阅读说明：本技术 阳极泥处理方法 (Anode mud treatment method ) 是由 许良 彭思尧 吴卫国 梁帅表 于 2020-11-11 设计创作，主要内容包括：本发明提供了一种阳极泥处理方法,首先将阳极泥和还原剂按预设重量比混合以便得到第一混合物料,对第一混合物料进行还原熔炼以便得到一次贵铅、一次炉渣和一次烟灰,还原熔炼在800℃-1000℃的条件下进行。再利用锑白炉对一次贵铅进行一次精炼,使得一次贵铅中的贱金属挥发,以便得到二次贵铅和二次烟灰。而后利用分银炉对二次贵铅进行二次精炼,以便得到金银合金和三次烟灰。本发明提供的阳极泥处理方法具有无需使用造渣剂和/或熔剂、渣率低、提高耐火材料的使用寿命、处理量大、处理效率高、能耗低和环保等特点。(The invention provides an anode mud treatment method, which comprises the steps of firstly mixing anode mud and a reducing agent according to a preset weight ratio to obtain a first mixed material, carrying out reduction smelting on the first mixed material to obtain first precious lead, first slag and first soot, and carrying out the reduction smelting at the temperature of 800-1000 ℃. And then, carrying out primary refining on the primary precious lead by using an antimony white furnace to volatilize base metals in the primary precious lead so as to obtain secondary precious lead and secondary soot. And then, carrying out secondary refining on the secondary precious lead by using a silver separating furnace so as to obtain a gold-silver alloy and tertiary soot. The anode mud treatment method provided by the invention has the characteristics of no need of using a slagging agent and/or a flux, low slag rate, long service life of a refractory material, large treatment capacity, high treatment efficiency, low energy consumption, environmental friendliness and the like.)

1. The anode mud treatment method is characterized by comprising the following steps:

a. mixing anode mud and a reducing agent according to a preset weight ratio to obtain a first mixed material, and carrying out reduction smelting on the first mixed material to obtain primary noble lead, primary slag and primary soot, wherein the reduction smelting is carried out at the temperature of 800-1000 ℃;

b. carrying out primary refining on the primary precious lead by using an antimony white furnace to volatilize base metals in the primary precious lead so as to obtain secondary precious lead and secondary soot; and

c. and (4) carrying out secondary refining on the secondary precious lead by using a silver separating furnace so as to obtain a gold-silver alloy and tertiary soot.

2. The anode slime treatment method according to claim 1, wherein said tertiary soot is mixed as a return with said anode slime and said reducing agent to obtain said first mixed material including said tertiary soot.

3. The anode slime treatment method according to claim 2, characterized in that: and mixing the anode mud, the tertiary soot and the reducing agent according to a preset weight ratio, and granulating by using a granulator to obtain the granular first mixed material.

4. The anode slime treatment method according to claim 2, characterized in that: the reducing agent is crushed coal or coke, the reduction smelting uses natural gas or pulverized coal as fuel, and the reduction smelting uses oxygen-enriched air as combustion-supporting gas;

in the reduction smelting, lead and antimony in the anode slime are oxidized to obtain the primary slag, arsenic and antimony in the anode slime are volatilized to obtain the primary soot, and the monomeric gold, the monomeric silver and the reduced silver, lead, antimony and bismuth in the anode slime form the primary noble lead;

optionally, the crushed coal is 3-10% of the sum of the weight of the anode mud and the tertiary soot, and optionally, the oxygen-enriched air has an oxygen concentration of 25-99%.

5. The anode slime treatment method according to claim 1, characterized in that: the anode mud is at least one of lead anode mud and copper anode mud.

6. The anode slime treatment method according to claim 1, characterized in that: the reduction smelting is carried out at the temperature of 900-1000 ℃;

optionally, the primary precious lead and the primary slag are discharged from the side-blown furnace periodically, and optionally, the discharge period of the primary precious lead and the primary slag is 2 hours to 5 hours.

