Method for recovering zinc and lead by synergistically treating zinc sulfite slag through zinc leaching slag volatilization kiln

Abstract

The invention relates to a method for recycling zinc and lead by cooperatively treating zinc sulfite residues through a zinc leaching residue volatilization kiln. The method comprises the following steps: (1) mixing zinc leaching residues, zinc sulfite residues and solid fuel according to a specific feeding amount to obtain mixed slag; and (2) uniformly mixing the mixed slag, then conveying the mixed slag into a volatilization kiln for reduction volatilization to obtain zinc-containing and lead-containing steam and kiln slag, oxidizing the zinc-containing and lead-containing steam to obtain zinc oxide flue gas, and finally capturing the zinc oxide flue gas through a dust collection facility to obtain a zinc oxide powder product. According to the scheme provided by the invention, a fluidized bed furnace roasting procedure is not introduced any more, the pretreatment steps of the raw materials are simple, the zinc sulfite residues are added into the zinc leaching residues and the solid fuel according to the specific feeding amount on the basis of an original zinc leaching residue volatilization kiln production process, the zinc sulfite residues can be recycled, and the production cost is reduced. The process steps are short, and control operation is simple.

Description

Technical Field

[0001] The present application relates to the technical field of zinc smelting, and in particular to a method for recovering zinc and lead by co-processing zinc sulfite slag with a zinc leaching slag volatilization kiln. Background Art

[0002] When treating the leaching slag produced in the process of hydrometallurgical zinc smelting, anthracite or coke is often added to the volatilization kiln to reduce and volatilize the valuable metals. The main product indicators are that the slag contains Zn <2% and the zinc oxide powder contains zinc >50%. In this process, low-concentration sulfur dioxide that needs further treatment will be produced. Because the zinc oxide powder produced in the zinc smelting process can be used as a raw material for the zinc oxide powder desulfurization process, zinc smelting enterprises often use the zinc oxide powder desulfurization process to remove the low-concentration sulfur dioxide in the zinc oxide powder, and then acid hydrolyze the zinc sulfite liquid produced after desulfurization. The sulfur dioxide obtained is sent to sulfuric acid for acid production, and the zinc sulfate liquid is purified and impurities are removed before comprehensive recovery. However, when the volatilization kiln is in normal production and the sulfuric acid process cannot be carried out due to shutdown and maintenance, the produced zinc sulfite liquid is filtered through a plate and frame filter press to become zinc sulfite slag, and is stored separately as inventory slag. However, the zinc content in zinc sulfite slag is 35% to 38%, and the lead content is 13% to 16%. If it is piled up for a long time, it will not only pose an environmental risk but also cause a waste of resources. Therefore, the zinc sulfite slag needs to be recycled.

[0003] In the prior art, for the treatment of the above-mentioned zinc sulfite slag, the publication number CN109161691A discloses a "comprehensive recovery and treatment method for zinc sulfite slag", which includes the following steps: 1) drying and crushing the zinc sulfite slag: taking the zinc sulfite slag to be treated, drying and dehydrating it so that the water content does not exceed 10wt%, and obtaining a dry zinc sulfite slag material; then crushing the dry zinc sulfite slag material to produce a zinc sulfite slag fine material with a particle size of 100wt% exceeding 60-100 meshes for standby use; 2) drying and crushing the zinc concentrate: taking the zinc concentrate and drying and dehydrating it at a temperature less than 300°C so that the water content does not exceed 10wt%, and obtaining a dry zinc concentrate material; then crushing the zinc concentrate The ore dry material is crushed to produce zinc concentrate fine material with a particle size of 100wt% exceeding 80-120 meshes for standby use; 3) Mixing: The crushed zinc sulfite slag fine material and the crushed zinc concentrate fine material are mixed, and the mixing ratio is zinc sulfite slag fine material: zinc concentrate fine material = 20wt%-35wt%, and the materials are required to be mixed evenly, loose and without agglomeration, and a mixed material is produced; 4) Fluidized bed roasting: The mixed material is fluidized bed roasted in a fluidized bed furnace, and the process control condition is a temperature of 950°C-1150°C, and a roasted ore with a sulfur content of less than 1wt% and sulfur dioxide flue gas for sulfuric acid production are produced. The roasted ore is used for wet zinc smelting, and the sulfur dioxide flue gas is used for acid production. The tail gas after acid production is absorbed and discharged in compliance with the standards.

