阅读说明：本技术 一种采用溶剂萃取电积工艺生产金属铅的方法 (Method for producing metallic lead by adopting solvent extraction electrodeposition process ) 是由 蒋航宇 董飘平 刘宇豪 赵尹 于 2020-11-13 设计创作，主要内容包括：本发明公开了一种采用溶剂萃取电积工艺生产金属铅的方法。包括以下步骤：a)将含铅物料球磨后与氯化配位浸出剂进行浸出、液固分离后得到含铅浸出液与浸出渣；b)将含铅浸出液调节pH后与铅萃取剂进行混合萃取得到负载铅离子的有机相以及萃余液,萃余液一部分返回步骤a)循环使用,一部分利用溶液中的SO_4~(2-)、Cl~-制备硫酸钙和氯化钙副产品；c)负载铅离子的有机相通过酸性洗涤液洗杂后得到纯净的铅负载有机相以及洗涤后液；d)纯净的铅负载有机相用酸性反萃剂反萃,得到再生有机相以及铅反萃富液；e)再生有机相返回步骤b)循环使用；f)铅反萃富液通过除油得到铅电积前液；g)铅电积前液通过电积得到金属铅,电积过程中再生的酸性反萃剂返回萃取系统循环使用。(The invention discloses a method for producing metallic lead by adopting a solvent extraction electrodeposition process. The method comprises the following steps: a) ball-milling the lead-containing material, leaching with a chlorinated coordination leaching agent, and carrying out liquid-solid separation to obtain a lead-containing leaching solution and leaching residues; b) adjusting the pH of the lead-containing leachate, mixing the lead-containing leachate with a lead extracting agent for extraction to obtain an organic phase loaded with lead ions and a raffinate, wherein part of the raffinate is returned to the step a) for recycling, and the other part of the raffinate utilizes SO in the solution 4 2‑ 、Cl ‑ Preparing calcium sulfate and calcium chloride byproducts; c) washing impurities in the lead ion-loaded organic phase by using an acidic washing solution to obtain a pure lead-loaded organic phase and a washing solution; d) acidity for pure lead-loaded organic phaseBack extraction with back extractant to obtain regenerated organic phase and lead back extraction pregnant solution; e) the regenerated organic phase returns to the step b) for recycling; f) degreasing the rich solution of the back extraction of lead to obtain a lead before-electrodeposition solution; g) the lead before electrodeposition is used to obtain metal lead through electrodeposition, and the regenerated acidic stripping agent in the electrodeposition process is returned to the extraction system for recycling.)

1. A method for producing metallic lead by adopting a solvent extraction electrodeposition process is characterized by comprising the following steps: the method comprises the following steps:

a) ball-milling the lead-containing material, leaching with a chlorinated coordination leaching agent, and carrying out liquid-solid separation to obtain a lead-containing leaching solution and leaching residues;

b) adjusting the pH of the lead-containing leachate, mixing the lead-containing leachate with a lead extracting agent for extraction to obtain an organic phase loaded with lead ions and a raffinate, wherein part of the raffinate is returned to the step a) for recycling, and the other part of the raffinate utilizes SO in the solution₄ ^2-、Cl^-Preparing calcium sulfate and calcium chloride byproducts;

c) washing impurities in the lead ion-loaded organic phase by using an acidic washing solution to obtain a pure lead-loaded organic phase and a washing solution;

d) carrying out back extraction on the pure lead-loaded organic phase by using an acidic back extractant Muse501 to obtain a regenerated organic phase and a lead back-extraction rich solution;

e) the regenerated organic phase returns to the step b) for recycling;

f) degreasing the rich solution of the back extraction of lead to obtain a lead before-electrodeposition solution;

g) the lead before electrodeposition is used to obtain metal lead through electrodeposition, and the regenerated acidic stripping agent in the electrodeposition process is returned to the extraction system for recycling.

