Method for cooperatively treating lead-copper anode slime mixture through precious lead furnace and top-blown furnace

Abstract

The invention discloses a method for cooperatively treating a lead-copper anode slime mixture through a noble lead furnace and a top-blown furnace, which comprises the following steps: mixing copper-lead anode slime according to a certain proportion, conveying the copper-lead anode slime into the noble lead furnace for melting, dividing the copper-lead anode slime into a reducing slag layer and a noble lead layer in a reducing atmosphere in the furnace, conveying the slag material into a slag converter through a chute, precious lead is conveyed into the top-blowing silver separating furnace through a chute to be oxidized and refined, and reducing slag is subjected to slag material secondary sedimentation in the slag converter. Later-stage slag, tellurium slag, alloy cleaning slag and crude silver are produced through deep oxidation refining, the later-stage slag returns to a bismuth system for treatment, the tellurium slag returns to a tellurium system for treatment, the alloy cleaning slag returns to a refining furnace for treatment, and the crude silver returns to gold, silver, platinum and palladium for treatment. The bottom blowing smelting furnace, the antimony production system and the bismuth production system are organically combined for cooperative treatment, liquid lead slag material chute stepped closed conveying is achieved in the production process, the production period can be shortened, the metal amount occupation pressure is reduced, the gold and silver direct recovery rate is increased, the working environment is improved, the labor intensity is reduced, and the production cost is reduced.

Description

Technical Field

[0001] The present invention relates to the technical field of chemical material recovery and treatment, and particularly to a method for treating a mixture of lead-copper anode slime. Background Art

[0002] In the precious metal smelting industry, there are many valuable metals in lead-copper anode slime, and the grades of valuable metals vary. The main metal elements in lead anode slime are gold, silver, antimony, bismuth, copper, lead, tellurium, etc., and the metal elements in copper anode slime are gold, silver, lead, bismuth, copper, selenium, tellurium, etc. There are mainly three categories of methods for treating lead-copper anode slime mixture in China: one is pyrometallurgical treatment, the second is hydrometallurgical treatment, and the third is pyrometallurgical-hydrometallurgical combined treatment process. Among these three treatment methods, pyrometallurgical treatment has the advantages of strong raw material adaptability and large processing capacity, while the all-wet treatment has problems such as a large amount of tail liquid and high difficulty in treating acidic and alkaline gases. Therefore, most domestic copper anode slimes are treated by sulfation roasting process to remove copper and selenium, and then mixed with lead anode slime for feeding into the pyrometallurgical smelting system. However, the traditional pyrometallurgical smelting system has problems such as low direct recovery rates of gold and silver, many types of intermediate materials, long return material cycle, and poor working environment.

[0003] In the prior art, after copper anode slime is sulfation roasted and sent to the pyrometallurgical system, it is mixed with lead anode slime for feeding into the pyrometallurgical smelting system. The pyrometallurgical smelting system uses a side-blown reduction furnace, and the produced bullion and reduction slag enter the converting furnace and slag converter respectively through a chute. The bullion is processed through the converting furnace and silver parting furnace to produce crude silver. The production cycle of the pyrometallurgical system is 7 days. During the production process, reduction slag, antimony oxide powder, pre-stage slag, post-stage slag, high-silver oxide powder, tellurium slag, and clean alloy slag materials are produced. There are many types of intermediate materials produced, and the return material cycle is long. The pyrometallurgical system has a large amount of metal occupation, a poor on-site working environment, low equipment automation, and high labor intensity of employees; among them, the treatment of copper-containing slag produced by the pyrometallurgical system is difficult, the gold and silver grades of the slag are high, the copper metal cannot be opened, and the copper metal has a high circulation cost during the system production process. Summary of the Invention

[0004] In view of the defects existing in the prior art, the present invention provides a method for co-processing lead-copper anode slime mixture through a bullion furnace and a top-blown furnace, which organically combines and synergistically processes copper-lead anode slime, antimony production system, and bismuth production system. During the production process, the liquid lead slag material is stepwise and tightly conveyed through a chute, which can shorten the pyrometallurgical production cycle, reduce the metal occupation amount, improve the direct recovery rates of gold and silver, improve the on-site working environment, reduce the labor intensity of employees, and reduce the production cost.

