Waste residue treatment method for recovering pb and zn from residues of zinc hydrometallurgy by means of full wet process

Abstract

The present invention belongs to the technical field of the treatment of metallurgical waste residues. Disclosed is a waste residue treatment method for recovering Pb and Zn from residues of zinc hydrometallurgy by means of a full wet process. The method comprises: adding residues of zinc hydrometallurgy to a sulfuric acid solution for washing to remove residual Zn2+ in the residues of zinc hydrometallurgy, and then performing first-stage solid-liquid separation; supplementing the obtained filtrate with a sulfuric acid solution, then returning same to a washing system so as to be circulated again, extracting Zn2+ by using P2O4 once the content of Zn2+ is greater than 20-25 g / L, supplementing the resulting raffinate with a sulfuric acid solution, then returning same to the washing system, and subjecting an organic phase to reverse extraction and then to purification and electrodeposition, thereby obtaining a zinc ingot; performing complexing on filter residues by using a complexing agent so as to remove Pb, and performing second-stage solid-liquid separation; adding a regenerant to the resulting filtrate, performing regeneration to remove Pb, and then performing third-stage solid-liquid separation; returning the resulting filtrate to the system for Pb removal by means of complexing so as to be circulated again, wherein the resulting filter residue is a PbS precipitate; and adding water to wash the filter residues obtained from the second-stage solid-liquid separation to obtain harmless residues. The residual valuable Pb and Zn in the smelting residues can be recovered to the maximum extent, the purity of the zinc ingot is greater than 99%, and the Pb content of lead-rich residues is greater than 36%; moreover, the energy consumption is substantially reduced, and the method thus has the advantages of energy conservation and environmental protection.

Description

A waste slag treatment method for fully wet recovery of Pb and Zn from wet zinc smelting slag Technical Field

[0001] The invention belongs to the technical field of metallurgical waste slag treatment, and particularly relates to a waste slag treatment method for fully wet-process recovery of Pb and Zn in wet zinc slag. Background Art

[0002] With the rapid development of the zinc smelting industry, conflicts such as resource and environmental issues have become increasingly prominent. High-grade, easily processed zinc sulfide resources are becoming increasingly depleted. The green metallurgy of low-grade oxygen-sulfur mixed / oxidized lead-zinc ores has become an important guarantee for the sustainable and healthy development of the domestic zinc smelting industry. It should be noted that the ore properties of some oxygen-sulfur mixed lead-zinc ores are relatively complex, with high oxidation rates, large mud contents, and characteristics such as lean, fine, and mixed materials. Directly entering the smelting process makes them difficult to utilize and has low recovery rates. In addition, with the exception of some valuable elements such as Pb, Zn, and Fe, the content of other valuable metal elements in such ores is extremely low. The profit margin for enterprises processing such ores is extremely low. If the smelting waste residues of such ores are further treated harmlessly, it is very likely to result in losses for the enterprises. Therefore, many resources have not been rationally and effectively developed and utilized.

[0003] With the country's increasing emphasis on the ecological environment, low-cost, harmless treatment of smelting waste residues is crucial for the effective utilization of these ores. Due to the complex composition and wide grade fluctuations of these low-grade, difficult-to-treat, oxygen-sulfur mixed lead-zinc ores, the leached residues after hydrometallurgy are complex in composition, with large fluctuations in the occurrence and content of harmful heavy metals such as Pb and Zn. Consequently, an economical, technically stable, and low-cost harmless treatment process for these waste residues has yet to be found. Currently, many companies still resort to stockpiling slag in storage, resulting in increasingly complex slag heaps and increasingly serious problems.

[0004] Smelting waste residues are stored in slag yards for long periods of time. Acid rain and other acidic liquids in nature, if soaked in the waste residues for long periods of time, dissolve the heavy metals in them. These heavy metals are then washed away by rainwater into surface rivers, seeping into the surrounding soil and then deep into the groundwater, posing a serious threat to the ecological environment of the surrounding areas. This has become a bottleneck for the sustainable and healthy development of the zinc smelting industry. Therefore, the present invention aims to provide a waste residue treatment method for recovering Pb and Zn from hydrometallurgical zinc slag. This method, through a fully wet process, achieves the recovery of most of the lead and zinc in the smelting slag. The recovered slag, after solidification treatment, meets the standards of general solid waste and can be used as a raw material for cement plants, thus having high application value and economic benefits. Technical Solutions

[0005] The object of the present invention is to provide a waste slag treatment method for fully wet recovery of Pb and Zn in hydrometallurgical zinc slag.

