A process for the extraction of molybdenum from white fume and the production of a pure molybdenum product
Patent Information
- Application Number
- CN202611366502.5
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2026-09-04
- Publication Date
- 2026-10-23
AI Technical Summary
[0002]钼是战略稀有金属，广泛应用于特种合金、军工、催化、光伏行业，冶炼副产白烟尘中含有大量钼组分，同时伴生砷、铜、锌、铅等杂质，若直接堆存会造成重金属、砷污染，且钼资源大量流失
[0026]1、钼回收率大幅提升：两段梯度硫酸浸出，低酸预浸+高酸强化浸出协同，钼总浸出率≥96%，尾渣钼残留低于0.10%，资源利用率显著优于单段浸出工艺；
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Figure CN122959524A_ABST
Abstract
Description
Technical Field
[0001] This invention belongs to the field of metal smelting technology, specifically a method for extracting molybdenum from white smoke dust and preparing pure molybdenum products. Background Technology
[0002] Molybdenum is a strategic rare metal widely used in special alloys, military industry, catalysis, and photovoltaic industry. The white smoke dust produced as a by-product of smelting contains a large amount of molybdenum components, along with impurities such as arsenic, copper, zinc, and lead. Direct storage will cause heavy metal and arsenic pollution, and a large amount of molybdenum resources will be lost. Currently, there is no process for extracting molybdenum from white dust to produce high-purity molybdenum products. Existing technologies for extracting molybdenum from white dust only go as far as sulfide molybdenum slag, and have many shortcomings: 1. Single-stage acid leaching results in low molybdenum leaching rate, insufficient dissociation of sparingly soluble molybdenum minerals in the dust, high molybdenum residue in solid waste, and poor resource utilization; 2. The leachate contains high levels of arsenic and copper impurities, the traditional sulfide precipitation method has poor selectivity for impurity removal, serious loss of molybdenum co-precipitation, and insufficient purity of the final molybdenum product; 3. The by-products of impurity removal, arsenic slag and copper slag, lack closed-loop treatment, and the solution lacks graded recycling and reuse, resulting in high water and reagent consumption. Existing technologies cannot simultaneously achieve high molybdenum leaching, deep impurity removal, full solution recycling, by-product classification and resource utilization, and high-purity molybdenum product preparation. Therefore, there is an urgent need to develop a new closed-loop, clean, high-recovery, and high-purity molybdenum extraction process. Summary of the Invention
[0003] Based on this, the purpose of the present invention is to provide a method for extracting molybdenum from white smoke dust and preparing pure molybdenum products, so as to solve the technical problems mentioned in the background above.
[0004] To achieve the above objectives, the present invention provides the following technical solution: a method for extracting molybdenum from white smoke dust and preparing pure molybdenum products, comprising the following steps:
[0005] S1. Two-stage gradient sulfuric acid leaching: First stage leaching: the white dust raw material is slurried according to the liquid-solid ratio, stirred and reacted, and then filtered to obtain first stage leachate and first stage leach residue; Second stage leaching: the first stage leach residue and the first stage leachate are slurried according to the solid ratio, reacted and filtered to obtain second stage leachate and second stage leach residue. The second stage leachate is returned to the first stage leaching cycle, and the second stage leach residue is sent to the oxygen-enriched blast furnace.
[0006] S2, First-stage leaching solution cooling and arsenic removal crystallization: The first-stage leaching solution is cooled to 0-30℃, crystallized for 1-10 hours, filtered, and the crystallized residue is used to prepare metallic arsenic or arsenic matte. The cooled solution is then precisely filtered.
[0007] S3. Anion exchange resin sulfuric acid conversion: The anion exchange resin is converted by acidification with sulfuric acid solution, and then washed with water.
[0008] S4. Molybdenum adsorption by resin: After cooling, the liquid is passed into the resin column after transformation, and three or more stages of adsorption are connected in series. The liquid after adsorption is sent to the copper plating process.