[0005] To solve the above technical problems, the present invention adopts the following technical solution: A method for co-processing lead-copper anode slime mixture through a bullion furnace and a top-blown furnace is carried out according to the following steps: Step 1: Pretreat the copper anode slime by removing copper and selenium to obtain copper-removed and selenium-extracted slag. After pretreatment, the copper content in the copper anode slime is less than 1%, and the Se content is less than 1%. Step 2: Charge the copper-removed and selenium-extracted slag obtained in Step 1 and lead anode slime in a mass ratio of 3 - 5:1. After mixing the charge, mix it with coke in a ratio of 10 - 11:14 and feed it into the bullion furnace. Continuously feed the mixed material and auxiliary materials in proportion. Control the furnace temperature with a pure oxygen burner, and blow out the arsenic and antimony components in the smelting material in the form of soot with the bottom oxygen lance; the lead-copper anode slime mixture melts in the bullion furnace. Under the reducing atmosphere in the furnace, it is divided into a reducing slag layer and a bullion layer, which are siphoned out through the slag port and lead port respectively. The reducing slag is transported to the slag converter through a chute, and the bullion is transported to the top-blown parting furnace through a chute. Step 3: Conduct secondary sedimentation of the slag material for the reducing slag produced in Step 2 in the slag converter, and assist with a reducing agent for sedimentation. Step 4: Conduct oxidative refining treatment on the bullion produced in Step 2 in the top-blown parting furnace to obtain a crude alloy of bullion and parting furnace slag; at least two retractable oxygen lance devices are provided at the top of the top-blown parting furnace to adjust and control the oxidative refining process in the furnace; slag discharge ports and lead discharge ports are provided on both sides of the furnace body, and slag discharge and lead discharge operations are carried out through the furnace body rotation system. Step 5: Transport the crude alloy of bullion obtained in Step 4 to the refining furnace, and respectively produce later slag, tellurium slag, clean alloy slag, and crude silver through deep oxidative refining. The later slag is returned to the bismuth system for treatment, the tellurium slag is returned to the tellurium system for treatment, the clean alloy slag is returned to the refining furnace for treatment, and the crude silver is returned to the gold, silver, platinum, and palladium treatment. Step 6: Transport the parting furnace slag obtained in Step 4 to the bismuth converter, and respectively produce bismuth slag and reduced alloy through reduction precipitation. The bismuth slag is returned to the antimony system for treatment, and the lead-bismuth alloy is transported to the tellurium removal pot. After tellurium removal and copper removal, it is returned to the bismuth refining system. Step 7: Classify and process the materials obtained in Step 6. The tellurium slag produced by the tellurium removal pot is returned to the tellurium refining system for treatment, the produced copper slag enters the intermittent vacuum furnace for treatment, and the produced lead-bismuth material enters the continuous vacuum furnace for treatment.

[0006] The main components of the lead anode slime include: gold 300 - 500 g / t, silver 3% - 7%, lead 12% - 18%, bismuth 8% - 15%, copper 0.5% - 1.5%, antimony 20% - 40%, arsenic 15% - 35%, tellurium 0.5% - 1%; the main components of the copper anode slime include: gold 1200 - 3000 g / t, silver 4% - 7%, lead 10% - 15%, bismuth 1% - 2%, copper 15% - 25%, antimony 2% - 4%, arsenic 5% - 10%, tellurium 0.5% - 4%, platinum 5 - 15 g / t, palladium 15 - 55 g / t.

[0007] The lead-copper anode slime mixture is co-treated with a precious lead furnace and a top-blown silver separating furnace, realizing the stepped closed conveying of the liquid lead slag material by a chute, and respectively using the supporting smelting furnaces to treat the intermediate materials, so that the valuable metals are recycled and treated in the corresponding processes.

[0008] In step 2, the smelting temperature of the precious lead furnace is controlled at 900 - 1100 °C, the oxygen-to-material ratio is controlled at 96 Nm³ / t, and the molten pool liquid level is controlled at 1 / 3 - 1 / 2, obtaining preliminary precious lead and preliminary reduced slag; the main components of the precious lead include 2000 - 3000 g / t of gold, 10% - 20% of silver, 15 - 25% of lead, 20 - 25% of bismuth, 3 - 5% of copper, 15 - 20% of antimony, 10 - 20% of arsenic, and 1.5 - 2.5% of tellurium; the main components of the preliminary reduced slag include 20 - 40 g / t of gold, 2000 - 3000 g / t of silver, 20 - 25% of lead, 2 - 5% of bismuth, 0.5 - 0.8% of copper, 14 - 18% of antimony, 10 - 15% of arsenic, and 0.2 - 0.4% of tellurium.