[0006] The object of the present invention is achieved as follows: the waste slag treatment method for recovering Pb and Zn from wet zinc smelting slag by the full wet method comprises pickling, zinc recovery, lead recovery, and waste slag treatment steps, specifically comprising:

[0007] A. Pickling: Add the wet zinc smelting slag into sulfuric acid solution for stirring and washing to remove the residual Zn in the zinc smelting slag. 2+ The liquid-solid ratio of washing is 3~6:1, the sulfuric acid concentration is 10~30g / L, the temperature is 20~80℃, the stirring speed is 300~600r / min, the washing time is 30~180min, and the first stage solid-liquid separation is carried out after washing.

[0008] B. Zinc recovery: The filtrate obtained from the first stage solid-liquid separation is supplemented with sulfuric acid solution and then returned to the stirring washing system for recirculation until the Zn in the washing liquid is 2+ When the content is >20-25g / L, use P204 to extract the Zn 2+ The raffinate is supplemented with sulfuric acid solution and returned to the stirring and washing system. The organic phase is sent to the purification electrolytic system after back extraction to obtain recovered zinc ingots.

[0009] C. Lead Recovery: After the filter residue obtained from the first stage solid-liquid separation is slurried, it is subjected to complexation and lead removal with a complexing agent to remove residual lead in the filter residue. The complexing agent is any one of disodium ethylenediaminetetraacetate (EDTA-Na2), tetrasodium ethylenediaminetetraacetate (EDTA-Na4), dipotassium ethylenediaminetetraacetate (EDTA-K2), and tripotassium ethylenediaminetetraacetate (EDTA-K3), or a combination thereof, with a complexing agent concentration of 50-70 g / L. The liquid-solid ratio for complexation and lead removal is 3-6:1, the pH is 5.2-6.7, the n (EDTA): n (Pb) is 1-4:1, the temperature is 30-60°C, and the reaction time is 2-6 hours. Then, the second stage solid-liquid separation is carried out.

[0010] The filtrate obtained from the second stage solid-liquid separation is added with a regeneration agent to regenerate the complexing agent and remove Pb. The regeneration agent is either Na2S or K2S or a combination of the two. The amount of regeneration agent added is 1 to 3 times the Pb content in the filtrate, the reaction temperature is 20 to 60°C, the reaction time is 1 to 4 hours, and then the third stage solid-liquid separation is carried out.

[0011] The filtrate obtained from the third stage solid-liquid separation is the lead-removing liquid, which is returned to the complexation and Pb removal system for recirculation. The filter residue obtained is PbS precipitation, that is, lead-rich residue.

[0012] D. Waste residue treatment: The filter residue obtained from the second stage solid-liquid separation is washed with water, stirred and filtered out to obtain harmless residue. The liquid-solid ratio of the washing is 2-6:1, the temperature is 20-80℃, the stirring speed is 300-600r / min, and the washing time is 30-180min. Beneficial effects

[0013] Compared with the prior art, the present invention has the following beneficial effects:

[0014] 1. The technical solution of the present invention can realize the full wet harmless treatment of hydrometallurgical zinc slag, which significantly reduces energy consumption compared with the existing pyrometallurgical harmless treatment technology.

[0015] 2. The valuable Pb and Zn metals remaining in the smelting slag can be recovered to the maximum extent. The purity of zinc ingots is greater than 99%, and the Pb content of lead-rich slag is greater than 36%.

[0016] 3. The technical solution of the present invention has a short process flow, the intermediate products of each process can be recycled, the reagent consumption is low, and it has outstanding environmental and economic benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] FIG1 is a flow chart of the technical solution of the present invention. Modes for Carrying Out the Invention

[0018] The present invention is further described below, but is not intended to limit the present invention in any way. Any changes or substitutions made based on the teachings of the present invention fall within the scope of protection of the present invention.

[0019] The waste slag treatment method for fully wet-process recovery of Pb and Zn from wet-process zinc smelting slag includes pickling, zinc recovery, lead recovery, and waste slag treatment steps, specifically including:

[0020] A. Pickling: Add the wet zinc smelting slag into sulfuric acid solution for stirring and washing to remove the residual Zn in the zinc smelting slag. 2+ The liquid-solid ratio of washing is 3~6:1, the sulfuric acid concentration is 10~30g / L, the temperature is 20~80℃, the stirring speed is 300~600r / min, the washing time is 30~180min, and the first stage solid-liquid separation is carried out after washing.