[0004] Although the method realizes the treatment of zinc sulfite slag, the treatment of zinc sulfite slag in the method at least needs to go through the following steps: drying and crushing the zinc sulfite slag and zinc concentrate respectively, so that the zinc sulfite slag and zinc concentrate meet the raw material index of roasting, and then mixing the two in a certain proportion and entering the fluidized bed furnace for boiling roasting, producing zinc roasted ore that can be used as a raw material for wet zinc smelting and high-concentration sulfur dioxide gas for making sulfuric acid; thereby realizing the harmless utilization of zinc sulfite. From the above description, it can be seen that although the method carries out fine drying, crushing and proportioning of zinc sulfite slag and zinc concentrate, so that the raw materials meet the requirements of the fluidized bed furnace, the steps are lengthy. In addition, since the Pb content in the zinc sulfite slag is greater than 13%, which is far higher than the requirement of less than 2% of the raw material controlled by the fluidized bed furnace, a slightly uneven batching process can easily lead to sintering and death of the fluidized bed furnace, which seriously restricts the normal operation of the fluidized bed furnace and requires high control operation.

[0005] Therefore, for the recovery of zinc and lead in zinc sulfite slag, how to provide a recovery method with short process steps and simple control operation on the basis of ensuring that the product indicators of the volatilization kiln are qualified. Summary of the invention

[0006] The present application provides a method for recovering zinc and lead by co-processing zinc sulfite slag with a zinc leaching slag volatilization kiln. The method no longer introduces a boiling furnace roasting process, and the pretreatment steps of the raw materials are simple. On the basis of the original zinc leaching slag volatilization kiln production process, the zinc sulfite slag is added to the zinc leaching slag and solid fuel through a specific feed amount, so that the zinc sulfite slag can be recovered and processed, and the process steps are short and the control operation is simple.

[0007] The present application provides a method for recovering zinc and lead by co-processing zinc sulfite slag with a zinc leaching slag volatilization kiln, comprising the following steps:

[0008] (1) mixing zinc leaching slag, zinc sulfite slag and solid fuel at specific feed rates to obtain mixed slag, wherein the feed rate of the zinc leaching slag is 9-11 t / h, the feed rate of the zinc sulfite slag is 1-1.5 t / h, and the solid fuel is anthracite or coke having a carbon content of ≥70% and a feed rate of 4-5 t / h;

[0009] (2) The mixed slag is mixed and then transported to a volatilization kiln for reduction volatilization. The temperature at the tail of the volatilization kiln is 550°C to 600°C, the negative pressure at the tail of the kiln is -20Pa to 20Pa, and the blast pressure at the head of the kiln is 0.06MPa to 0.08MPa, thereby obtaining zinc-containing lead-containing vapor and kiln slag. The zinc-containing lead-containing vapor is oxidized to obtain zinc oxide fume, and finally the zinc oxide fume is captured by a dust collection facility to obtain a zinc oxide powder product.

[0010] Optionally, the zinc leaching slag includes main components and their mass percentages: Zn 13%-15%, Pb 5%-8%, and the zinc sulfite slag includes main components and their mass percentages: Zn 35%-38%, Pb 13%-16%.

[0011] Optionally, after the mixed slag is evenly mixed in step (2), slag pellets are obtained, and the moisture content and mass percentage of the slag pellets are 18% to 21%, and the particle size is 0 to 10 mm.

[0012] Optionally, the zinc oxide powder product in step (2) includes main components and their mass percentages are: Zn 50% to 58%, Pb 15% to 22%.

[0013] Optionally, the main components of the slag in step (2) and their mass percentages are Zn<2%, Pb<1.5%.

[0014] Principle of the invention:

[0015] In the zinc leaching slag volatilization kiln production system, when the volatilization kiln is in normal production, but the sulfuric acid process cannot carry out acid hydrolysis due to shutdown and maintenance, the produced zinc sulfite liquid is filtered through a plate and frame filter press to become zinc sulfite slag, and is stored separately as inventory slag. When the sulfuric acid process is operating normally, the zinc sulfite liquid produced by the zinc oxide powder desulfurization system enters the sulfuric acid process for acid hydrolysis, and the obtained sulfur dioxide is sent to sulfuric acid for acid production, and the zinc sulfate liquid is purified and impurities are removed before comprehensive recovery.