[0009] In step 4, the smelting temperature of the top-blown silver separating furnace is controlled at 800 - 1000 °C, obtaining secondary precious lead and later slag; the main components of the secondary precious lead include 2800 - 3500 g / t of gold, 40% - 50% of silver, 12 - 2% of lead, 20 - 25% of bismuth, 7 - 10% of copper, 5 - 8% of antimony, 3 - 7% of arsenic, and 3 - 5% of tellurium; the main components of the later slag are 30 - 50 g / t of gold, 3000 - 5000 g / t of silver, 30 - 35% of lead, 10 - 14% of bismuth, 2.4 - 3.5% of copper, 5 - 10% of antimony, 14 - 16% of arsenic, and 1 - 1.5% of tellurium.

[0010] Among them, the angles of the pure oxygen burners in the precious lead furnace and the top-blown silver separating furnace are 18 - 20 degrees respectively, the oxygen lances at the bottom of the precious lead furnace and the top of the top-blown silver separating furnace are vertically placed, and the rotation angles of the furnace bodies of the precious lead furnace and the top-blown silver separating furnace are 0 - 90 degrees respectively.

[0011] In step 2, the arsenic and antimony components in the smelting materials are blown out in the form of soot by the bottom oxygen lance and collected through bag dust collection in the dust collection system. The arsenic and antimony soot is returned to the antimony system to recover antimony metal after dearsenification.

[0012] In step 2, a bottom lead outlet is provided in the precious lead furnace, and the bottom precious lead is discharged according to the production cycle to reduce the metal occupation in the bottom blowing furnace.

[0013] In step 3, the upper-layer reduced slag after sedimentation is poured into a slag bag, and the slag bag is transported to the raw material bin by an electric flat car to be prepared as raw materials for the antimony system.

[0014] The method of the present invention has the following advantages compared with the prior art: 1. The lead bullion furnace - top - blown furnace system is adopted to treat the mixed lead - copper anode slime, which has a strong ability to process mixed materials and can meet the needs of large - scale production. It has strong raw material adaptability and can process most complex lead - copper anode slime materials. It is equipped with antimony, bismuth, tellurium, gold, silver, platinum, palladium, and arsenic - removal systems, and additional environmental protection facilities for tail gas treatment are added. It can achieve synchronous and collaborative smelting of all - system materials and improve the operation efficiency of the precious metal system materials.

[0015] The combustion system of the smelting furnace is adjusted from the traditional oxygen lance heating and burner to a pure - oxygen burner, which has the functions of automatic furnace temperature control and automatic adjustment, makes full use of fuel energy, and reduces energy consumption.

[0016] At least two oxygen lances are arranged at the top of the top - blown silver - separating furnace, which increases the contact area with the molten bath during the blowing process. The top - blown method can improve the blowing oxidation effect. A retractable oxygen lance is adopted, enabling the on - site operators to flexibly adjust the insertion depth of the oxygen lance in a timely manner according to the thickness of the molten bath in the furnace and the blowing situation, so as to improve the blowing efficiency. Compared with the traditional bottom - blown furnace, it will further reduce the metal occupation in the furnace. When slagging and lead - discharging operations are carried out, the bottom metal molten bath can be completely discharged, and there is no obvious metal occupation in the furnace. The direct - recovery rates of gold and silver in the precious metal system are increased to 99% and 98.8% respectively, which are 0.5% and 0.03% higher than the original system. The production cycle is reduced from 7 days to 3 days compared with the original system, significantly reducing the metal occupation in the pyrometallurgical system.

[0017] The angles of the pure - oxygen burners of the lead bullion furnace and the top - blown silver - separating furnace are 18 - 20 degrees. The oxygen lances at the bottom of the lead bullion furnace and the top of the top - blown silver - separating furnace are vertically placed, and the rotation angles of the furnace bodies of the lead bullion furnace and the top - blown silver - separating furnace are set to 0 - 90 degrees. It can achieve a good stepped layout. During the production process, the liquid lead - slag materials are transported in a stepped and sealed manner through a chute, changing the original system of manual hoisting and transferring materials, significantly improving the on - site operation environment and reducing the labor intensity.