2. The method of claim 1, wherein the chloride complex lixiviant of step a) is a mixed salt ion solution comprising NH₄ ⁺The content of the organic solvent is 30-130 g/L, Cl^-The content of 120-260 g/L, SO₄ ^2-The content is 85g/L, Ca²⁺3～50g/L、Mg²⁺1～15g/L、Na⁺0～5.0g/L。

3. The method for producing metallic lead by the solvent extraction electrodeposition process as claimed in claim 1, wherein the pH is adjusted to 7.0 to 8.0 with ammonia before the extraction in step b).

4. The method for producing metallic lead by the solvent extraction electrodeposition process according to claim 1, wherein the lead extractant in the step b) is an acidic phosphine-containing extractant, and the acidic phosphine-containing extractant Muse302 comprises 5-15% by mass of 5-nonylsalicylic acid, 10-15% by mass of 2-ethylhexyl phosphoric acid mono-2-ethylhexyl ester, 5-10% by mass of 1-phenyl-3-methyl-4-benzoylpyrazolone and diluent sulfonated kerosene.

5. The method of claim 1, wherein a portion of the raffinate from step b) is treated with soluble calcium salt to remove SO from the system₄ ^2-The calcium sulfate byproduct with the purity of 98 percent is removed, SO that the problem of SO in the raw material is solved₄ ^2-The problem of enrichment; removal of SO₄ ^2-Recovering ammonia water from lead extraction raffinate through slaked lime alkali adjustment and ammonia distillationThen evaporating and crystallizing to obtain calcium chloride byproduct, thereby solving the problem of Cl in the raw material^-The problem of enrichment.

6. The method for producing metallic lead by the solvent extraction electrodeposition process as claimed in claim 1, wherein the acidic washing solution in step c) is any one or more of acetic acid solution, hydrochloric acid solution, nitric acid solution, methanesulfonic acid solution, ethylsulfonic acid solution and soluble lead salt.

7. The method for producing metallic lead by solvent extraction electrodeposition according to claim 1, wherein in the step d), the acidic stripping agent Muse501 is any one or more of oxalic acid, citric acid, capric acid, sulfamic acid, methanesulfonic acid and ethylsulfonic acid; wherein the concentration of the acid is controlled to be 1.0-6.0 mol/L.

8. The method of claim 1, wherein the step e) further comprises adding an additive that inhibits side reactions at the anode of the electrolytic lead, wherein the additive is a mixture of phosphate and arsenate, and the phosphate and arsenate are 50% each.

9. The method for producing metallic lead by the solvent extraction electrodeposition process as claimed in claim 1, wherein the oil content of the lead before electrodeposition obtained after degreasing in step f) is less than 10 ppm.

10. The method for producing metallic lead by the solvent extraction electrodeposition process as claimed in claim 1, wherein in the step g), the electrodeposition parameter current density is 100 to 1000A/m²The addition amount of the mixture of phosphate and arsenate is 1.0-8.0 g/L, the addition amount of lignosulfonate is 0.5-10 g/L, the temperature of the electrolyte is 35-50 ℃, the circulation amount of the electrolyte is 20-100L/h, the inter-polar distance is 40-100 mm, the material of the electrolytic anode plate is titanium-based lead dioxide, and the cathode is a stainless steel plate.

Technical Field

The invention relates to a process for recovering lead by wet metallurgy, in particular to a method for producing metallic lead by adopting a solvent extraction electrodeposition process.

Background

At present, the smelting mode of lead is almost pyrometallurgy, and if refined lead is obtained, crude lead is obtained by pyrometallurgy, and then the obtained crude lead is refined and electrolyzed to obtain the refined lead. The method for preparing the refined lead has the advantages of long flow, high energy consumption, large equipment investment and high production cost.