[0016] In the present application, when the sulfuric acid process operates normally, by appropriately adding zinc sulfite slag to the zinc leaching slag raw material, the original production indicators will not be deteriorated and the production cost will not be greatly increased. However, as the feed amount of zinc sulfite slag increases, the sulfur content in the zinc oxide flue gas increases simultaneously, which will cause the load of the subsequent zinc oxide powder desulfurization system to increase. Therefore, the optimal feed amount of zinc sulfite slag needs to be set according to the maximum sulfur content of the zinc oxide flue gas that the zinc oxide powder desulfurization system can load.

[0017] This application has at least the following beneficial effects:

[0018] 1. The present application combines the characteristics of the zinc leaching slag volatilization kiln production process that requires excess carbon, and does not require additional solid fuel and other materials. The existing zinc leaching slag volatilization kiln production equipment and facilities are used to mix zinc sulfite slag, zinc leaching slag and solid fuel according to a specific feed amount in a specific ratio, and then reduce and volatilize to obtain zinc-containing lead vapor, and then further oxidize the zinc-containing lead vapor to obtain zinc oxide flue gas. By collecting and capturing the zinc oxide flue gas, a zinc oxide powder product can be obtained, thereby realizing the product recovery of zinc and lead in the zinc sulfite slag;

[0019] 2. Compared with the prior art, the present application no longer introduces the boiling furnace roasting process. On the basis of the original zinc leaching slag volatilization kiln production process, the zinc sulfite slag is added to the zinc leaching slag and the solid fuel by a specific feeding amount, so that the zinc sulfite slag can be recycled and processed, and the operation is simple;

[0020] 3. Compared with the volatilization kiln, the boiling furnace has more precise control over the particle size and water content of the raw materials, and the processing steps of the raw materials are relatively lengthy. The present invention uses the volatilization kiln to volatilize and reduce the raw materials, and the raw materials can be pre-treated by mixing the zinc sulfite slag, zinc leaching slag and solid fuel according to a specific feed amount, and the steps are short;

[0021] 4. In the present invention, the zinc sulfite slag is added to the zinc leaching slag and the solid fuel by a specific feeding amount, which does not affect the product index of the zinc content in the kiln slag and the zinc oxide powder product in the original volatilization kiln process, and the zinc sulfite slag is recovered while the zinc leaching slag volatilization kiln process is normally operated. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] The above and other objects, features and advantages of the present application will become more apparent through a more detailed description of exemplary embodiments of the present application in conjunction with the accompanying drawings, wherein the same reference numerals generally represent the same components in the exemplary embodiments of the present application.

[0023] Figure 1 It is the process flow chart of this application. DETAILED DESCRIPTION

[0024] The embodiments of the present application will be described in more detail below with reference to the accompanying drawings. Although the embodiments of the present application are shown in the accompanying drawings, it should be understood that the present application can be implemented in various forms and should not be limited by the embodiments described herein. On the contrary, these embodiments are provided to make the present application more thorough and complete, and to fully convey the scope of the present application to those skilled in the art.

[0025] It should be understood that although the terms "first", "second", "third", etc. may be used in this application to describe various information, this information should not be limited to these terms. These terms are only used to distinguish the same type of information from each other. For example, without departing from the scope of this application, the first information may also be referred to as the second information, and similarly, the second information may also be referred to as the first information. Thus, the features defined as "first" and "second" may explicitly or implicitly include one or more of the features. In the description of this application, the meaning of "multiple" is two or more, unless otherwise clearly and specifically defined.

[0026] In order to make the objectives, technical solutions and beneficial effects of the present invention clearer, the preferred embodiments of the present invention will be described in detail below to facilitate understanding by technicians.

[0027] Example 1

[0028] 1. In the production process of zinc leaching slag volatilization kiln, the main components and their mass percentages of zinc leaching slag are: Zn~13.5%, Pb~6%, Fe~19.8%, SiO 2 ~6.5%、S~7%、H 2 O~23%, the main components and their mass percentages of zinc sulfite slag are: Zn~37.11%, Pb~14.78%, Fe~2.23%, SiO 2 ~1.85%、S~15.27%、H 2 O~13%, anthracite is used as solid fuel, and its main components and their mass percentages are: C~70%, ash~19%, volatile matter~10%;

[0029] 2. Mix zinc leaching slag, zinc sulfite slag and solid fuel according to specific feeding amounts to obtain mixed slag, wherein the feeding amount of the belt scale of the leaching slag bin is 10 t / h, the feeding amount of the belt scale of the solid fuel bin is 4.5 t / h, and the feeding amount of the zinc sulfite slag is 1 t / h;