[0018] The unified recovery of the rare - dispersed metal tellurium in the copper - lead anode slime is realized. The tellurium content in the lead anode slime is relatively low, about 0.4% grade, while the tellurium content in the copper anode slime is as high as 1%. In the traditional industry, the copper anode slime is treated separately by wet method to recover tellurium, resulting in a large amount of waste water. In the present invention, after the anode slime is de - seleniumized, the copper - lead anode slime is mixed and ore - blended, and then intensively blown with pure oxygen. During the process of making tellurium slag, by controlling the oxidation degree of copper, silver, and tellurium, the enrichment of tellurium is realized. The grade of the enriched tellurium slag can reach 14 - 20%, and the problem of waste - water treatment is avoided. Brief Description of the Drawings

[0019] Figure 1 It is the process flow chart of the present invention; Figure 2 It is the schematic diagram of the process layout of the present invention.

[0020] In the figure, 1 is the lead bullion furnace, 2 is the top - blown silver - separating furnace (which can be simply referred to as the top - blown furnace), 3 is the refining furnace, 4 is the bismuth converter, and 5 is the slag converter. Detailed implementation mode

[0021] The following will further illustrate the present invention with reference to the attached Figure 1-2 The present invention will be further described through specific embodiments: Embodiment 1 Raw materials: Composition of copper anode slime: gold 1425 g / t, silver 4.68%, lead 8%, bismuth 1.36%, copper 19.5%, antimony 2.4%, arsenic 7%, tellurium 0.7%, platinum 8 g / t, palladium 32.8 g / t; Composition of lead anode slime: gold 395.48 g / t, silver 3.87%, lead 18%, bismuth 10%, copper 1.2%, antimony 32.4%, arsenic 28.44%, tellurium 0.84%. The input amount of the mixed material is: 4 t / h. Taking a 7-day production cycle as an example, the specific steps are as follows: Step 1: Pretreat the copper anode slime by copper removal and selenium removal to obtain copper-removed and selenium-enriched slag. After pretreatment, the copper content in the copper anode slime is <1%, and the Se content is <0.1%.

[0022] Step 2: Mix the copper-removed and selenium-enriched slag obtained in Step 1 with the lead anode slime according to a ratio of 4:1. After mixing, mix the mixture with coke particles according to a ratio of 11:1 and feed it into the precious lead furnace 1. The mixed material and the auxiliary materials are continuously fed in proportion. Control the furnace temperature with a pure oxygen burner, and blow out the arsenic and antimony components in the smelting material in the form of soot through the bottom oxygen lance. Collect it through the bag filter of the dust collection system. After dearsenification, the arsenic and antimony soot is returned to the antimony system to recover antimony metal. The lead-copper anode slime mixture is melted in the precious lead furnace 1. Under the reducing atmosphere in the furnace, it is divided into a reducing slag layer and a precious lead layer, which are respectively discharged by siphoning through the slag port and the lead port. The slag material is transported to the slag converter 5 through a chute, and the precious lead is transported to the top-blown silver separating furnace 2 through a chute; The precious lead furnace 1 is provided with a bottom lead port, and the bottom precious lead is discharged according to the production cycle to reduce the occupation of metal in the bottom-blown furnace.

[0023] The lead-copper anode slime mixed material is cooperatively processed by the precious lead furnace 1 and the top-blown silver separating furnace 2 to realize the stepped closed transportation of the liquid lead slag material through the chute. The intermediate materials are respectively processed by the supporting smelting furnaces, so that the valuable metals are recycled and processed in the corresponding processes.

[0024] Step 3: Perform secondary sedimentation of the slag material on the reducing slag produced in Step 2 in the slag converter. After sedimentation assisted by a reducing agent, the upper reducing slag is poured into a slag ladle, and the slag ladle is transported to the raw material bin by an electric flat car for preparing raw materials for the antimony system.

[0025] Step 4: Perform oxidative refining treatment on the precious lead produced in Step 2 in the top-blown silver separating furnace 2 to obtain the crude alloy of the precious lead and the silver separating furnace slag; The precious lead is transported to the top-blown silver separating furnace 2 through the flue gas port. There are two telescopic oxygen lance devices at the top of the top-blown silver separating furnace 2, which are used as adjustable devices to control the oxidative refining process in the furnace. There are slag discharge ports and lead discharge ports on both sides of the furnace body, and slag discharge and lead discharge operations are carried out through the furnace body rotation system.