In recent years, many researchers have studied lead hydrometallurgy, and typical hydrometallurgy processes include ferric salt leaching, alkaline leaching, solid-phase transformation, electrochemical leaching, chloride leaching, amine leaching, pressure leaching, ammonium ammoniate leaching, hydrofluoric acid, and hydrofluoric acid leaching. However, harmful gases (such as hydrogen fluoride, chlorine and the like) are generated in the process of electrodepositing lead by the traditional wet process, so that the environment pollution and the equipment corrosion are caused, the energy consumption per ton of products is high, and the flow is complex. In addition, the impurity removal is difficult, and if the raw materials contain some soluble salts, anions carried by the salts enter the solution, and the separation of the anions is very difficult.

Disclosure of Invention

Aiming at the defects in the prior art, the invention provides a method for producing metallic lead by adopting a solvent extraction electrodeposition process, which particularly can use sulfuric acid as a production raw material and can utilize SO enriched in the raw material₄ ^2-、Cl^-By-products of calcium sulfate and calcium chloride are produced. The solution does not need to be purified and decontaminated in the whole production process, and the leaching agent, the extracting agent and the back extracting agent are all recycled. The whole process flow is simple to operate, low in equipment investment, low in running cost, clean and efficient.

In order to achieve the purpose, the invention adopts the following technical scheme: a method for producing metallic lead by a solvent extraction electrodeposition process, comprising the steps of:

a) ball-milling the lead-containing material, leaching with a chlorinated coordination leaching agent, and carrying out liquid-solid separation to obtain a lead-containing leaching solution and leaching residues;

b) adjusting the pH of the lead-containing leachate, mixing the lead-containing leachate with a lead extracting agent for extraction to obtain an organic phase loaded with lead ions and a raffinate, wherein part of the raffinate is returned to the step a) for recycling, and the other part of the raffinate utilizes SO in the solution₄ ^2-、Cl^-Preparing calcium sulfate and calcium chloride byproducts;

c) washing impurities in the lead ion-loaded organic phase by using an acidic washing solution to obtain a pure lead-loaded organic phase and a washing solution;

d) carrying out back extraction on the pure lead-loaded organic phase by using an acidic back extractant Muse501 to obtain a regenerated organic phase and a lead back-extraction rich solution;

e) the regenerated organic phase returns to the step b) for recycling;

f) degreasing the rich solution of the back extraction of lead to obtain a lead before-electrodeposition solution;

g) the lead before electrodeposition is used to obtain metal lead through electrodeposition, and the regenerated acidic stripping agent in the electrodeposition process is returned to the extraction system for recycling.

In the process of separating and extracting lead from waste lead batteries, lead-zinc ores, lead oxide ores, low-grade complex lead-containing waste residues and lead-containing sludge, the solution is not required to be purified, wherein the leaching agent, the extracting agent and the back-extraction agent are all recycled, no waste water, waste acid or waste gas is generated in the production process, no pollution is caused to the environment, and the method has the advantages of simple process, low equipment investment, low operation cost, cleanness, high efficiency and the like.

Preferably, in step a), the chlorinated coordination leaching agent is a mixed salt ion solution (Muse 3#), wherein NH₄ ⁺The content of the organic solvent is 30-130 g/L, Cl^-The content of 120-260 g/L, SO₄ ^2-The content is 85g/L, Ca²⁺3～50g/L、Mg²⁺1～15g/L、Na⁺0-5.0 g/L; the lead-containing material comprises one or more of lead oxide, lead carbonate, lead chloride, lead hydroxide, lead sulfate or waste lead; the solid-liquid separation equipment is a filter press, a sedimentation centrifuge, a sedimentation thickener, a floating ball clarifier, a bag filter or a separation column. Book (I)The Muse3# leaching agent in the invention has three important characteristics: the first characteristic is as follows: can directionally leach lead in lead-containing materials such as lead oxide, lead carbonate, lead sulfate, lead chloride, lead hydroxide and the like, and lead is leached with Pb under the condition of solution in the presence of the leaching agent²⁺Exists in the form of complex ions; the second characteristic is that: when the leaching agent reaches a certain concentration, lead sulfate can be rapidly dissolved, and the saturated solubility can reach 30 g/L; the third characteristic: at the same concentration, the solubility of calcium sulfate was 0 g/l.