7. The anode slime treatment method according to claim 1, characterized in that:

in the primary refining, the primary noble lead is blown and oxidized by the antimony white furnace, arsenic and antimony in the primary noble lead are volatilized to obtain the secondary soot enriched with arsenic and antimony, and the secondary noble lead is formed after arsenic and antimony are removed from the primary noble lead;

optionally, the furnace temperature of the antimony white furnace is 700-900 ℃, and optionally, the antimony white furnace is a converter, an electric furnace, a refining pot or a reverberatory furnace.

8. The anode slime treatment method according to claim 1, characterized in that: mixing the primary slag and a reducing agent according to a preset weight ratio to obtain a second mixed material, and carrying out slag depletion treatment on the second mixed material by using a depletion furnace to obtain low-grade noble lead, secondary slag and depleted soot, wherein the slag depletion is carried out at the temperature of 1000-1200 ℃;

optionally, mixing the secondary precious lead and the low-grade precious lead, and performing secondary refining on the mixture of the secondary precious lead and the low-grade precious lead;

or mixing the primary precious lead and the low-grade precious lead, and performing primary refining on the mixture of the primary precious lead and the low-grade precious lead.

9. The anode slime treatment method according to claim 8, characterized in that: and the second mixed material is subjected to heat preservation and sedimentation in the dilution furnace, and the low-grade noble lead is formed by the monomer gold and the monomer silver in the primary furnace slag and the reduced silver, lead, antimony and bismuth.

10. The anode slime treatment method according to claim 1, characterized in that: the silver separating furnace adopts oxygen-enriched gas as an oxidant;

optionally, the oxygen-enriched gas is blown in an amount of 50Nm³/h-150Nm³Optionally, the oxygen-enriched air has an oxygen concentration of 25% to 99%.

Technical Field

The invention relates to the technical field of nonferrous technology smelting, in particular to an anode mud treatment method.

Background

Anode mud produced in the electrolytic refining process of nonferrous metals such as copper, lead and the like can be enriched with a large amount of rare and precious metals, and the anode mud is an important source for extracting rare and precious metals such as gold, silver, antimony, bismuth, tellurium and the like. The lead anode slime treatment generally adopts a combined process of a fire method and a wet method, but the technology has longer production period and poorer production environment. The pyrogenic process for treating the copper anode slime mostly adopts a Kaldo furnace introduced abroad, so that the investment is large, the returned materials are more, and the produced furnace slag is inconvenient to recover. The commonly used wet treatment technology of the copper anode slime has the disadvantages of large reagent consumption, large amount of generated wastewater, long process flow and poor applicability.

Although the conventional technology for treating anode mud by a pyrogenic process is simple in technological process, strong in adaptability and simple in equipment, various problems still exist, such as low comprehensive utilization rate of valuable metals, high energy consumption, low automation degree, poor operation environment, requirement of stockpiling and pre-oxidation of raw materials, low equipment treatment efficiency, incapability of meeting the turnover requirement of modern smelting plants and the like, and the development of the technology for treating anode mud by the pyrogenic process is restricted by the factors.

Disclosure of Invention

The present invention is directed to solving, at least to some extent, one of the technical problems in the related art. Therefore, the embodiment of the invention provides an anode mud treatment method.

According to an embodiment of the invention, the anode mud treatment method comprises the following steps:

a. mixing anode mud and a reducing agent according to a preset weight ratio to obtain a first mixed material, and carrying out reduction smelting on the first mixed material to obtain primary noble lead, primary slag and primary soot, wherein the reduction smelting is carried out at the temperature of 800-1000 ℃;

b. carrying out primary refining on the primary precious lead by using an antimony white furnace to volatilize base metals in the primary precious lead so as to obtain secondary precious lead and secondary soot; and

c. and (4) carrying out secondary refining on the secondary precious lead by using a silver separating furnace so as to obtain a gold-silver alloy and tertiary soot.

According to the anode mud treatment method provided by the embodiment of the invention, the anode mud and the reducing agent are subjected to reduction smelting, so that the slag can be formed by utilizing the self-contained components of the anode mud, the preparation of materials in advance is not needed, and a slag forming agent and/or a flux are not needed to be added. Therefore, not only can the slagging agent and/or the fluxing agent be saved and the slag rate be reduced, but also the erosion of the fluxing agent to the refractory material in the side blowing furnace can be reduced.