[0026] Step 5: Convey the crude alloy of the lead bullion obtained in Step 4 to the refining furnace 3, and through deep oxidation refining, produce post slag, tellurium slag, clean alloy slag, and crude silver respectively. The bismuth slag is returned to the bismuth system for treatment, the tellurium slag is returned to the tellurium system for treatment, the clean alloy slag is returned to the refining furnace for treatment, and the crude silver is returned to the gold, silver, platinum, and palladium treatment.

[0027] Step 6: Convey the cupellation slag obtained in Step 4 to the bismuth converter 4, and through reduction precipitation, produce bismuth slag and reduced alloy respectively. The bismuth slag is returned to the antimony system for treatment, and the reduced alloy is conveyed to the tellurium removal pot. After tellurium removal and copper removal, it is returned to the bismuth refining system.

[0028] Step 7: Classify and process the materials obtained in Step 6. The tellurium slag produced by the tellurium removal pot is returned to the tellurium refining system for treatment. The produced copper slag enters the intermittent vacuum furnace for treatment, and the produced lead-bismuth material enters the continuous vacuum furnace for treatment.

[0029] In Step 2, the smelting temperature of the lead bullion furnace 1 is controlled at about 950 °C (between 900 - 1100 °C), the oxygen-to-material ratio is controlled at 96 Nm³ / t, and the molten bath liquid level is controlled at 1 / 3 - 1 / 2 to obtain preliminary lead bullion and preliminary reduction slag. The main components of the preliminary lead bullion are 2475.14 g / t of gold, 142217.45 of silver, 14.58% of lead, 21.47% of bismuth, 3.9% of copper, 17.74% of antimony, 15.95% of arsenic, and 1.8% of tellurium; the main components of the preliminary reduction slag are 21.5 g / t of gold, 2364.85 g / t of silver, 24.2% of lead, 3.45% of bismuth, 0.35% of copper, 16.54% of antimony, 12.48% of arsenic, and 0.22% of tellurium.

[0030] In Step 4, the smelting temperature of the top-blown cupellation furnace 2 is controlled at about 850 °C to obtain secondary lead bullion and post slag. The main components of the secondary lead bullion are 3085.54 g / t of gold, 42.85 of silver, 14.56% of lead, 24.57% of bismuth, 7.6% of copper, 5.84% of antimony, 4.1% of arsenic, and 3.86% of tellurium; the main components of the post slag are 32.6 g / t of gold, 3650 g / t of silver, 35.6% of lead, 12.6% of bismuth, 2.4% of copper, 6.3 of antimony, 12.6% of arsenic, and 1.2% of tellurium.

[0031] In Steps 2 and 4, the pure oxygen burner angles of the lead bullion furnace 1 and the top-blown cupellation furnace 2 are 20 degrees. The oxygen lances at the bottom of the lead bullion furnace 1 and the top of the top-blown cupellation furnace 2 are vertically placed, and the furnace body rotation angles of the lead bullion furnace 1 and the top-blown cupellation furnace 2 are 0 - 90°.

[0032] Results: Taking a 7-day production cycle as an example, 3611.45 kg of crude silver was produced. The main components of crude silver were 14691.54 g / t gold, 97.85% silver, 0.14% bismuth, 0.44% copper, 0.024% tellurium, 40.14 g / t platinum, and 148.55 g / t palladium. The calculated crude silver direct recovery rate was 91.21%, the gold recovery rate was 99.47%, and the silver recovery rate was 99.24%.

[0033] Example 2 Raw materials: The main components of lead anode mud are: gold 480g / t, silver 6.8%, lead 16.8%, bismuth 12.5%, copper 1.2%, antimony 36.5%, arsenic 33.2%, and tellurium 0.8%; the main components of copper anode mud are: gold 2860g / t, silver 6.6%, lead 14.6%, bismuth 1.2%, copper 22.1%, antimony 3.4%, arsenic 8.9%, tellurium 0.67%, platinum 14.23g / t, and palladium 54.62g / t. The mixed material input rate is: 4t / h. Taking a 7-day production cycle as an example, the specific steps are as follows: Step 1: Pre-treat the copper anode mud to remove copper and selenium to obtain copper-removed and selenium-extracted slag. After pre-treatment, the copper anode mud contains less than 1% copper and less than 0.1% selenium.