Preferably, in step b), the pH of the pre-extraction solution is adjusted to 7.0-8.0 by ammonia water, and the lead extractant is an acidic phosphine-containing extractant Muse 302.

Preferably, the acidic phosphine-containing extractant Muse302 consists of 5-15% by mass of 5-nonylsalicylic acid (HRJ-4277), 10-15% by mass of 2-ethylhexyl phosphoric acid mono-2-ethylhexyl ester (PC-88A), 5-10% by mass of 1-phenyl-3-methyl-4-benzoyl pyrazolone (HPMBP) and diluent sulfonated kerosene.

The extraction selectivity of the extractant Muse302 for selectively extracting lead is up to more than 99.8 percent, and the loading capacity of the extractant Muse302 for lead reaches 10 g/v percent; solves the problem of SO in the raw materials₄ ^2-、Cl^-In the Muse3# leaching system, SO₄ ^2-Is very easy to react with Ca²⁺Forming needle-shaped calcium sulfate dihydrate precipitate; cl^-Then with Ca²⁺The calcium chloride is formed, and both byproducts can meet the requirements of industrial products, so that the production cost is reduced.

The main chemical reactions involved are as follows:

PbO+2(Muse3#)⁺+2Cl^-＝Pb(Muse3#)₂Cl₂+H₂O

Pb(OH)₂+2(Muse3#)⁺+2Cl^-＝Pb(Muse3#)₂Cl₂+2H₂O

PbCO₃+2(Muse3#)⁺+2Cl^-＝Pb(Muse3#)₂Cl₂+H₂O+CO₂↑

the leaching principle of the lead sulfate in a Muse3# leaching agent solution system is as follows:

PbSO₄+2(Muse3#)⁺+2Cl^-→Pb(Muse3#)₂Cl₂+SO₄ ^2-

the extraction principle is as follows:

2H(Muse302)+Pb²⁺→Pb(Muse302)₂+2H⁺

preferably, in the step c), the acidic washing solution used in the washing process is any one or a mixture of more of an acetic acid solution, a hydrochloric acid solution, a nitric acid solution, a methanesulfonic acid solution, an ethylsulfonic acid solution and a soluble lead salt. The raffinate part returns to the leaching system for recycling, and the main chemical reactions involved are as follows:

Pb(Muse3#)₂Cl₂+2Muse302→Pb(Muse302)₂+2Muse3#++2Cl^-

the regeneration principle is that the extracting agents Muse302 and Pb are adopted²⁺The ionic bonding allowed the reaction to proceed to the right, Muse3# +, with Cl^-Continuously regenerating the lead ions back to the leaching system to complex new lead ions.

Preferably, in the step d), the acidic stripping agent is one or more of oxalic acid, citric acid, capric acid, sulfamic acid, methanesulfonic acid and ethylsulfonic acid, and has the advantages of high boiling point, good stability, strong acidity, low toxicity, high conductivity (close to the same concentration of hydrochloric acid or sulfuric acid), high solubility of lead salt in water, and the concentration of the acid is controlled to be 1.0-6.0 mol/L. Acid mist is not generated in the process of electrodeposition, and the electrochemical reaction in the process of electrodeposition is as follows:

and (3) cathode reaction: pb²⁺+2e^-＝Pb

And (3) anode reaction: h₂O-2e^-＝2H⁺+1/2O₂

The total reaction is as follows: pb²⁺+H₂O＝Pb+1/2O₂+2H⁺

The back extraction principle is as follows:

Pb(Muse302)₂+2H⁺→2H(Muse302)+Pb²⁺

the Muse501 stripping agent has the following five advantages:

first, excellent lead salt solubility, Pb²⁺The saturation solubility in Muse501 solvent was 2.6mol/dm^-3；

Second, having excellent conductivity;

thirdly, the catalyst is very stable and is not easy to be damaged in a strong oxidation environment;

fourthly, the toxicity is low and the biological degradation is easy to occur;

fifthly, acid mist is not generated in the process of electrodeposition, and environmental pollution is avoided.