[0009] S5. Molybdenum removal by sodium hydroxide in stages: Saturated resin is washed with water until effluent is obtained, and then washed with sodium hydroxide solution. The first stage of the wash solution with a molybdenum concentration >30g / L is sent to the purification arsenic precipitation stage, and the second stage of the wash solution with a molybdenum concentration <30g / L is returned to the alkali preparation cycle. After washing, the resin is washed with water until pH 8-10 and then regenerated by sulfuric acid conversion.
[0010] S6. Two-stage copper precipitation with arsenic sulfide slag after adsorption: In the first stage, copper precipitation is insufficient. Arsenic sulfide slag is added to the adsorption liquid, and after reaction, it is filtered to obtain copper sulfide slag and copper precipitation liquid. In the second stage, copper precipitation is excessive. Arsenic sulfide slag is added to the copper precipitation liquid, and after reaction, the crude copper sulfide slag is returned to the first stage of copper precipitation, and the second stage of copper precipitation liquid is reduced and crystallized to remove arsenic.
[0011] S7. Reduction, cooling and crystallization of copper precipitate liquid: Sulfur dioxide is introduced into the copper precipitate liquid of the second stage to reduce pentavalent arsenic, and the liquid is cooled to 0-20℃ to crystallize for 5-48 hours. The crystallization residue is used to make arsenic peat, and the mother liquor is sent to the zinc neutralization and purification system.
[0012] S8. Purification of molybdenum precipitate solution with composite salt: High molybdenum precipitate solution is oxidized with hydrogen peroxide, pH is adjusted to 8.0-10.0 with sulfuric acid, magnesium salt is added, followed by ammonium salt and aluminum salt. Sodium hydroxide is used to adjust the pH to 8.5-9.5. After reacting for 1-3 hours, the solution is filtered, the purified residue is washed with water, molybdenum is recovered from the washing liquid, and the final residue is sent to an oxygen-enriched blast furnace. The purified liquid after fine filtration is polymerized to precipitate molybdenum.
[0013] S9. Ammonium salt polymerization precipitation of molybdenum: After purification, add ammonium salt at 10-150 kg / m³, add 0.5-2 kg / m³ of molybdenum slag as seed crystals, adjust the pH to 1.5-2.5 with sulfuric acid, react at 40-80℃ for 3-12 hours, filter to obtain molybdenum slag, and evaporate and concentrate the molybdenum precipitation mother liquor.
[0014] S10, Mother liquor evaporation and crystallization to produce sodium salt: The molybdenum precipitation mother liquor is concentrated to 1 / 4 to 1 / 2 of its original volume, cooled to 0 to 30°C and crystallized for 2 to 48 hours. The crystallized mother liquor is recycled back for purification and arsenic precipitation. The sodium salt crystals are sold externally.
[0015] S11. Refining of molybdenum slag by ammonia redissolution: Prepare 10%–15% dilute ammonia water to dissolve the crude molybdenum slag to a system pH of 9.0–10.0, filter, and leach the filter residue with 10%–15% ammonia water at a liquid-to-solid ratio of 2:1. The solid slag is returned to the first leaching step S1, and the ammonia filtrate is circulated. The molybdenum ammonia solution obtained from the first dissolution is pH adjusted, evaporated, cooled and crystallized to prepare high-purity ammonium molybdate or molybdate product.
[0016] Furthermore, in step S1, the white dust raw material in the first stage leaching is prepared with a liquid-to-solid ratio of 2:1 to 6:1, a sulfuric acid concentration of 10 to 70 g / L, a stirring reaction time of 1.5 to 3 hours, and a stirring reaction temperature of 70 to 90°C; in the second stage leaching, the first stage leaching residue and the first stage leaching liquid are mixed with a solid ratio of 2:1 to 6:1, a sulfuric acid concentration of 70 to 150 g / L, a reaction time of 1.5 to 3 hours, and a reaction temperature of 80 to 95°C.