[0021] B. Zinc recovery: The filtrate obtained from the first stage solid-liquid separation is supplemented with sulfuric acid solution and then returned to the stirring washing system for recirculation until the Zn in the washing liquid is 2+ When the content is >20-25g / L, use P204 to extract the Zn 2+ The raffinate is supplemented with sulfuric acid solution and then returned to the stirring and washing system. The organic phase is sent to the purification electrolytic system after back extraction to obtain recovered zinc ingots with a purity of >99%.

[0022] C. Lead Recovery: After the filter residue obtained from the first stage solid-liquid separation is slurried, it is subjected to complexation and lead removal with a complexing agent to remove residual lead in the filter residue. The complexing agent is any one of disodium ethylenediaminetetraacetate (EDTA-Na2), tetrasodium ethylenediaminetetraacetate (EDTA-Na4), dipotassium ethylenediaminetetraacetate (EDTA-K2), and tripotassium ethylenediaminetetraacetate (EDTA-K3), or a combination thereof, with a complexing agent concentration of 50-70 g / L. The liquid-solid ratio for complexation and lead removal is 3-6:1, the pH is 5.2-6.7, the n (EDTA): n (Pb) is 1-4:1, the temperature is 30-60°C, and the reaction time is 2-6 hours. Then, the second stage solid-liquid separation is carried out.

[0023] The filtrate obtained from the second stage solid-liquid separation is added with a regeneration agent to regenerate the complexing agent and remove Pb. The regeneration agent is either Na2S or K2S or a combination of the two. The amount of regeneration agent added is 1 to 3 times the Pb content in the filtrate. The reaction temperature is 20-60°C and the reaction time is 1 to 4 hours. Then the third stage solid-liquid separation is carried out.

[0024] The filtrate obtained from the third stage solid-liquid separation is the lead-removing liquid, which is returned to the complexation and Pb removal system for recirculation. The filter residue obtained is PbS precipitation, that is, lead-rich residue.

[0025] D. Waste residue treatment: The filter residue obtained from the second stage solid-liquid separation is washed with water, stirred and filtered out to obtain harmless residue. The liquid-solid ratio of the washing is 2-6:1, the temperature is 20-80℃, the stirring speed is 300-600r / min, and the washing time is 30-180min.

[0026] In the pickling process, the preferred values ​​of the process parameters are: liquid-to-solid ratio of washing is 4~5:1, sulfuric acid concentration is 15~25g / L, temperature is 40~60℃, stirring speed is 400~500r / min, and washing time is 60~150min.

[0027] In the zinc recovery process, the filtrate obtained from the first stage solid-liquid separation is supplemented with sulfuric acid solution and then returned to the stirring and washing system, and is circulated again for 6 to 10 times.

[0028] In the lead recovery process, the preferred process parameters are: a complexing agent concentration of 55-65 g / L; a liquid-to-solid ratio of 4-5:1 for complexation lead removal; a pH of 5.5-6.5; an n(EDTA):n(Pb) ratio of 2-3:1; a temperature of 40-50°C; and a reaction time of 3-5 hours. The regeneration agent addition amount is twice the Pb content in the filtrate, the reaction temperature is 30-50°C, and the reaction time is 2-3 hours. The lead content of the lead-rich slag is >36%.

[0029] In the waste residue treatment process, the preferred values ​​of the process parameters are: a liquid-to-solid ratio of 3 to 5:1, a temperature of 40 to 60°C, a stirring speed of 400 to 500 rpm, and a washing time of 60 to 150 minutes. The washing water is returned to the waste residue washing system for recirculation.

[0030] Example 1

[0031] A. Pickling: Add 20g / L sulfuric acid solution to the wet zinc smelting slag and stir and wash it to remove the residual Zn in the zinc smelting slag. 2+ The liquid-solid ratio of washing is 4:1, the temperature is 30℃, the stirring speed is 400r / min, the washing time is 60min, and the first stage solid-liquid separation is carried out after washing.

[0032] B. Zinc recovery: The filtrate obtained from the first stage solid-liquid separation is supplemented with sulfuric acid solution and then returned to the stirring washing system for recirculation until the Zn in the washing liquid is 2+ When the content is greater than 20g / L, use P204 to extract the Zn 2+ The raffinate is supplemented with sulfuric acid solution and returned to the stirring and washing system. The organic phase is sent to the purification electrolytic system after back extraction to obtain recovered zinc ingots.