Preferably, the step e) further comprises adding an additive for inhibiting the side reaction of the electrolytic lead anode, wherein the additive is a mixture of phosphate and arsenate, and the phosphate and the arsenate respectively account for 50%. The inhibition effect of the mixture of phosphate and arsenate on lead dioxide is the result of selective adsorption of the mixture of phosphate and arsenate on the electrode, so that the lead recovery rate is increased, and the power consumption is reduced. The side reaction of the anode is as follows:

Pb²⁺+2H₂O-2e^-＝PbO₂+4H⁺

preferably, in the step f), the lead content in the lead strip pregnant solution is controlled to be 100-300 g/L, the acid concentration is controlled to be 0.25-3.0mol/L, and the oil content is less than 10 ppm.

Preferably, in the step g), the current density of the electrodeposition parameter is 100-1000A/m²The addition amount of the mixture of phosphate and arsenate is 1.0-8.0 g/L, the addition amount of lignosulfonate is 0.5-10 g/L, the temperature of the electrolyte is 35-50 ℃, the circulation amount of the electrolyte is 20-100L/h, the inter-polar distance is 40-100 mm, the material of the electrolytic anode plate is titanium-based lead dioxide, and the cathode is a stainless steel plate. Compared with the traditional electrolytic lead, the electrolytic lead has the advantages of high electric efficiency and low power consumption per ton of products

The invention has the following beneficial effects: can directionally leach lead in lead-containing materials such as lead oxide, lead carbonate, lead sulfate, lead chloride, lead hydroxide and the like, and lead is leached with Pb under the condition of solution in the presence of the leaching agent²⁺Exists in the form of complex ions; the leaching agent reaches a certain concentrationLead sulfate can be rapidly dissolved, and the saturated solubility can reach 30 g/L; at the same concentration, the solubility of calcium sulfate is 0 g/L; the invention discloses an extractant Muse302 capable of selectively extracting lead, which avoids the traditional low-efficiency chemical impurity removal purification process, the extraction selectivity of the extractant for lead is up to more than 99.8 percent, and the load capacity for lead reaches-10 g/v percent; containing Pb²⁺The complex ion solution can regenerate the Muse3# leaching agent after being mixed with the extracting agent Muse302 for extracting lead, and returns to the leaching system for recycling; the invention discloses a Muse501 stripping agent suitable for lead electrodeposition, which has excellent lead salt solubility and Pb²⁺The saturation solubility in Muse501 solvent was 2.6mol/dm^-3(ii) a Has excellent conductivity; the catalyst is very stable and is not easy to be damaged in a strong oxidation environment; low toxicity and easy biodegradation; acid mist is not generated in the process of electrodeposition, so that the environmental pollution is avoided; the additive for inhibiting the side reaction of the electrolytic lead anode is invented, the recovery rate of lead is increased, and the power consumption is reduced; SO in the raw Material₄ ^2-、Cl^-The problem of enrichment in the traditional leaching agent system is effectively solved, and in the Muse3# leaching system, SO₄ ^2-Is very easy to react with Ca²⁺Forming needle-shaped calcium sulfate dihydrate precipitate; cl^-Then with Ca²⁺Calcium chloride is formed, and both byproducts can meet the requirements of industrial products, so that the production cost is reduced; compared with the traditional electrolytic lead, the electrolytic lead has the advantages of high electric efficiency and low power consumption per ton of products; the leaching agent, the extracting agent and the back extracting agent in the whole process flow realize regeneration and recycling, and the method has the advantages of simple operation, clean running process, high efficiency and no waste gas.

Drawings

FIG. 1 is a process flow diagram of the present invention.

Detailed Description

A method of producing metallic lead by a solvent extraction electrodeposition process according to the present invention is further illustrated by figure 1.