According to the anode mud treatment method provided by the embodiment of the invention, the reduction smelting is carried out at the temperature of 800-1000 ℃, so that the temperature of a molten pool in a furnace kiln is lower, the fuel is saved, the energy consumption is reduced, the unorganized emission of volatile elements can be reduced, the smoke yield is reduced, and the field environment is improved.

In addition, the reduction smelting is carried out by using the side-blown converter, the temperature of the converter can be more effectively controlled, and the operation is simple. The side-blown furnace is internally provided with a molten pool for side-blowing, so that the melt and the first mixed material can be stirred, the first mixed material can be rapidly dispersed in the melt, the melting and the reduction of the first mixed material can be more favorably realized, and the treatment efficiency of the anode mud can be greatly improved. In addition, the side-blown converter can continuously process materials, so the anode mud processing method provided by the invention has the characteristics of large processing capacity, high operation efficiency and the like.

The antimony white furnace is adopted to refine the primary precious lead for one time, so that the processing burden of the silver separating furnace can be effectively reduced, and the operation efficiency of the silver separating furnace is improved. In an antimony white furnace, a large amount of volatile base metals in the primary precious lead volatilize and are enriched to form secondary soot, and the soot has single component, so that the base metals are convenient to recover. And finally, secondary refining is performed by adopting a silver separating furnace, the technology for refining the precious lead by adopting the silver separating furnace is mature, the operation is skilled, and the product quality is easy to control.

Therefore, the anode mud treatment method provided by the invention has the characteristics of no need of using a slagging agent and/or a flux, low slag rate, long service life of the refractory material, large treatment capacity, high treatment efficiency, low energy consumption, environmental friendliness and the like.

In addition, the anode mud treatment method also has the following additional technical characteristics:

in some embodiments, the tertiary soot is mixed as a return with the anode slime and the reducing agent to obtain the first mixed material comprising the tertiary soot.

In some embodiments, the anode slime, the tertiary soot and the reducing agent are mixed in a predetermined weight ratio and then granulated using a granulator to obtain the first mixed material in a granular form.

In some embodiments, the reducing agent is crushed coal or coke breeze, the reduction smelting utilizes natural gas or pulverized coal as fuel, and the reduction smelting utilizes oxygen-enriched air as combustion-supporting gas; in the reduction smelting, lead and antimony in the anode slime are oxidized to obtain the primary slag, arsenic and antimony in the anode slime are volatilized to obtain the primary soot, and the monomeric gold, the monomeric silver and the reduced silver, lead, antimony and bismuth in the anode slime form the primary noble lead; optionally, the crushed coal is 3-10% of the sum of the weight of the anode mud and the tertiary soot, and optionally, the oxygen-enriched air has an oxygen concentration of 25-99%.

In some embodiments, the anode slime is at least one of lead anode slime and copper anode slime.

In some embodiments, the reduction smelting is carried out at a temperature of 900 ℃ to 1000 ℃; optionally, the primary precious lead and the primary slag are discharged from the side-blown furnace periodically, and optionally, the discharge period of the primary precious lead and the primary slag is 2 hours to 5 hours.

In some embodiments, in the primary refining, the primary precious lead is subjected to blowing oxidation by using the antimony white furnace, arsenic and antimony in the primary precious lead are volatilized to obtain the secondary ash enriched with arsenic and antimony, and the primary precious lead is subjected to arsenic and antimony removal to form secondary precious lead; optionally, the furnace temperature of the antimony white furnace is 700-900 ℃, and optionally, the antimony white furnace is a converter, an electric furnace, a refining pot or a reverberatory furnace.

In some embodiments, the primary slag and the reducing agent are mixed according to a preset weight ratio to obtain a second mixed material, and the second mixed material is subjected to slag depletion treatment by using a depletion furnace to obtain low-grade precious lead, secondary slag and depleted soot, wherein the slag depletion is performed at the temperature of 1000-1200 ℃; optionally, mixing the secondary precious lead and the low-grade precious lead, and performing secondary refining on the mixture of the secondary precious lead and the low-grade precious lead; or mixing the primary precious lead and the low-grade precious lead, and performing primary refining on the mixture of the primary precious lead and the low-grade precious lead.