[0034] Step 2: The copper-removal and selenium-extraction slag obtained in Step 1 is mixed with lead anode slime in a ratio of 3:1 (a 5:1 ratio is also acceptable). After mixing, the mixture is mixed with coke pellets in a 10:1 ratio and introduced into the precious lead furnace 1. The mixture and auxiliary materials are continuously fed in proportion. A pure oxygen burner controls the furnace temperature. A bottom oxygen lance removes arsenic and antimony components from the smelting material as fly ash. This fly ash is then collected through a bag filter system. After arsenic removal, the arsenic and antimony fly ash is returned to the antimony system for antimony metal recovery. The lead-copper anode slime mixture is melted in the precious lead furnace 1. Under the reducing atmosphere, it separates into a reducing slag layer and a precious lead layer. These layers are siphoned off through the slag and lead ports, respectively. The slag is conveyed via a chute to the slag converter 5, while the precious lead is conveyed via a chute to the top-blown silver separation furnace 2. The precious lead furnace 1 is equipped with a bottom lead port to release the precious lead according to the production cycle, reducing metal pressure in the bottom-blown furnace.

[0035] The lead-copper anode mud mixture is processed in coordination with the precious lead furnace 1 and the top-blown silver separation furnace 2 to achieve stepped and closed transportation of the liquid lead slag material chute. The intermediate materials are processed in matching smelting furnaces respectively, so that the valuable metals are recycled and processed in the corresponding process.

[0036] Step 3: The reduced slag produced in step 2 is subjected to secondary sedimentation in the slag converter. After sedimentation with the aid of reducing agent, the upper reduced slag is poured into the slag bag, which is transported to the raw material bin via an electric flat car as raw material preparation for the antimony system.

[0037] Step 4: The lead bullion produced in Step 2 is subjected to oxidative refining in the top-blown silver separating furnace 2 to obtain the crude alloy of lead bullion and silver separating furnace slag; the lead bullion is conveyed into the top-blown silver separating furnace 2 through the flue gas outlet. There are two telescopic oxygen lance devices at the top of the top-blown silver separating furnace 2, which are used as adjustable devices to control the oxidative refining process in the furnace. There are slag discharge ports and lead discharge ports on both sides of the furnace body, and slag discharge and lead discharge operations are carried out through the furnace body rotation system.

[0038] Step 5: The lead bullion obtained in Step 4 is conveyed into the refining furnace 3, and through deep oxidative refining, late slag, tellurium slag, clean alloy slag, and crude silver are respectively produced. The late slag is returned to the bismuth system for treatment, the tellurium slag is returned to the tellurium system for treatment, the clean alloy slag is returned to the refining furnace for treatment, and the crude silver is returned to the gold, silver, platinum, and palladium treatment.

[0039] Step 6: The silver separating furnace slag obtained in Step 4 is conveyed into the bismuth converter 4, and through reduction precipitation, bismuth slag and reduced alloy are respectively produced. The bismuth slag is returned to the antimony system for treatment, and the reduced alloy is conveyed to the tellurium removal pot. After tellurium removal and copper removal, it is returned to the bismuth refining system.

[0040] Step 7: The materials obtained in Step 6 are classified for treatment. The tellurium slag produced by the tellurium removal pot is returned to the tellurium refining system for treatment, the copper slag produced enters the intermittent vacuum furnace for treatment, and the lead-bismuth materials produced enter the continuous vacuum furnace for treatment.

[0041] In Step 2, the smelting temperature of the lead bullion furnace 1 is controlled at about 1050 °C (between 900 - 1100 °C), the oxygen-to-material ratio is controlled at 96 Nm³ / t, and the molten pool liquid level is controlled at 1 / 2 to obtain preliminary lead bullion and preliminary reduction slag. The main components of the preliminary lead bullion are 2890 g / t of gold, 16.25% of silver, 24.32% of lead, 22.36% of bismuth, 4.65% of copper, 18.23% of antimony, 18.2% of arsenic, and 2.41% of tellurium; the main components of the preliminary reduction slag are 38.9 g / t of gold, 2840 g / t of silver, 24.1% of lead, 4.6% of bismuth, 0.78% of copper, 16.3% of antimony, 14.6% of arsenic, and 0.4 of tellurium.