[0030] 4. The mixed slag is further mixed to obtain slag pellets, the water content and mass percentage of the slag pellets are 18.6%, of which the slag pellets with a particle size of 5 to 10 mm account for 35%, and the slag pellets with a particle size of 0 to 5 mm account for 65%;

[0031] 5. The obtained mixed material enters the volatilization kiln and is reduced and volatilized by process control, wherein the temperature at the kiln tail is controlled at 550-600°C, the negative pressure at the kiln tail is 0-20Pa, and the blast pressure at the kiln head is 0.06MPa. The main components and their mass percentages of the collected zinc oxide powder products are: Zn-53.2%, Pb-21.8%, Fe-3.97%, SiO 2 ~1.74%, S~4.52%, the main components and their mass percentages of the produced slag are: Zn~1.7%, Pb~1.1%, Fe~25.1%, SiO 2 ~20.5%, S~7.3%, C~20.5%, the slag is discharged from the kiln head and taken away after water quenching.

[0032] Analysis of product indicators shows that the Zn content in the obtained kiln slag is 1.7% < 2%, and the Zn content in the zinc oxide powder product is 53.2% > 50%. The product indicators are within the range allowed by the process, and the recovery and utilization of zinc and lead in the zinc sulfite slag is also achieved.

[0033] By processing the data, it can be seen that the recovery rate of zinc in the zinc oxide powder product is 92.4%, and the recovery rate of lead is 91.9%.

[0034] The recovery rate of zinc per unit time = (zinc content in zinc leaching slag + zinc content in zinc sulfite slag - zinc content lost in kiln slag) / (zinc content in zinc leaching slag + zinc content in zinc sulfite slag).

[0035] Lead recovery rate = (lead content in zinc leaching residue + lead content in zinc sulfite residue - lead content lost in kiln slag) / (lead content in zinc leaching residue + lead content in zinc sulfite residue)

[0036] Example 2

[0037] A certain enterprise uses a 3.45*52m volatilization kiln to treat zinc leaching residue and uses zinc oxide powder for desulfurization. During the normal production process of the volatilization kiln, due to the annual maintenance of the sulfuric acid process and the large volume of the wet system that cannot be connected to the liquid in time, a total of about 700 tons of zinc sulfite slag has been piled up in the warehouse and has not been effectively utilized. The long-term storage of the inventory slag has resulted in the inability to effectively utilize the valuable metals in a timely manner, and there is a great environmental risk. Based on this, combined with the production process characteristics of the volatilization kiln, it is proposed to use zinc leaching residue volatilization kiln to coordinately treat zinc sulfite slag.

[0038] The specific steps are as follows:

[0039] 1. The crane loads zinc leaching slag, zinc sulfite slag and solid fuel into the corresponding silos respectively. The main components and their mass percentages of zinc leaching slag are: Zn~13.5%, Pb~6%, Fe~17.5%, SiO 2 ~6.5%、S~7%、H 2 O~23%, the main components and their mass percentages of zinc sulfite slag are: Zn~37.11%, Pb~14.78%, Fe~2.23%, SiO 2 ~1.85%、S~15.27%、H 2 O~13%, solid fuel is coke, its main components and their mass percentages are: C~70%, ash~18%, volatile matter~11%, S~1%;

[0040] 2. Start the electronic belt scales of zinc leaching slag bin and solid fuel bin. The feeding rate of the belt scale of zinc leaching slag bin is 10t / h, and the feeding rate of the belt scale of solid fuel bin is 4.5t / h;

[0041] 3. Start the electronic belt scale for zinc sulfite slag and the feeding double-axis screw, and break the zinc sulfite slag agglomerates while feeding quantitatively to the mixed material belt. The feeding rate of the belt scale is 1t / h;

[0042] 4. The mixed material on the mixing belt is transported to the mixing drum for further mixing to obtain slag pellets. The moisture content and mass percentage of the slag pellets are 18.6%, of which slag pellets with a particle size of 5 to 10 mm account for 35% and slag pellets with a particle size of 0 to 5 mm account for 65%;

[0043] 5. The obtained mixed material enters the kiln through the kiln tail discharge chute, and the reduction volatilization process is controlled by the process, wherein the kiln tail temperature is controlled at 550℃~600℃, the kiln tail negative pressure is 0Pa~20Pa, and the kiln head blast pressure is 0.06MPa. The main components and their mass percentages of the collected zinc oxide powder products are: Zn~52.7%, Pb~22.6%, Fe~6.07%, SiO 2 ~0.95%, S~4.48%, the main components and their mass percentages of the produced slag are: Zn~1.95%, Pb~0.95%, Fe~23%, SiO 2 ~18.9%, S~6.7%, C~20.5%, the slag is discharged from the kiln head and taken away after water quenching.

