiple pressure equalization holes (5), which are evenly spaced along the circumferential direction of the pressure equalization pipe (4). The center lines of the equalizing pipe (4), the partition plate (6), and the air box (2) overlap.

6. The production apparatus for pyrometallurgical desulfurization of complex zinc concentrate as described in claim 5, characterized in that, The pressure equalization and dispersion air distribution structure includes two or more pressure equalization pipes (4). The multiple pressure equalization pipes (4) are stacked and interconnected along the height direction away from the wind box (2). The cross-section of the multiple pressure equalization pipes (4) gradually decreases from bottom to top.

7. The production apparatus for pyrometallurgical desulfurization of complex zinc concentrate as described in claim 5 or 6, characterized in that, The diameter of the equalizing holes (5) on the multiple equalizing pipes (4) from bottom to top gradually increases.

8. The production apparatus for pyrometallurgical desulfurization of complex zinc concentrate as described in claim 5 or 6, characterized in that, The furnace body (1) is equipped with a furnace opening device (8), an inspection window (9), a feed inlet (10), a discharge outlet (11), a heat dissipation device (12), an operating door (14), a smoke exhaust outlet (7), and a temperature detection device (13); the feed inlet (10) and the discharge outlet (11) are located at both ends of the material flow direction; The bellows (2) includes a box body (201) and a gas distribution plate (202). The box body (201) is in the shape of an inverted cone. The gas distribution plate (202) is fixedly connected to the top of the box body (201). The gas distribution plate (202) is provided with a plurality of ventilation holes evenly spaced on it. The partition plate (6) is fixedly connected to the box body and divides the box body into the first low-oxygen zone and the first oxygen-rich zone.

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