[0042] In Step 4, the smelting temperature of the above-mentioned top-blown silver separating furnace is controlled at 1000 °C to obtain secondary lead bullion and late slag. The main components of the lead bullion are 3490 g / t of gold, 48.6% of silver, 18% of lead, 24.1% of bismuth, 6.8% of copper, 8.9% of antimony, 6.8% of arsenic, and 4.5% of tellurium; the main components of the late slag are 48.52 g / t of gold, 4800 g / t of silver, 35.24% of lead, 12.68% of bismuth, 3.6% of copper, 8.85% of antimony, 15.64% of arsenic, and 1.44% of tellurium.

[0043] In Steps 2 and 4, the pure oxygen burner angles of the lead bullion furnace 1 and the top-blown silver separating furnace 2 are 20 degrees. The oxygen lances at the bottom of the lead bullion furnace 1 and the top of the top-blown silver separating furnace 2 are vertically placed, and the furnace body rotation angles of the lead bullion furnace 1 and the top-blown silver separating furnace 2 are 0 - 90 degrees.

[0044] Results: Taking a 7-day production cycle as an example, 4867.2 kg of crude silver was produced. The main components of the crude silver were 15477.65 g / t of gold, 98.04% silver, 0.13% bismuth, 0.24% copper, 0.018% tellurium, 46.55 g / t of platinum, and 176.08 g / t of palladium. After calculation, the direct recovery rate of crude silver was 91.87%, the gold recovery rate was 99.5%, and the silver recovery rate was 99.19%.

[0045] The present invention has been described in detail above. The above description is only the preferred embodiment of the present invention and cannot limit the scope of the present invention. That is, all equivalent changes and modifications made according to the scope of this application should still fall within the scope covered by the present invention.

Claims

1. A method for co-processing a lead-copper anode mud mixture by a bullion furnace and a top-blown converter, characterized in that: Proceed as follows: Step 1: Pretreat the copper anode slime by removing copper and selenium to obtain copper-removed and selenium-extracted slag. After pretreatment, the copper content in the copper anode slime is less than 1%, and the Se content is less than 1%. Step 2: Charge the copper-removed and selenium-extracted slag obtained in Step 1 and lead anode slime in a mass ratio of 3-5:

1. After mixing the charge, mix it with coke in a ratio of 10-11:14 and feed it into the bullion furnace. Continuously feed the mixed material and auxiliary materials in proportion. Control the furnace temperature with a pure oxygen burner, and blow out the arsenic and antimony components in the smelting material in the form of soot with a bottom oxygen lance. The lead-copper anode slime mixture is melted in the bullion furnace. Under the reducing atmosphere in the furnace, it is divided into a reducing slag layer and a bullion layer, which are siphoned out through the slag notch and lead notch respectively. The reducing slag is transported to the slag converter through a chute, and the bullion is transported to the top-blown dezincing furnace through a chute. Step 3: Conduct secondary sedimentation of the slag material in the slag converter for the reducing slag produced in Step 2, and assist with a reducing agent for sedimentation. Step 4: Conduct oxidative refining treatment on the bullion produced in Step 2 in the top-blown dezincing furnace to obtain the crude alloy of the bullion and the dezincing furnace slag. At least two retractable oxygen lance devices are provided at the top of the top-blown dezincing furnace to adjust and control the oxidative refining process in the furnace. Slag discharge ports and lead discharge ports are provided on both sides of the furnace body, and slag discharge and lead discharge operations are carried out through the furnace body rotation system. Step 5: Transport the crude alloy of the bullion obtained in Step 4 to the refining furnace, and respectively produce late slag, tellurium slag, clean alloy slag, and crude silver through deep oxidative refining. The late slag is returned to the bismuth system for treatment, the tellurium slag is returned to the tellurium system for treatment, the clean alloy slag is returned to the refining furnace for treatment, and the crude silver is returned to the gold, silver, platinum, and palladium treatment. Step 6: Transport the dezincing furnace slag obtained in Step 4 to the bismuth converter, and respectively produce bismuth slag and reduced alloy through reduction precipitation. The bismuth slag is returned to the antimony system for treatment, and the lead-bismuth alloy is transported to the tellurium removal pot. After tellurium removal and copper removal, it is returned to the bismuth refining system. Step 7: Classify the materials obtained in Step 6 for treatment. The tellurium slag produced by the tellurium removal pot is returned to the tellurium refining system for treatment, the produced copper slag enters the intermittent vacuum furnace for treatment, and the produced lead-bismuth material enters the continuous vacuum furnace for treatment.