[0033] C. Lead recovery: After the filter residue obtained from the first stage solid-liquid separation is slurried, it is subjected to complexation and lead removal with 50 g / L disodium ethylenediaminetetraacetic acid (EDTA-Na2) to remove the residual lead in the filter residue. The liquid-solid ratio of the complexation and lead removal is 4:1, the pH is 6.1, the temperature is 40°C, and the reaction time is 3 hours. Then, the second stage solid-liquid separation is carried out.

[0034] The regeneration agent Na2S is added to the filtrate obtained from the second stage solid-liquid separation to regenerate the complexing agent and remove Pb. The amount of regeneration agent added is twice the Pb content in the filtrate, the reaction temperature is 30°C, the reaction time is 2h, and then the third stage solid-liquid separation is carried out.

[0035] The filtrate obtained from the third stage solid-liquid separation is the lead-removing liquid, which is returned to the complexation Pb removal system for recirculation. The obtained filter residue is PbS precipitate, that is, lead-rich residue with a Pb content of 38.13%.

[0036] D. Waste Residue Treatment: The residue from the second-stage solid-liquid separation is washed with water, stirred, and filtered to form harmless residue. This residue is then sent for toxicity leaching and identification as Class I general solid waste. The washing process uses a liquid-to-solid ratio of 3:1, a temperature of 40°C, an agitator speed of 400 rpm, and a washing time of 60 minutes. The washing water is returned to the waste residue washing system for recirculation.

[0037] Example 2

[0038] A. Pickling: Add 15g / L sulfuric acid solution to the wet zinc smelting slag and stir and wash it to remove the residual Zn in the zinc smelting slag. 2+The liquid-solid ratio of washing is 5:1, the temperature is 25℃, the stirring speed is 500r / min, the washing time is 150min, and the first stage solid-liquid separation is carried out after washing.

[0039] B. Zinc recovery: The filtrate obtained from the first stage solid-liquid separation is supplemented with sulfuric acid solution and then returned to the stirring washing system for recirculation until the Zn in the washing liquid is 2+ When the content is greater than 25g / L, use P204 to extract the Zn 2+ The raffinate is supplemented with sulfuric acid solution and returned to the stirring and washing system. The organic phase is sent to the purification electrolytic system after back extraction to obtain recovered zinc ingots.

[0040] C. Lead Recovery: After the filter residue obtained from the first stage solid-liquid separation is slurried, it is subjected to complexation and lead removal using a 1:1 mixture of 70 g / L disodium ethylenediaminetetraacetic acid (EDTA-Na2) and 70 g / L tetrasodium ethylenediaminetetraacetic acid (EDTA-Na4) to remove residual lead in the filter residue. The liquid-solid ratio of the complexation and lead removal is 3:1, the pH is 6.5, the temperature is 30°C, and the reaction time is 2.5 h. Then, the second stage solid-liquid separation is carried out.

[0041] The regeneration agent K2S is added to the filtrate obtained from the second stage solid-liquid separation to regenerate the complexing agent and remove Pb. The amount of regeneration agent added is 1 times the Pb content in the filtrate, the reaction temperature is 40°C, the reaction time is 1h, and then the third stage solid-liquid separation is carried out.

[0042] The filtrate obtained from the third stage solid-liquid separation is the lead-removing liquid, which is returned to the complexation Pb removal system for recirculation. The obtained filter residue is PbS precipitate, that is, lead-rich residue with a Pb content of 36.26%.

[0043] D. Waste Residue Treatment: The residue from the second-stage solid-liquid separation is washed with water, stirred, and filtered to form harmless residue. This residue is then sent for toxicity leaching and identification as Class I general solid waste. The washing process uses a liquid-to-solid ratio of 5:1, a temperature of 60°C, an agitator speed of 500 rpm, and a washing time of 150 minutes. The wash water is returned to the waste residue washing system for recirculation.

[0044] Example 3

[0045] A. Pickling: Add 10g / L sulfuric acid solution to the wet zinc smelting slag and stir and wash it to remove the residual Zn in the zinc smelting slag. 2+ The liquid-solid ratio of washing is 3:1, the temperature is 60℃, the stirring speed is 300r / min, the washing time is 180min, and the first stage solid-liquid separation is carried out after washing.