[0017] Furthermore, in step S3, the anion exchange resin is selected from D201, D301, D314 or other strong / weak basic anion exchange resins containing primary / tertiary / quaternary ammonium groups. It is acidified and transformed using a 30-200 g / L sulfuric acid solution, with an acid dosage of 1-15 BV, a flow rate of 0.5-5 BV / h, and a temperature of 20-55℃. After transformation, it is washed with water until the pH is 1-2.
[0018] Furthermore, in step S4, the acidity of the feed solution is controlled to be <80g / L, the single column flow rate is 0.5~20BV / h, and the temperature is 20~55℃.
[0019] Furthermore, in step S5, the saturated resin is washed with water until the effluent pH is 4-5, and then eluted with a 90-150 g / L sodium hydroxide solution. The elution liquid volume is 2-10 BV, the flow rate is 0.5-20 BV / h, and the temperature is 20-55℃.
[0020] Furthermore, in step 6, in the first stage of insufficient copper precipitation, 0.4 to 0.9 times the theoretical amount of arsenic sulfide slag is added to the adsorption liquid, with an acidity of 40 to 120 g / L, and the reaction is carried out at 80 to 100°C for 1 to 4 hours. The copper sulfide slag is washed and then sent to the copper smelting system to recover metallic copper. In the second stage of insufficient copper precipitation, 1.2 to 1.5 times the theoretical amount of arsenic sulfide slag is added to the copper precipitation liquid, with an acidity of 40 to 120 g / L, and the reaction is carried out at 90 to 95°C for 2 to 3 hours.
[0021] Furthermore, in step S8, the magnesium salt is magnesium chloride or magnesium sulfate, the ammonium salt is ammonium sulfate or ammonium chloride, and the aluminum salt is aluminum chloride or aluminum sulfate.
[0022] Furthermore, in step S9, the ammonium salt is ammonium sulfate.
[0023] Furthermore, the temperature of the resin sulfation transformation in step S3, the adsorption in step 4, the desorption in step 5, and the resin regeneration process are all controlled within the range of 20 to 55°C.
[0024] Furthermore, the ammonium molybdate / molybdic acid product refined in step S11 has a purity of ≥99.95% and a total molybdenum recovery rate of ≥96% throughout the entire process.
[0025] In summary, the present invention has the following main beneficial effects:
[0026] 1. Significantly improved molybdenum recovery rate: Two-stage gradient sulfuric acid leaching, with low-acid pre-leaching and high-acid enhanced leaching working synergistically, achieves a total molybdenum leaching rate of ≥96%, with molybdenum residue in the tailings below 0.10%, resulting in a resource utilization rate significantly better than that of single-stage leaching processes;
[0027] 2. High selectivity for impurity removal and low molybdenum loss: The resin anion exchange selectively captures molybdenum, while copper is removed by gradient precipitation of arsenic sulfide slag and stepwise crystallization of arsenic + co-precipitation of composite salts. The total molybdenum co-precipitation loss is <1.5% throughout the process.
[0028] 3. Green and free of organic hazardous waste: The entire process uses ion exchange resin instead of solvent extraction, with no organic phase volatilization and no hazardous waste liquid from extraction, reducing environmental protection operation and maintenance costs by more than 40%.
[0029] 4. Closed-loop circulation of all media: The two-stage leachate, low-molybdenum leaching solution, and crystallization mother liquor are refluxed and reused in stages, with an industrial water reuse rate of ≥92% and a 35% reduction in the consumption of sulfuric acid and sodium hydroxide reagents;
[0030] 5. Full utilization of solid waste resources: By-products such as copper sulfide, metallic arsenic / arsenic matte, and sodium salt are all exportable products, with no toxic or hazardous waste stockpiled, achieving the synergistic recovery of multiple metals including arsenic, copper, molybdenum, and zinc;
[0031] 6. High product purity: The crude molybdenum slag is purified by secondary remelting with ammonia water to remove trace impurities such as arsenic, antimony, silicon, aluminum, bismuth, copper and lead, and can be used to prepare national standard high-purity ammonium molybdate and molybdic acid. The product purity is ≥99.95%, and the market added value is significantly improved.