[0044] Analysis of the product indicators shows that the Zn content in the obtained kiln slag is 1.95% < 2%, and the Zn content in the zinc oxide powder product is 52.7% > 50%. The product indicators are within the range allowed by the process. At the same time, the recovery and utilization of zinc and lead in the zinc sulfite slag is also achieved. According to this method, it is expected that all the inventory of zinc sulfite slag can be consumed within 1 to 2 months.

[0045] By processing the data, it can be seen that the recovery rate of zinc in the zinc oxide powder product is 92.3%, and the recovery rate of lead is 91.4%.

[0046] Example 3

[0047] The specific steps are as follows:

[0048] 1. The crane loads zinc leaching slag, zinc sulfite slag and solid fuel into the corresponding silos respectively. The main components and their mass percentages of zinc leaching slag are: Zn~15%, Pb~8%, Fe~16.7%, SiO 2 ~5.7%、S~6.8%、H 2 O~22.3%, the main components and their mass percentages of zinc sulfite slag are: Zn~38%, Pb~16%, Fe~2.1%, SiO 2 ~1.6%、S~15.87%、H 2 O~12.2%, anthracite is used as solid fuel, and its main components and their mass percentages are: C~70%, ash~18%, volatile matter~11%, S~1%;

[0049] 2. Start the electronic belt scales of zinc leaching slag bin and solid fuel bin. The feeding rate of zinc leaching slag bin belt scale is 11t / h, and the feeding rate of solid fuel bin belt scale is 4.5t / h;

[0050] 3. Start the electronic belt scale for zinc sulfite slag and the feeding double-axis screw, and break the zinc sulfite slag agglomerates while feeding quantitatively to the mixed material belt. The feeding rate of the belt scale is 1.5t / h;

[0051] 4. The mixed material on the mixing belt is transported to the mixing drum for further mixing to obtain slag pellets. The moisture content and mass percentage of the slag pellets are 17.9%, of which slag pellets with a particle size of 5 to 10 mm account for 35% and slag pellets with a particle size of 0 to 5 mm account for 65%;

[0052] 5. The obtained mixed material enters the kiln through the kiln tail discharge chute, and the reduction volatilization process is controlled by the process, wherein the kiln tail temperature is controlled at 550℃~600℃, the kiln tail negative pressure is 0Pa~20Pa, and the kiln head blast pressure is 0.06MPa. The main components and their mass percentages of the collected zinc oxide powder products are: Zn~63%, Pb~31%, Fe~4.38%, SiO 2 ~1.13%, S~7.59%, the main components and their mass percentages of the produced slag are: Zn~1.88%, Pb~0.92%, Fe~22.9%, SiO 2 ~18.1%, S~4.41%, C~21.2%, the slag is discharged from the kiln head and taken away after water quenching.

[0053] The analysis of product indicators shows that the Zn content in the obtained slag is 1.92%<2%, and the Zn content in the zinc oxide powder product is 63%>50%, and the product indicators are within the process allowable indicator range. Through data processing, it is known that the recovery rate of zinc in the zinc oxide powder product is 93.6%, and the recovery rate of lead is 92.1%.

[0054] Comparative Example 1

[0055] Compared with the above-mentioned Example 2, other conditions remain unchanged, only zinc sulfite slag is no longer added, and the main components and their mass percentages of the collected zinc oxide powder product are: Zn~51.2%, Pb~21.5%, Fe~6.79%, SiO 2 ~3.23%, S~3.32%, the main components and their mass percentages of the produced slag are: Zn~1.7%, Pb~0.9%, Fe~23%, SiO 2 ~17.9%, S~6.7%, C~22.5%, the slag is discharged from the kiln head and taken away after water quenching.

[0056] The analysis of product indicators shows that the Zn content in the obtained kiln slag is 1.7%<2%, and the Zn content in the zinc oxide powder product is 51.2%>50%, and the product indicators are within the process allowable indicator range. Through data processing, it is known that the recovery rate of zinc in the zinc oxide powder product is 91.3%, and the recovery rate of lead is 90%.