In some embodiments, the second mixed material is subjected to heat preservation and sedimentation in the dilution furnace, and the single gold, the single silver and the reduced silver, the lead, the antimony and the bismuth in the primary slag form the low-grade noble lead.

In some embodiments, the silver separation furnace uses oxygen-rich gas as an oxidant; optionally, the oxygen-enriched gas is blown in an amount of 50Nm³/h-150Nm³Optionally, the oxygen-enriched air has an oxygen concentration of 25% to 99%.

Additional aspects and advantages of the invention will be set forth in part in the description which follows and, in part, will be obvious from the description, or may be learned by practice of the invention.

Drawings

Fig. 1 is a flow chart of an anode slime treatment method according to an embodiment of the present invention.

Detailed Description

Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings. The embodiments described below with reference to the drawings are illustrative and intended to be illustrative of the invention and are not to be construed as limiting the invention.

A flow chart of an anode sludge treatment method according to an embodiment of the present invention is described below with reference to fig. 1.

As shown in fig. 1, the anode slime treatment method according to the embodiment of the invention comprises the following steps:

a. mixing anode mud and a reducing agent according to a preset weight ratio to obtain a first mixed material, feeding the first mixed material into a side-blown furnace, and carrying out reduction smelting in the side-blown furnace to obtain primary noble lead, primary slag and primary soot, wherein the reduction smelting is carried out at the temperature of 800-1000 ℃.

b. And (3) feeding the primary precious lead into an antimony white furnace for primary refining, so that a large amount of volatile base metals in the primary precious lead volatilize, and secondary precious lead and secondary soot are obtained.

c. And (4) feeding the secondary precious lead into a silver separating furnace for secondary refining so as to obtain a gold-silver alloy rich in precious metals such as gold and silver and the like and tertiary soot.

According to the anode mud treatment method provided by the embodiment of the invention, the anode mud and the reducing agent are subjected to reduction smelting, so that the slag can be formed by utilizing the self-contained components of the anode mud, the preparation of materials in advance is not needed, and a slag forming agent and/or a flux are not needed to be added. Therefore, not only can the slagging agent and/or the fluxing agent be saved and the slag rate be reduced, but also the erosion of the fluxing agent to the refractory material in the side blowing furnace can be reduced. The slag rate in some embodiments of the invention is reduced by more than 10% compared to processes in which slag formers and/or fluxes are added.

According to the anode mud treatment method provided by the embodiment of the invention, the reduction smelting is carried out at the temperature of 800-1000 ℃, so that the temperature of a molten pool in a furnace kiln is lower, the fuel is saved, the energy consumption is reduced, the unorganized emission of volatile elements can be reduced, the smoke yield is reduced, and the field environment is improved.

In addition, the reduction smelting is carried out by using the side-blown converter, the temperature of the converter can be more effectively controlled, and the operation is simple. The side-blown furnace is internally provided with a molten pool for side-blowing, so that the melt and the first mixed material can be stirred, the first mixed material can be rapidly dispersed in the melt, the melting and the reduction of the first mixed material can be more favorably realized, and the treatment efficiency of the anode mud can be greatly improved. In addition, the side-blown converter can continuously process materials, so the anode mud processing method provided by the invention has the characteristics of large processing capacity, high operation efficiency and the like.

The antimony white furnace is adopted to refine the primary precious lead for one time, so that the processing burden of the silver separating furnace can be effectively reduced, and the operation efficiency of the silver separating furnace is improved. In an antimony white furnace, a large amount of volatile base metals in the primary precious lead volatilize and are enriched to form secondary soot, and the soot has single component, so that the base metals are convenient to recover. And finally, secondary refining is performed by adopting a silver separating furnace, the technology for refining the precious lead by adopting the silver separating furnace is mature, the operation is skilled, and the product quality is easy to control.

Therefore, the anode mud treatment method provided by the invention has the characteristics of no need of using a slagging agent and/or a flux, low slag rate, long service life of the refractory material, large treatment capacity, high treatment efficiency, low energy consumption, environmental protection, simple equipment, lower cost and the like.