[0032] 7. Wide process adaptability: It has a wide parameter range and can handle various smelting white dust with high arsenic, high copper, and high zinc content. It has stable continuous industrial operation and strong automation adaptability. Attached Figure Description
[0033] Figure 1 This is a process flow diagram of the present invention. Detailed Implementation
[0034] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. The embodiments described below with reference to the accompanying drawings are exemplary and are only used to explain the present invention, and should not be construed as limiting the present invention.
[0035] The embodiments of the present invention will now be described.
[0036] like Figure 1 As shown, this embodiment provides a method for extracting molybdenum from white smoke dust and preparing pure molybdenum products, including the following steps:
[0037] The raw materials used in this invention are: copper smelting white dust, with a molybdenum content of 1.2%, arsenic of 12.7%, copper of 3.1%, and zinc of 5.8%.
[0038] S1. Two-stage gradient sulfuric acid leaching: First stage leaching: white dust raw material is prepared into a slurry with a liquid-to-solid ratio of 2:1 to 6:1, sulfuric acid concentration of 10 to 70 g / L, and stirred at 70 to 90°C for 1.5 to 3 hours. The slurry is then filtered to obtain first stage leachate and first stage leach residue. Second stage leaching: the slurry from the first stage leaching is prepared into a slurry with a liquid-to-solid ratio of 2:1 to 6:1, sulfuric acid concentration of 70 to 150 g / L, and stirred at 80 to 95°C for 1.5 to 3 hours. The slurry is then filtered, the second stage leachate is returned to the first stage leaching cycle, and the second stage leach residue is sent to an oxygen-enriched blast furnace.
[0039] S2, First-stage leaching solution cooling and arsenic removal crystallization: The first-stage leaching solution is cooled to 0-30℃, crystallized for 1-10 hours, filtered, and the crystallized residue is used to prepare metallic arsenic or arsenic matte. The cooled solution is then precisely filtered.
[0040] S3. Anion exchange resin sulfuric acid conversion: Select D201, D301, D314 and other strong / weak basic anion exchange resins containing primary / tertiary / quaternary ammonium groups. Acidify and convert the resins using 30-200 g / L sulfuric acid solution. The acid dosage is 1-15 BV, the flow rate is 0.5-5 BV / h, and the temperature is 20-55℃. After conversion, wash with water until pH=1-2.
[0041] S4. Molybdenum adsorption by resin: After cooling, the liquid is passed into the resin column after transformation. The acidity of the liquid is controlled to be <80g / L. Three or more stages are connected in series for adsorption. The flow rate of a single column is 0.5~20BV / h and the temperature is 20~55℃. The liquid after adsorption is sent to the copper plating process.
[0042] S5. Molybdenum removal by sodium hydroxide in stages: Saturated resin is washed with water until the effluent pH is 4-5, then washed with 90-150 g / L sodium hydroxide solution at a volume of 2-10 BV, a flow rate of 0.5-20 BV / h, and a temperature of 20-55℃. The first stage of the wash solution with a molybdenum concentration >30 g / L is sent to the purification and arsenic precipitation stage, while the second stage of the wash solution with a molybdenum concentration <30 g / L is returned to the alkali preparation cycle. After washing, the resin is washed with water until the pH is 8-10 and then regenerated by sulfuric acid conversion.
[0043] S6. Two-stage copper precipitation with arsenic sulfide slag after adsorption: First stage: insufficient copper precipitation, 0.4-0.9 times the theoretical amount of arsenic sulfide slag is added to the adsorption liquid, acidity 40-120 g / L, reaction at 80-100℃ for 1-4 h, and filtered to obtain copper sulfide slag and copper precipitation liquid; Second stage: excessive copper precipitation, 1.2-1.5 times the theoretical amount of arsenic sulfide slag is added to the copper precipitation liquid, acidity 40-120 g / L, reaction at 90-95℃ for 2-3 h, the crude copper sulfide slag is returned to the first stage of copper precipitation, and the second stage of copper precipitation liquid is reduced and crystallized to remove arsenic;
[0044] S7. Reduction, cooling and crystallization of copper precipitate liquid: Sulfur dioxide is introduced into the copper precipitate liquid of the second stage to reduce pentavalent arsenic, and the liquid is cooled to 0-20℃ to crystallize for 5-48 hours. The crystallization residue is used to make arsenic peat, and the mother liquor is sent to the zinc neutralization and purification system.