[0046] B. Zinc recovery: The filtrate obtained from the first stage solid-liquid separation is supplemented with sulfuric acid solution and then returned to the stirring washing system for recirculation until the Zn in the washing liquid is 2+ When the content is greater than 20g / L, use P204 to extract the Zn 2+The raffinate is supplemented with sulfuric acid solution and returned to the stirring and washing system. The organic phase is sent to the purification electrolytic system after back extraction to obtain recovered zinc ingots.

[0047] C. Lead Recovery: The filter residue obtained from the first stage solid-liquid separation was slurried and then subjected to complexation with 60 g / L dipotassium ethylenediaminetetraacetic acid (EDTA-K2) to remove the residual Pb in the filter residue. The liquid-solid ratio of the complexation for Pb removal was 6:1, the pH was 5.2, the temperature was 50°C, and the reaction time was 6 h. Then, the second stage solid-liquid separation was carried out.

[0048] The filtrate obtained from the second stage solid-liquid separation was added with a 1:1 compound of Na2S and K2S to regenerate the complexing agent and remove Pb. The amount of compounding agent added was 3 times the Pb content in the filtrate. The reaction temperature was 20°C and the reaction time was 4h. The third stage solid-liquid separation was then carried out.

[0049] The filtrate obtained from the third stage solid-liquid separation is the lead-removing liquid, which is returned to the complexation Pb removal system for recirculation. The resulting filter residue is PbS precipitate, i.e., lead-rich residue with a Pb content of 37.18%.

[0050] D. Waste Residue Treatment: The residue from the second-stage solid-liquid separation is washed with water, stirred, and filtered to form harmless residue. This residue is then sent for toxicity leaching and identification as Class I general solid waste. The washing process uses a liquid-to-solid ratio of 2:1, a temperature of 80°C, an agitator speed of 600 rpm, and a washing time of 30 minutes. The washing water is returned to the waste residue washing system for recirculation.

[0051] Example 4

[0052] A. Pickling: Add 30g / L sulfuric acid solution to the wet zinc smelting slag and stir and wash it to remove the residual Zn in the zinc smelting slag. 2+ The liquid-solid ratio of washing is 6:1, the temperature is 80℃, the stirring speed is 600r / min, the washing time is 30min, and the first stage solid-liquid separation is carried out after washing.

[0053] B. Zinc recovery: The filtrate obtained from the first stage solid-liquid separation is supplemented with sulfuric acid solution and then returned to the stirring washing system for recirculation until the Zn in the washing liquid is 2+ When the content is greater than 20g / L, use P204 to extract the Zn 2+ The raffinate is supplemented with sulfuric acid solution and returned to the stirring and washing system. The organic phase is sent to the purification electrolytic system after back extraction to obtain recovered zinc ingots.

[0054] C. Lead Recovery: The filter residue obtained from the first stage solid-liquid separation was slurried and then subjected to complexation with 55 g / L tripotassium ethylenediaminetetraacetate (EDTA-K3) to remove the residual Pb in the filter residue. The liquid-solid ratio of the complexation for Pb removal was 5:1, the pH was 6.7, the temperature was 60°C, and the reaction time was 4.5 h. Then, the second stage solid-liquid separation was carried out.

[0055] The regeneration agent Na2S is added to the filtrate obtained from the second stage solid-liquid separation to regenerate the complexing agent and remove Pb. The amount of regeneration agent added is 1.5 times the Pb content in the filtrate, the reaction temperature is 60°C, the reaction time is 3h, and then the third stage solid-liquid separation is carried out.

[0056] The filtrate obtained from the third stage solid-liquid separation is the lead-removing liquid, which is returned to the complexation Pb removal system for recirculation. The obtained filter residue is PbS precipitate, that is, lead-rich residue with a Pb content of 36.49%.

[0057] D. Waste Residue Treatment: The residue from the second-stage solid-liquid separation is washed with water, stirred, and filtered to form harmless residue. This residue is then sent to a toxicity leaching facility for identification as Class I general solid waste. The washing process is performed at a liquid-to-solid ratio of 6:1, a temperature of 20°C, an agitator speed of 300 rpm, and a washing time of 180 minutes. The wash water is then returned to the waste residue washing system for recirculation.