As shown in fig. 1, in the anode slime treatment method provided in the embodiment of the present invention, the anode slime is at least one of lead anode slime and copper anode slime, that is, the anode slime may be lead anode slime after deleading or copper anode slime after copper removal, or may be mixed anode slime including lead anode slime and copper anode slime.

By way of example, in the anode slime treatment method provided by the embodiment of the invention, the tertiary soot discharged from the silver separation furnace can be used as a return material and mixed with the anode slime and the reducing agent according to a preset weight ratio, so that a first mixed material comprising the tertiary soot is obtained.

Optionally, the reducing agent is crushed coal or coke. When the crushed coal is used as the reducing agent, the weight of the crushed coal is 3 to 10 percent of the sum of the weight of the anode mud and the weight of the tertiary soot.

Further, the first mixed material is granulated using a granulator to obtain a granulated first mixed material. And continuously feeding the granular first mixed material into the side-blown furnace by using the feeder so as to perform reduction smelting in the side-blown furnace. The first mixed material is made into particles, so that the dust raising of the material in the transfer process can be reduced, and the smoke dust rate is reduced. Alternatively, the granulator used may be one of a cylinder granulator, a disc granulator, a kneader.

Preferably, the first mixed material is subjected to reduction smelting by using an oxygen-enriched side-blown furnace. And fuel and combustion-supporting gas are sprayed into a molten pool of the oxygen-enriched side-blown converter through the oxygen-enriched combustion spray gun, and the fuel and the combustion-supporting gas generate combustion reaction to provide required heat for the reduction smelting process. The temperature in the molten pool of the oxygen-enriched side-blown furnace is controlled to be 800-1000 ℃ by controlling the injection speed and/or the injection amount of the fuel and the combustion-supporting gas. The low-temperature reduction smelting process can effectively reduce energy consumption and reduce the unorganized emission of volatile elements so as to further reduce the smoke yield. Further preferably, the reduction smelting can also be carried out at the temperature of 900-1000 ℃, so that the unorganized emission of volatile elements can be further reduced, and the smoke yield can be further reduced.

Optionally, the fuel adopted by the oxygen-enriched side-blown furnace is natural gas or pulverized coal, and the combustion-supporting gas is oxygen-enriched air. Natural gas and pulverized coal are relatively readily available fuels in smelters. Oxygen-enriched air is used as combustion-supporting gas, so that the smoke yield can be reduced, the combustion efficiency of fuel can be improved, and energy conservation and emission reduction are realized.

Preferably, the oxygen-enriched side-blown converter adopts natural gas as fuel, and the blowing amount of the natural gas is 100-200Nm³The blowing amount of the oxygen-enriched air is 300-³H is used as the reference value. Optionally, the oxygen-enriched air has an oxygen concentration of 25% to 99%, where the oxygen concentration is a volume percentage, i.e. the ratio of the volume of oxygen in the oxygen-enriched air to the volume of the oxygen-enriched air is 25% to 99%.

After the first mixed material enters the side-blowing furnace, the first mixed material is rapidly dispersed in the melt along with the stirring of the melt, the first mixed material and the surrounding melt are subjected to rapid heat transfer, anode mud in the first mixed material is heated, and then processes such as melting, decomposition, reduction and the like are carried out. In the process, elements such as lead, antimony and the like which are easy to oxidize in the anode mud and oxygen are subjected to oxidation slagging reaction to generate primary slag. The primary slag floats in the molten pool to form a primary slag layer, which mainly comprises compounds rich in lead and antimony and is also mixed with a small amount of precious metals such as gold, silver and the like.

Meanwhile, a reducing atmosphere is formed in a molten pool of the side-blown converter due to the addition of a reducing agent, and volatile elements such as arsenic and antimony in the anode mud volatilize and enter smoke dust to form primary soot. The primary soot is cooled by the cooling flue and collected by a soot collector, so that substances such as antimony, arsenic and the like enriched in the primary soot can be recovered.