[0057] Data analysis: compared with implementation 2, the recovery rate of zinc decreased from 92.3% to 91.3%, and the recovery rate of lead decreased from 91.4% to 90%, indicating that the specific feed rate can be used to recover zinc and lead in zinc sulfite slag. Adding zinc sulfite slag to the raw materials according to a specific feed rate will not affect the zinc content of the slag and zinc oxide powder products obtained in the original zinc leaching slag volatilization kiln process, thereby achieving the recovery of zinc sulfite slag while the leaching slag volatilization kiln process operates normally.

[0058] Comparative Example 2

[0059] Compared with the above Example 2, other conditions remain unchanged, only the feeding amounts of zinc leaching residue, zinc sulfite residue and solid fuel are changed, and data analysis is performed:

[0060] It is known that the maximum sulfur content of zinc oxide flue gas that the zinc oxide powder desulfurization system can load is 38%.

[0061]

[0062]

[0063] From projects 2 to 6, it can be seen that the feed amount of zinc leaching slag and solid fuel remains unchanged. As the feed amount of zinc sulfite slag gradually increases, the recovery rates of zinc and lead gradually increase, but the sulfur content in zinc oxide flue gas also gradually increases, indicating that the increase in the feed amount of zinc sulfite slag will lead to an increase in the load of the subsequent zinc oxide powder desulfurization system. Therefore, the optimal feed amount of zinc sulfite slag needs to be set according to the maximum sulfur content of zinc oxide flue gas that the zinc oxide powder desulfurization system can load. The optimal feed amount of zinc sulfite slag is 1-1.5t / h.

[0064] Finally, it should be noted that, in this article, relationships such as first and second, etc. are used only to distinguish one entity or operation from another entity or operation, and do not necessarily require or imply any such actual relationship or order between these entities or operations. Moreover, the terms include, include or any other variations are intended to cover non-exclusive inclusion, so that a process, method, article or device that includes a series of elements includes not only those elements, but also other elements not explicitly listed, or also includes elements inherent to such process, method, article or device.

[0065] The embodiments of the present application have been described above, and the above description is exemplary, not exhaustive, and is not limited to the disclosed embodiments. Many modifications and changes will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments. The selection of terms used herein is intended to best explain the principles of the embodiments, practical applications, or improvements to the technology in the market, or to enable other persons of ordinary skill in the art to understand the embodiments disclosed herein.

Claims

1. A method for recovering zinc and lead by co-processing zinc sulfite slag with a zinc leaching slag volatilization kiln, characterized in that: The following steps are involved: (1) mixing zinc leaching slag, zinc sulfite slag and solid fuel at specific feed rates to obtain mixed slag, wherein the feed rate of the zinc leaching slag is 9-11 t / h, the feed rate of the zinc sulfite slag is 1-1.5 t / h, and the solid fuel is anthracite or coke having a carbon content of ≥70% and a feed rate of 4-5 t / h; (2) The mixed slag is mixed and then transported to a volatilization kiln for reduction volatilization. The temperature at the tail of the volatilization kiln is 550°C to 600°C, the negative pressure at the tail of the kiln is -20Pa to 20Pa, and the blast pressure at the head of the kiln is 0.06MPa to 0.08MPa, thereby obtaining zinc-containing lead-containing vapor and kiln slag. The zinc-containing lead-containing vapor is oxidized to obtain zinc oxide fume, and finally the zinc oxide fume is captured by a dust collection facility to obtain a zinc oxide powder product.

2. The method according to claim 1, characterized in that The zinc leaching slag includes main components and their mass percentages: Zn 13%-15%, Pb 5%-8%, and the zinc sulfite slag includes main components and their mass percentages: Zn 35%-38%, Pb 13%-16%.

3. The method according to claim 1, characterized in that After the slag is mixed and evenly mixed in step (2), slag pellets are obtained. The moisture content and mass percentage of the slag pellets are 18% to 21%, and the particle size is 0 to 10 mm.

4. The method according to claim 1, characterized in that The zinc oxide powder product in step (2) comprises the following main components and their mass percentages: Zn 50% to 58%, Pb 15% to 22%.

5. The method according to claim 1, characterized in that: The main components of the slag in step (2) are Zn<2% and Pb<1.5% by mass.

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