2. The method for co-processing lead-copper anode slime mixture by blast furnace and top-blown converter according to claim 1, characterized in that: The main components of the lead anode slime include: 300-500 g / t of gold, 3%-7% of silver, 12%-18% of lead, 8%-15% of bismuth, 0.5%-1.5% of copper, 20%-40% of antimony, 15%-35% of arsenic, 0.5%-1% of tellurium; the main components of the copper anode slime include: 1200-3000 g / t of gold, 4%-7% of silver, 10%-15% of lead, 1%-2% of bismuth, 15%-25% of copper, 2%-4% of antimony, 5%-10% of arsenic, 0.5%-4% of tellurium, 5-15 g / t of platinum, 15-55 g / t of palladium.

3. The method for co-processing lead-copper anode mud mixture by means of a bullion furnace and a top-blown converter according to claim 1, characterized in that: The lead-copper anode slime mixed material is co-treated with a bullion furnace and a top-blown dezincing furnace to achieve stepped and sealed transportation of the liquid lead slag material through a chute. The intermediate materials are respectively treated with supporting smelting furnaces, so that the valuable metals are recycled and treated in the corresponding processes.

4. The method for co-processing lead-copper anode slime mixture by using a reverberatory furnace and a top-blown converter according to claim 1, characterized in that: In Step 2, the smelting temperature of the bullion furnace is controlled at 900 - 1100 °C, the oxygen-to-charge ratio is controlled at 96 Nm³ / t, and the molten bath level is controlled at 1 / 3 - 1 / 2, obtaining preliminary bullion and preliminary reduced slag; the main components of the bullion include 2000 - 3000 g / t of gold, 10% - 20% of silver, 15 - 25% of lead, 20 - 25% of bismuth, 3 - 5% of copper, 15 - 20% of antimony, 10 - 20% of arsenic, and 1.5 - 2.5% of tellurium; the main components of the preliminary reduced slag include 20 - 40 g / t of gold, 2000 - 3000 g / t of silver, 20 - 25% of lead, 2 - 5% of bismuth, 0.5 - 0.8% of copper, 14 - 18% of antimony, 10 - 15% of arsenic, and 0.2 - 0.4% of tellurium.

5. The method for co-processing lead-copper anode mud mixture by using a reverberatory furnace and a top-blown converter according to claim 1, characterized in that: In Step 4, the smelting temperature of the top-blown parting furnace is controlled at 800 - 1000 °C, obtaining secondary bullion and later slag; the main components of the secondary bullion include 2800 - 3500 g / t of gold, 40% - 50% of silver, 12 - 2% of lead, 20 - 25% of bismuth, 7 - 10% of copper, 5 - 8% of antimony, 3 - 7% of arsenic, and 3 - 5% of tellurium; the main components of the later slag are 30 - 50 g / t of gold, 3000 - 5000 g / t of silver, 30 - 35% of lead, 10 - 14% of bismuth, 2.4 - 3.5% of copper, 5 - 10% of antimony, 14 - 16% of arsenic, and 1 - 1.5% of tellurium.

6. The method for co-processing lead-copper anode mud mixture by using a reverberatory furnace and a top-blown converter according to claim 1, characterized in that: The angles of the pure oxygen burners in the bullion furnace and the top-blown parting furnace are 18 - 20 degrees respectively. The oxygen lances at the bottom of the bullion furnace and the top of the top-blown parting furnace are both vertically placed. The rotation angles of the furnace bodies of the bullion furnace and the top-blown parting furnace are 0 - 90 degrees respectively.

7. The method for co-processing lead-copper anode mud mixture by using a reverberatory furnace and a top-blown converter according to claim 1, wherein: In Step 2, the arsenic- and antimony-containing components of the smelting materials are blown out in the form of soot by the bottom oxygen lance and collected through bag dust collection in the dust collection system. The arsenic- and antimony-containing soot is returned to the antimony system for antimony metal recovery after arsenic removal.

8. The new process for jointly preparing cadmium sulfide from lead-zinc smelting slag according to claim 1, characterized in that: In Step 2, a bottom lead outlet is provided in the bullion furnace, and the bottom bullion is discharged according to the production cycle to reduce the metal occupation in the bottom-blown furnace.

9. The new process for jointly preparing cadmium sulfide from lead-zinc smelting slag according to claim 1, characterized in that: In Step 3, the upper-layer reduced slag after sedimentation is poured into a slag bag, and the slag bag is transported to the raw material bin by an electric flat car for preparing raw materials for the antimony system.

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