A method for producing metallic lead by adopting a solvent extraction electrodeposition process comprises the following steps:

a) ball milling the lead-containing materialLeaching with a chlorinated coordination leaching agent, and performing solid-liquid separation to obtain a lead-containing leaching solution and leaching residues. In the embodiment, the chloridized coordination leaching agent is a mixed salt ion solution (Muse 3#), wherein NH₄ ⁺The content of the organic solvent is 30-130 g/L, Cl^-The content of 120-260 g/L, SO₄ ^2-The content is 85g/L, Ca²⁺3～50g/L、Mg²⁺1～15g/L、Na⁺0-5.0 g/L; the lead-containing material comprises one or more of lead oxide, lead carbonate, lead chloride, lead hydroxide, lead sulfate or waste lead.

b) Adjusting the pH value of the lead-containing leachate to 7.0-8.0 by using ammonia water, mixing and extracting the lead-containing leachate with a lead extracting agent Muse302 according to the A/O ratio of 1-6: 1, wherein the extraction temperature is 20-55 ℃, and standing and layering the lead-containing leachate after oscillation for 1-10 min to obtain an organic phase loaded with lead ions and raffinate; after extracting other metals, returning part of the obtained raffinate to the leaching section for recycling, and producing byproducts calcium sulfate and calcium chloride; in the embodiment, the lead extractant is an acidic phosphine-containing extractant Muse302, and the acidic phosphine-containing extractant Muse302 consists of 5-15% by mass of 5-nonylsalicylic acid (HRJ-4277), 10-15% by mass of 2-ethylhexyl phosphoric acid mono-2-ethylhexyl ester (PC-88A), 5-10% by mass of 1-phenyl-3-methyl-4-benzoyl pyrazolone (HPMBP) and diluent sulfonated kerosene.

c) Washing the lead ion-loaded organic phase obtained in the step b) by using an acidic washing solution to obtain a washed organic phase and washed water, and returning the washed water to the step a); in the embodiment, one or more of acetic acid, hydrochloric acid, nitric acid, methanesulfonic acid, ethyl sulfonic acid liquid and soluble lead salt are prepared in proportion, impurity ions extracted from an organic phase, such as zinc, cadmium, calcium, copper, magnesium, iron and the like, and entrained extraction stock solution are washed, and the purity of the organic phase entering a back extraction section is ensured.

d) And c) performing back extraction on the washed organic phase obtained in the step c) by using a back extraction agent to obtain a regenerated organic phase and a back extraction rich solution, adjusting the phase ratio of the back extraction, and controlling the lead content of the rich solution to be 100-300 g/L and the acid concentration to be 0.25-3.0 mol/L. The stripping agent adopts high-concentration organic acid Muse501, wherein the concentration of the acid is controlled to be 1.0-6.0 mol/L.

e) The regenerated organic phase obtained in the step d) returns to the step b) for recycling.

f) And d) removing oil from the back extraction rich solution obtained in the step d) through air flotation and activated carbon to obtain lead before-electrodeposition solution, wherein the oil content is less than 10 ppm.

g) And f), electrodepositing the lead pre-electrodeposition solution obtained in the step f) to obtain metal lead. Wherein the lead electrodeposition parameter current density is 100-1000A/m²The addition amount of the mixture of phosphate and arsenate is 1.0-8.0 g/L, the addition amount of lignosulfonate is 0.5-10 g/L, the temperature of the electrolyte is 25-50 ℃, the circulation amount of the electrolyte is 20-100L/h, the inter-polar distance is 40-100 mm, the electrolytic anode plate is made of titanium-based lead dioxide, and the cathode is a stainless steel plate. At 200A/m²The electric efficiency under the current density can reach more than 97 percent, and the power consumption per ton of products is as low as 530 Kwh.

In the extraction process, the pH is under the neutral condition, so that the direct extraction of lead ions by organic phase unsaponifiable materials is realized, and the single-stage extraction rate can reach more than 90%. In the back extraction process, organic acid Muse501 with high equivalent weight is adopted to carry out back extraction on the organic phase, and the enrichment of lead ions is realized through the ratio adjustment of the organic phase and the water phase. Solves the problem of SO in the raw materials by producing calcium sulfate and calcium chloride₄ ^2-、Cl^-The problem of enrichment.