Claims

1. A waste residue treatment method for recovering Pb and Zn from zinc hydrometallurgy slag by a fully wet process, characterized in that It includes pickling, zinc recovery, lead recovery, and waste residue treatment processes, specifically including: A. Pickling: Add the zinc hydrometallurgy residue to the sulfuric acid solution for stirring and washing to remove the residual Zn in the zinc hydrometallurgy residue 2+ , the liquid-solid ratio of the washing is 3-6:1, the sulfuric acid concentration is 10-30 g / L, the temperature is 20-80 °C, the stirring speed is 300-600 r / min, the washing time is 30-180 min, and the first-stage solid-liquid separation is carried out after washing; B. Zinc recovery: The filtrate obtained from the first-stage solid-liquid separation is returned to the stirring and washing system for recycling after being supplemented with sulfuric acid solution until the Zn content in the washing liquid is > 20 - 25 g / L. Then, P204 is used to extract Zn from it. 2+ After that, the raffinate is returned to the stirring and washing system after being supplemented with sulfuric acid solution, and the organic phase is sent to the purification and electrowinning system after back-extraction to obtain recycled zinc ingots. 2+ ​ C. Lead recovery: After the filter residue obtained from the first-stage solid-liquid separation is slurried, a complexing agent is used for complexing to remove Pb residues in the filter residue. The complexing agent is any one or a combination of disodium ethylenediaminetetraacetate (EDTA-Na2), tetrasodium ethylenediaminetetraacetate (EDTA-Na4), dipotassium ethylenediaminetetraacetate (EDTA-K2), and tripotassium ethylenediaminetetraacetate (EDTA-K3). The concentration of the complexing agent is 50-70 g / L; the liquid-solid ratio for complexing to remove Pb is 3-6:1, the pH is 5.2-6.7, n(EDTA):n(Pb) is 1-4:1, the temperature is 30-60 °C, and the reaction time is 2-6 h. Then, the second-stage solid-liquid separation is carried out; The filtrate obtained from the second-stage solid-liquid separation is added with a regenerant to regenerate and remove Pb from the complexing agent. The regenerant is any one or a combination of Na2S or K2S; the addition amount of the regenerant is 1-3 times the Pb content in the filtrate, the reaction temperature is 20-60 °C, the reaction time is 1-4 h, and then the third-stage solid-liquid separation is carried out; The filtrate obtained from the third-stage solid-liquid separation is the lead-removing liquid, which is returned to the complexing to remove Pb system for recycling. The obtained filter residue is PbS precipitate, i.e., lead-rich slag; D. Waste residue treatment: The filter residue obtained from the second-stage solid-liquid separation is washed by stirring with water, and then filtered out to obtain harmless slag. The liquid-solid ratio for washing is 2-6:1, the temperature is 20-80 °C, the stirring speed is 300-600 r / min, and the washing time is 30-180 min.

2. The waste residue treatment method according to claim 1, wherein In the pickling process, the liquid-solid ratio for washing is 4-5:1, the sulfuric acid concentration is 15-25 g / L, the temperature is 40-60 °C, the stirring speed is 400-500 r / min, and the washing time is 60-150 min.

3. The waste residue treatment method according to claim 1, characterized in that In the zinc recovery process, the filtrate obtained from the first-stage solid-liquid separation is returned to the stirring and washing system after supplementing sulfuric acid solution, and recycled 6-10 times again.

4. The waste residue treatment method according to claim 1, wherein In the lead recovery process, the concentration of the complexing agent is 55-65 g / L.

5. The waste residue treatment method according to claim 1, wherein In the lead recovery process, the liquid-solid ratio for complexing to remove Pb is 4-5:1, the pH is 5.5-6.5, n(EDTA):n(Pb) is 2-3:1, the temperature is 40-50 °C, and the reaction time is 3-5 h.

6. The waste residue treatment method according to claim 1, characterized in that In the lead recovery process, the addition amount of the regenerant is 2 times the Pb content in the filtrate, the reaction temperature is 30-50 °C, and the reaction time is 2-3 h.

7. The waste residue treatment method according to claim 1, wherein In the lead recovery process, the Pb content in the lead-rich slag > 36%.

8. The waste residue treatment method according to claim 1, wherein In the waste residue treatment process, the liquid-solid ratio for washing is 3-5:1, the temperature is 40-60 °C, the stirring speed is 400-500 r / min, and the washing time is 60-150 min.

9. The waste residue treatment method according to claim 1, wherein In the waste residue treatment process, the washing water is returned to the waste residue washing system for recycling.

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