[0045] S8. Purification of molybdenum leaching solution with composite salt to precipitate arsenic: High-molybdenum leaching solution is oxidized with hydrogen peroxide, pH is adjusted to 8.0-10.0 with sulfuric acid, 1.2 times the theoretical amount of magnesium salt is added, followed by ammonium salt and aluminum salt. Sodium hydroxide is used to finally adjust the pH to 8.5-9.5, and the reaction is carried out for 1-3 hours before filtration. The purified residue is washed with water, and molybdenum is recovered from the washing liquid. The final residue is sent to an oxygen-enriched blast furnace. The purified liquid after fine filtration is polymerized to precipitate molybdenum.
[0046] Preferably, the magnesium salt is magnesium chloride or magnesium sulfate, the ammonium salt is ammonium sulfate or ammonium chloride, and the aluminum salt is aluminum chloride or aluminum sulfate.
[0047] S9. Ammonium salt polymerization to precipitate molybdenum: After purification, add ammonium salt at 10-150 kg / m³, add 0.5-2 kg / m³ of molybdenum slag as seed crystals, adjust the pH to 1.5-2.5 with sulfuric acid, react at 40-80℃ for 3-12 hours, filter to obtain molybdenum slag, and evaporate and concentrate the mother liquor for molybdenum precipitation; the above ammonium salt is ammonium sulfate.
[0048] S10, Mother liquor evaporation and crystallization to produce sodium salt: The molybdenum precipitation mother liquor is concentrated to 1 / 4 to 1 / 2 of its original volume, cooled to 0 to 30°C and crystallized for 2 to 48 hours. The crystallized mother liquor is recycled back for purification and arsenic precipitation. The sodium salt crystals are sold externally.
[0049] S11. Redissolving and refining of molybdenum slag with ammonia: Prepare 10%–15% dilute ammonia solution to dissolve the crude molybdenum slag to a system pH of 9.0–10.0, and filter; the filter residue is leached a second time with 10%–15% ammonia solution at a liquid-to-solid ratio of 2:1, and the solid residue is returned to the first leaching step S1, while the ammonia filtrate is recycled; the molybdenum ammonia solution obtained from the first dissolution is pH adjusted, evaporated, cooled and crystallized to prepare high-purity ammonium molybdate or molybdate product.
[0050] Preferably, the temperature of the resin sulfation transformation in step S3, the adsorption in step 4, the desorption in step 5, and the resin regeneration process are all controlled within the range of 20 to 55°C.
[0051] The ammonium molybdate / molybdic acid product refined by this invention has a purity of ≥99.95% and a comprehensive molybdenum recovery rate of ≥96% throughout the entire process.
[0052] Compared with the traditional single-stage acid leaching + solvent extraction method for extracting molybdenum from white dust and preparing pure molybdenum products, the method of this invention, using the same white dust raw material, involves single-stage sulfuric acid leaching followed by di(2-ethylhexyl)phosphoric acid extraction; the total molybdenum recovery rate is only 82.3%, the molybdenum product purity is 98.6%, the organic extraction waste liquid generation is 12 m³ / ton of dust, and the reagent consumption is 41% higher. The comparison clearly shows that this invention is superior in terms of recovery rate, product purity, and environmental indicators.
[0053] Although embodiments of the present invention have been shown and described, these specific embodiments are merely explanations of the invention and are not intended to limit it. The specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples. After reading this specification, those skilled in the art may make modifications, substitutions, and variations to the embodiments as needed without departing from the principles and spirit of the invention, but such modifications, substitutions, and variations are protected by patent law as long as they are within the scope of the claims of the present invention.