The monomer gold and the monomer silver in the anode slime and the reduced silver, lead, antimony and bismuth form primary noble lead, namely the primary noble lead comprises the monomer gold and the monomer silver in the anode slime and the reduced metals such as the silver, the lead, the antimony and the bismuth. That is, the primary noble lead is an alloy rich in metals such as lead, antimony, bismuth, gold, silver, and the like. The primary noble lead continuously sinks in the molten pool, and a primary noble lead layer is formed at the bottom of the molten pool.

And (3) optionally, periodically discharging the primary slag and the primary precious lead out of the side-blown converter from a metal port and a slag port of the side-blown converter respectively, wherein the discharge period of the primary precious lead and the primary slag is 2-5 hours.

The technical scheme of the application is further explained by taking antimony as an example. As described above, the primary slag, the primary soot, and the primary noble lead contain antimony, and therefore, antimony in the anode slime is not entirely oxidized or entirely reduced, but a part of antimony is oxidized, a part of antimony is reduced, a part of reduced antimony enters the primary soot, and the rest of reduced antimony enters the primary noble lead.

And discharging the primary noble lead from the side blowing furnace, and feeding the primary noble lead into an antimony white furnace for primary refining. As an example, air is blown by an air duct to blow air into an antimony white furnace, and the primary precious lead is blown and oxidized. In the process, most of arsenic and antimony in the primary precious lead volatilize to form secondary soot rich in arsenic and antimony. The secondary soot may be referred to as antimony white. The secondary soot can be further recycled to recover substances such as arsenic, antimony and the like. The primary noble lead is subjected to arsenic and antimony removal to form secondary noble lead. Because of the primary refining, the content of noble metals such as gold, silver and the like in the secondary noble lead is higher than that in the primary noble lead.

The antimony white furnace is adopted to refine the primary precious lead for one time, so that the refining burden of the silver separating furnace can be effectively reduced, and the operation efficiency of the silver separating furnace is improved. Meanwhile, a large amount of volatile elements such as arsenic, antimony and the like in the primary noble lead can be separated and enriched in secondary soot, so that the secondary soot is convenient to further recycle. The antimony white furnace can be selected from a converter, an electric furnace, a refining pot or a reverberatory furnace. Because the available types of the antimony white furnace are more, the adaptive furnace type can be selected according to the actual situation, and the investment cost and the operation cost can be effectively reduced.

Optionally, the working period of discharging secondary noble lead from the antimony white furnace is 10-12 hours. The furnace temperature of the antimony white furnace is 700-900 ℃,namely, the blow oxidation is performed at 700 to 900 ℃, whereby the blow oxidation is low-temperature blow oxidation. The blowing amount of air in the antimony white furnace was 50Nm³/h-150Nm³/h。

Further, in some embodiments, the primary slag and the reducing agent are mixed in a predetermined weight ratio to obtain a second mixed material. And feeding the second mixed material into a depletion furnace to carry out slag depletion treatment on the primary slag. The primary slag mainly comprises lead and antimony and contains a small amount of precious metals such as gold and silver. And (3) performing heat preservation and sedimentation in a dilution furnace in the primary slag, wherein low-grade noble lead or secondary noble lead is formed by the gold and silver with low content and the reduced metal elements such as silver, lead, antimony, bismuth and the like in the primary slag, and the low-grade noble lead is sedimentated. That is, the low-grade precious lead or the next precious lead includes gold and silver contained in the primary slag and metal elements such as silver, lead, antimony and bismuth which are reduced.

During the slag depletion treatment of the primary slag, volatile elements in the primary slag are reduced to form a small amount of depleted soot, and the remaining primary slag forms secondary slag. The secondary slag can be precipitated to recover the residual valuable metals such as lead, antimony and the like, or returned to a lead smelting plant for treatment.

Alternatively, the slag depletion is carried out at a temperature of 1000 ℃ to 1200 ℃. Alternatively, the reducing agent may be crushed coal or coke. When the crushed coal is used as the reducing agent, the weight of the crushed coal is 1-5% of the weight of the primary slag. The deslagging operation period of the impoverishment furnace is 5-6 hours.