The present invention is further illustrated by the following specific examples.

Example 1

Passing a material containing lead slag containing 20% of lead, lead-containing sludge and lead-zinc through NH₄ ⁺The content is 110g/L, Cl^-Content 205g/L, SO₄ ^2-The content is 50g/L, Ca²⁺5.0g/L、Mg²⁺5.0g/L、 Na⁺And (3) mixing and leaching 4.0g/L of Muse3# leaching agent, and filtering to obtain a lead-containing leachate, wherein the lead content in the leachate is 4-16g/L, and the SS is less than 5 ppm. Adjusting the pH of the solution to 7.5 by using ammonia water, mixing the solution with an acidic phosphine-containing extractant Muse302 for extraction, oscillating for 3min to obtain an organic phase loaded with lead ions, wherein the acidic phosphine-containing extractant Muse302 comprises 5 mass percent of 5-nonylsalicylic acid (HRJ-4277), 10 mass percent of 2-ethylhexyl phosphate mono-2-ethylhexyl (PC-88A) and the mass percent of5% of 1-phenyl-3-methyl-4-benzoyl pyrazolone (HPMBP) and diluent sulfonated kerosene.

After the organic phase is washed by an acidic washing solution, organic acid Muse501 stripping agent is adopted for stripping to obtain pregnant solution containing lead at 150g/L and acid concentration of 1.00 mol/L. After the rich solution of lead is subjected to active carbon degreasing, the lead pre-electrodeposition solution with oil content less than 5ppm is obtained. Controlling the current density to 400A/m²The additive amount of sodium phosphate and sodium arsenate is 2.0g/L, the additive amount of sodium lignosulfonate is 3.0g/L, the temperature of the electrolyte is 40 ℃, the circulation amount of the electrolyte is 80L/h, the inter-polar distance is 45mm, the electrolytic anode plate is a titanium-based lead dioxide material plate, the cathode is a stainless steel plate, high-purity metal lead is obtained by electrodeposition, the cell voltage is 2.74V, the electric efficiency is 97%, the anode side reaction is obviously inhibited, and the power consumption per ton of product is 727.0 Kwh. And returning part of the lead extraction raffinate to leaching for recycling. And adding calcium chloride to combine with sulfate radical in the solution to obtain calcium sulfate as side product with purity up to 98%, adding calcined lime to regulate alkali and evaporate ammonia to obtain calcium chloride solution, and final evaporating to crystallize to obtain calcium chloride as side product.

Example 2

Passing a lead sulfate material containing 20% of lead through NH₄ ⁺The content is 90g/L, Cl^-The content is 180g/L, SO₄ ^2-The content is 40g/L, Ca²⁺4.0g/L、Mg²⁺4.0g/L、Na⁺3.0g/L Muse3# leaching agent is mixed, leached and filtered to prepare the lead-containing leachate, wherein the lead content in the leachate is 6-8g/L, and the SS is less than 5 ppm. Adjusting the pH of the solution to 7.8 by using ammonia water, mixing the solution with an acidic phosphine-containing extractant Muse302 for extraction, and oscillating for 3min to obtain an organic phase loaded with lead ions, wherein the acidic phosphine-containing extractant Muse302 comprises 5 mass percent of 5-nonylsalicylic acid (HRJ-4277), 10 mass percent of 2-ethylhexyl phosphoric acid mono-2-ethylhexyl ester (PC-88A), 5 mass percent of 1-phenyl-3-methyl-4-benzoyl pyrazolone (HPMBP) and a diluent of sulfonated kerosene.