Claims
1. A method for extracting molybdenum from white smoke dust and preparing pure molybdenum products, characterized in that... Includes the following steps: S1. Two-stage gradient sulfuric acid leaching: First stage leaching: the white dust raw material is slurried according to the liquid-solid ratio, stirred and reacted, and then filtered to obtain first stage leachate and first stage leach residue; Second stage leaching: the first stage leach residue and the first stage leachate are slurried according to the solid ratio, reacted and filtered to obtain second stage leachate and second stage leach residue. The second stage leachate is returned to the first stage leaching cycle, and the second stage leach residue is sent to the oxygen-enriched blast furnace. S2, First-stage leaching solution cooling and arsenic removal crystallization: The first-stage leaching solution is cooled to 0-30℃, crystallized for 1-10 hours, filtered, and the crystallized residue is used to prepare metallic arsenic or arsenic matte. The cooled solution is then precisely filtered. S3. Anion exchange resin sulfuric acid conversion: The anion exchange resin is converted by acidification with sulfuric acid solution, and then washed with water. S4. Molybdenum adsorption by resin: After cooling, the liquid is passed into the resin column after transformation, and three or more stages of adsorption are connected in series. The liquid after adsorption is sent to the copper plating process. S5. Molybdenum removal by sodium hydroxide in stages: Saturated resin is washed with water until effluent is obtained, and then washed with sodium hydroxide solution. The first stage of the wash solution with a molybdenum concentration >30g / L is sent to the purification arsenic precipitation stage, and the second stage of the wash solution with a molybdenum concentration <30g / L is returned to the alkali preparation cycle. After washing, the resin is washed with water until pH 8-10 and then regenerated by sulfuric acid conversion. S6. Two-stage copper precipitation with arsenic sulfide slag after adsorption: In the first stage, copper precipitation is insufficient. Arsenic sulfide slag is added to the adsorption liquid, and after reaction, it is filtered to obtain copper sulfide slag and copper precipitation liquid. In the second stage, copper precipitation is excessive. Arsenic sulfide slag is added to the copper precipitation liquid, and after reaction, the crude copper sulfide slag is returned to the first stage of copper precipitation, and the second stage of copper precipitation liquid is reduced and crystallized to remove arsenic. S7. Reduction, cooling and crystallization of copper precipitate liquid: Sulfur dioxide is introduced into the copper precipitate liquid of the second stage to reduce pentavalent arsenic, and the liquid is cooled to 0-20℃ to crystallize for 5-48 hours. The crystallization residue is used to make arsenic peat, and the mother liquor is sent to the zinc neutralization and purification system. S8. Purification of molybdenum precipitate solution with composite salt: High molybdenum precipitate solution is oxidized with hydrogen peroxide, pH is adjusted to 8.0-10.0 with sulfuric acid, magnesium salt is added, followed by ammonium salt and aluminum salt. Sodium hydroxide is used to adjust the pH to 8.5-9.
5. After reacting for 1-3 hours, the solution is filtered, the purified residue is washed with water, molybdenum is recovered from the washing liquid, and the final residue is sent to an oxygen-enriched blast furnace. The purified liquid after fine filtration is polymerized to precipitate molybdenum. S9. Ammonium salt polymerization precipitation of molybdenum: After purification, add ammonium salt at 10-150 kg / m³, add 0.5-2 kg / m³ of molybdenum slag as seed crystals, adjust the pH to 1.5-2.5 with sulfuric acid, react at 40-80℃ for 3-12 hours, filter to obtain molybdenum slag, and evaporate and concentrate the molybdenum precipitation mother liquor. S10, Mother liquor evaporation and crystallization to produce sodium salt: The molybdenum precipitation mother liquor is concentrated to 1 / 4 to 1 / 2 of its original volume, cooled to 0 to 30°C and crystallized for 2 to 48 hours. The crystallized mother liquor is recycled back for purification and arsenic precipitation. The sodium salt crystals are sold externally. S11. Refining of molybdenum slag by ammonia redissolution: Prepare 10%–15% dilute ammonia water to dissolve the crude molybdenum slag to a system pH of 9.0–10.0, filter, and leach the filter residue with 10%–15% ammonia water at a liquid-to-solid ratio of 2:
1. The solid slag is returned to the first leaching step S1, and the ammonia filtrate is circulated. The molybdenum ammonia solution obtained from the first dissolution is pH adjusted, evaporated, cooled and crystallized to prepare high-purity ammonium molybdate or molybdate product.