The primary slag is subjected to slag depletion treatment, so that the precious metals in the primary slag can be further recovered, and the direct recovery rate of the precious metals is improved. The impoverishment furnace may be one of a converter, an impoverishment furnace and a reverberatory furnace. Because the selection types of the depletion furnace are more, the corresponding furnace type can be selected according to the actual situation, and the investment cost and the operation cost can be effectively reduced.

Further optionally, the secondary precious lead and the low-grade precious lead are mixed, and the mixture of the secondary precious lead and the low-grade precious lead is subjected to secondary refining together. Or mixing the primary noble lead and the low-grade noble lead, and carrying out primary refining on the mixture of the primary noble lead and the low-grade noble lead.

And (3) carrying out secondary refining on the secondary precious lead (or the mixture of the secondary precious lead and the low-grade precious lead) by adopting a silver separating furnace. Preferably, the silver separating furnace adopts an oxygen-enriched combustion burner, so that the automation degree is high, the temperature rising speed is high, the combustion efficiency is high, the smoke emission is low, and the energy conservation and emission reduction are realized. The oxygen-enriched combustion burner can more accurately control the furnace temperature of the silver separating furnace. Optionally, the fuel used by the silver separating furnace is one of natural gas and diesel oil.

Optionally, the furnace temperature in the silver separating furnace is 1000-1200 ℃. The reaction period of the secondary refining is 15-25 hours. Oxygen-enriched gas is blown into the silver-separating furnace as oxidant, and the blowing amount of the oxygen-enriched gas is 50Nm³/h-150Nm³H is used as the reference value. Optionally, the oxygen-enriched air has an oxygen concentration of 25% to 99%, where the oxygen concentration is volume percent.

And (3) enriching the monomer gold and the monomer silver in the secondary noble lead to form a gold-silver alloy, casting the gold-silver alloy into an anode plate, and carrying out silver electrolytic refining. Antimony in the secondary precious lead is volatilized to form tertiary soot, and elements such as copper, bismuth and the like in the secondary precious lead can be oxidized in the silver separating furnace to form refining slag. The silver separating furnace has mature technology for refining the precious lead, skilled operation and easy control of product quality.

The following examples are used to describe the anode slime treatment method provided by the present invention:

the first embodiment is as follows:

lead anode slime (containing 20% of Pb, 18% of Sb, 5% of Bi, 10% of Ag and 10% of As, wherein the percentages (%) refer to mass percent) and crushed coal are mixed according to a ratio of 100: 5 to obtain a first mixed material, and simultaneously adding a returned material, wherein the returned material is the third-time ash discharged from the silver separating furnace. And then conveying the first mixed material to a cylindrical granulator through a belt for granulation, wherein the cylindrical granulator makes the first mixed material into granules, and the water content of the materials is controlled not to exceed 35%.

And (3) feeding the granulated first mixed material into the oxygen-enriched side-blown furnace through a feeding port continuously before feeding the granulated first mixed material into the oxygen-enriched side-blown furnace. The oxygen-enriched side-blown converter adopts natural gas as fuel and oxygen-enriched air as combustion-supporting gas, wherein the concentration of oxygen in the oxygen-enriched air is 70%. Spraying natural gas and oxygen-enriched air into the molten bath through a spray gun, and maintaining the temperature in the oxygen-enriched side-blown furnace at 900 ℃.

The anode mud is subjected to reduction smelting in a molten pool to generate primary soot, primary precious lead and primary slag. The composition of the first lead consists of 30% of Pb, 10% of Sb, 35% of Bi, 25% of Ag and 1.2% of As. The primary slag mainly comprises lead and antimony compounds, and is doped with a small amount of noble metal elements. The primary soot mainly comprises arsenic and antimony.

The period of discharging the primary noble lead and the primary slag of the oxygen-enriched side-blown converter is 3 hours. That is, every 3 hours, it is necessary to discharge primary noble lead from the metal tap and primary slag from the slag tap. And feeding the discharged primary noble lead into an antimony white furnace for primary refining, and feeding the discharged primary slag into a depletion furnace for slag depletion. The furnaces and kilns are directly connected by adopting chutes.