After the organic phase is washed by an acidic washing solution, organic acid Muse501 stripping agent is adopted for stripping to obtain pregnant solution containing lead at 170g/L and acid concentration of 1.20 mol/L. The lead is rich inAnd (3) after the liquid is subjected to active carbon oil removal, obtaining lead pre-electrodeposition liquid with oil content less than 5 ppm. Controlling the current density to 200A/m²The additive amount of sodium phosphate and sodium arsenate is 2.5g/L, the additive amount of sodium lignosulfonate is 2.0g/L, the temperature of the electrolyte is 40 ℃, the circulation amount of the electrolyte is 80L/h, the inter-polar distance is 45mm, the electrolytic anode plate is a titanium-based lead dioxide material plate, the cathode is a stainless steel plate, high-purity metal lead is obtained by electrodeposition, the cell voltage is 2.06V, the electric efficiency is 99.2%, the anode side reaction is obviously inhibited, and the power consumption per ton of finished products is 536.5 KWh. And returning part of the lead extraction raffinate to leaching for recycling. And adding calcium chloride to combine with sulfate radical in the solution to obtain calcium sulfate as side product with purity up to 98%, adding calcined lime to regulate alkali and evaporate ammonia to obtain calcium chloride solution, and final evaporating to crystallize to obtain calcium chloride as side product.

Example 3

Filtering slag after the material containing lead 18 percent of lead is leached by pressurized oxygen and is reacted with NH₄ ⁺The content is 120g/L, Cl^-The content is 240g/L, SO₄ ^2-The content is 60g/L, Ca²⁺6.0g/L、Mg²⁺5.0g/L、 Na⁺And (3) mixing and leaching 3.5g/L Muse3# leaching agent, and filtering to obtain a lead-containing leachate, wherein the lead content in the leachate is 8-12g/L, and the SS is less than 5 ppm. Adjusting the pH of the solution to 7.1 by using ammonia water, mixing the solution with an acidic phosphine-containing extractant Muse302 for extraction, and oscillating for 3min to obtain an organic phase loaded with lead ions, wherein the acidic phosphine-containing extractant Muse302 comprises 5 mass percent of 5-nonylsalicylic acid (HRJ-4277), 10 mass percent of 2-ethylhexyl phosphoric acid mono-2-ethylhexyl ester (PC-88A), 5 mass percent of 1-phenyl-3-methyl-4-benzoyl pyrazolone (HPMBP) and a diluent of sulfonated kerosene.

After the organic phase is washed by an acidic washing solution, organic acid Muse501 stripping agent is adopted for stripping to obtain pregnant solution containing lead at 160g/L and acid concentration of 0.80 mol/L. After the rich solution of lead is subjected to active carbon degreasing, the lead pre-electrodeposition solution with oil content less than 5ppm is obtained. Controlling the current density to 200A/m²The addition amounts of sodium phosphate and sodium arsenate are respectively 1.5g/L, the mixed addition amount of calcium lignosulfonate and sodium lignosulfonate is 1.5g/L, the temperature of the electrolyte is 45℃,The electrolyte circulation amount is 80L/h, the inter-polar distance is 45mm, the electrolytic anode plate is a titanium-based lead dioxide material plate, the cathode is a stainless steel plate, high-purity metal lead is obtained by electrodeposition, the cell voltage is 2.12V, the electric efficiency is 98.8 percent, the anode side reaction is obviously inhibited, and the power consumption per ton of finished products is 555.2 Kwh. And returning part of the lead extraction raffinate to leaching for recycling. And adding calcium chloride to combine with sulfate radical in the solution to obtain calcium sulfate as side product with purity up to 98%, adding calcined lime to regulate alkali and evaporate ammonia to obtain calcium chloride solution, and final evaporating to crystallize to obtain calcium chloride as side product.

In conclusion, the method comprehensively utilizes a large amount of raw materials which are incapable of being comprehensively utilized and contain high content of other impurities, such as low-grade lead slag, lead-containing sludge, lead-zinc ores, lead pastes, particularly lead sulfate and the like, and has the advantages of simple process flow operation, low equipment investment, low running cost, environmental protection, cleanness and high efficiency.

The above description is only a preferred embodiment of the present invention, and the protection scope of the present invention is not limited to the above embodiments, and all technical solutions belonging to the idea of the present invention belong to the protection scope of the present invention.