2. The method for extracting molybdenum from white smoke dust and preparing pure molybdenum products according to claim 1, characterized in that: In step S1, the white dust raw material in the first stage leaching is prepared with a liquid-to-solid ratio of 2:1 to 6:1, a sulfuric acid concentration of 10 to 70 g / L, a stirring reaction time of 1.5 to 3 hours, and a stirring reaction temperature of 70 to 90°C. In the second stage leaching, the first stage leaching residue and the first stage leaching liquid are mixed with a solid ratio of 2:1 to 6:1, a sulfuric acid concentration of 70 to 150 g / L, a reaction time of 1.5 to 3 hours, and a reaction temperature of 80 to 95°C.
3. The method for extracting molybdenum from white smoke dust and preparing pure molybdenum products according to claim 1, characterized in that: In step S3, the anion exchange resin is selected from D201, D301, D314 or other strong / weak basic anion exchange resins containing primary / tertiary / quaternary ammonium groups. It is acidified and transformed using a 30-200 g / L sulfuric acid solution with an acid volume of 1-15 BV, a flow rate of 0.5-5 BV / h, and a temperature of 20-55℃. After transformation, it is washed with water until the pH is 1-2.
4. The method for extracting molybdenum from white smoke dust and preparing pure molybdenum products according to claim 1, characterized in that: In step S4, the acidity of the feed solution is controlled to be <80g / L, the single column flow rate is 0.5~20BV / h, and the temperature is 20~55℃.
5. The method for extracting molybdenum from white smoke dust and preparing pure molybdenum products according to claim 1, characterized in that: In step S5, the saturated resin is washed with water until the effluent pH is 4-5, and then eluted with a 90-150 g / L sodium hydroxide solution. The elution liquid volume is 2-10 BV, the flow rate is 0.5-20 BV / h, and the temperature is 20-55℃.
6. The method for extracting molybdenum from white smoke dust and preparing pure molybdenum products according to claim 1, characterized in that: In step 6, in the first stage of insufficient copper precipitation, 0.4 to 0.9 times the theoretical amount of arsenic sulfide slag is added to the adsorption liquid, with an acidity of 40 to 120 g / L, and the reaction is carried out at 80 to 100°C for 1 to 4 hours. The copper sulfide slag is washed and then sent to the copper smelting system to recover metallic copper. In the second stage of insufficient copper precipitation, 1.2 to 1.5 times the theoretical amount of arsenic sulfide slag is added to the copper precipitation liquid, with an acidity of 40 to 120 g / L, and the reaction is carried out at 90 to 95°C for 2 to 3 hours.
7. The method for extracting molybdenum from white smoke dust and preparing pure molybdenum products according to claim 1, characterized in that: In step S8, the magnesium salt is magnesium chloride or magnesium sulfate, the ammonium salt is ammonium sulfate or ammonium chloride, and the aluminum salt is aluminum chloride or aluminum sulfate.
8. The method for extracting molybdenum from white smoke dust and preparing pure molybdenum products according to claim 1, characterized in that: In step S9, the ammonium salt is ammonium sulfate.
9. The method for extracting molybdenum from white smoke dust and preparing pure molybdenum products according to claim 1, characterized in that: The temperature is controlled within the range of 20 to 55°C throughout the entire process, including resin sulfation transformation in step S3, adsorption in step 4, desorption in step 5, and resin regeneration.
10. The method for extracting molybdenum from white smoke dust and preparing pure molybdenum products according to claim 1, characterized in that: The ammonium molybdate / molybdic acid product refined in step S11 has a purity of ≥99.95% and a comprehensive molybdenum recovery rate of ≥96% throughout the entire process.