The primary soot and crushed coal are mixed according to the mass ratio of 100:3 and are fed into a depletion furnace. In this embodiment, the temperature of the reverberatory furnace is kept at 1000-. The primary slag is subjected to heat preservation and sedimentation in a dilution furnace to form secondary slag, dilution soot and low-grade noble lead, and the slag operation period of the dilution furnace is 6 hours. The secondary slag can be sent to recover valuable metals such as lead, antimony and the like. Mixing low-grade noble lead and primary noble lead for primary refining.

In the embodiment, a converter is selected as an antimony white furnace, 4 air ducts are used for blowing air into the converter, primary precious lead and low-grade precious lead are oxidized, and the furnace temperature is kept at 800 ℃. The one-time operation period of the antimony white furnace is 12 hours. The primary noble lead and the low-grade noble lead form secondary noble lead and secondary ash rich in arsenic and antimony after arsenic and antimony are removed. The secondary soot can be sent to recover arsenic, antimony and other substances. And (4) feeding the secondary precious lead into a silver separating furnace for secondary refining.

In the process of secondary refining in the silver separating furnace, air oxidation refining is carried out on the secondary precious lead in the early stage, and bismuth in the secondary precious lead is oxidized to form bismuth slag. And in the later stage, oxygen-enriched air oxidation refining is carried out on the secondary noble lead, and the copper in the secondary noble lead is oxidized so as to form copper slag. And (3) enriching the monomer gold and the monomer silver in the secondary noble lead to form a gold-silver alloy, casting the finally generated gold-silver alloy into an anode plate (the content of gold and silver is more than 98 percent), and carrying out silver electrolytic refining. Antimony in the secondary precious lead is volatilized to form tertiary soot. And mixing the tertiary soot discharged from the silver separating furnace as a return material with the lead anode slime, and entering the next anode slime treatment process.

Example two:

the same as the first example, except that the anode slime was decoppered copper anode slime, and the anode slime had Pb 15%, Sb 3%, Bi 2%, Ag 10%, and Cu 1%.

Example three:

the difference from the first embodiment is that the oxygen-enriched side-blown converter uses pulverized coal as fuel.

Example four:

the difference from the first embodiment is that the impoverishment furnace is a impoverishment furnace.

Example five:

the difference from the first embodiment is that the antimony white furnace is a reverberatory furnace, 20 air ducts are used for blowing air into the reverberatory furnace, the furnace temperature is maintained at 800 ℃, and burners are used for supplementing heat to the reverberatory furnace when necessary.

In the description of the present invention, it is to be understood that the terms "central," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," "circumferential," and the like are used in the orientations and positional relationships indicated in the drawings for convenience in describing the invention and to simplify the description, and are not intended to indicate or imply that the referenced devices or elements must have a particular orientation, be constructed and operated in a particular orientation, and are therefore not to be considered limiting of the invention.

Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In the description of the present invention, "a plurality" means at least two, e.g., two, three, etc., unless specifically limited otherwise.

In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "connected," "secured," and the like are to be construed broadly and can, for example, be fixedly connected, detachably connected, or integrally formed; may be mechanically coupled, may be electrically coupled or may be in communication with each other; they may be directly connected or indirectly connected through intervening media, or they may be connected internally or in any other suitable relationship, unless expressly stated otherwise. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.

In the present invention, unless otherwise expressly stated or limited, the first feature "on" or "under" the second feature may be directly contacting the first and second features or indirectly contacting the first and second features through an intermediate. Also, a first feature "on," "over," and "above" a second feature may be directly or diagonally above the second feature, or may simply indicate that the first feature is at a higher level than the second feature. A first feature being "under," "below," and "beneath" a second feature may be directly under or obliquely under the first feature, or may simply mean that the first feature is at a lesser elevation than the second feature.

In the present disclosure, the terms "one embodiment," "some embodiments," "an example," "a specific example," or "some examples" and the like mean that a specific feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present disclosure. In this specification, the schematic representations of the terms used above are not necessarily intended to refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, various embodiments or examples and features of different embodiments or examples described in this specification can be combined and combined by one skilled in the art without contradiction.

Although embodiments of the present invention have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention, and that variations, modifications, substitutions and alterations can be made to the above embodiments by those of ordinary skill in the art within the scope of the present invention.