Method for extracting metallic gallium from vanadium extraction converter sludge

Abstract

The present application provides a kind of method for extracting metal gallium by vanadium extraction converter sludge, comprising the following steps: S1: vanadium extraction converter sludge is leached with leaching agent, and gallium leaching solution is obtained;S2: the gallium leaching solution of step S1 is extracted, and gallium-containing organic phase is obtained;S3: the gallium-containing organic phase of step S2 is back-extracted, and gallium-containing aqueous phase is obtained;S4: the gallium-containing aqueous phase of step S3 is treated to obtain gallium-containing precipitate, and the gallium-containing precipitate is dissolved in alkali to obtain gallium-containing alkali solution, which is treated by electrolysis to obtain metal gallium.The raw material for extracting gallium is unique, the gallium content is high, the gallium extraction process is short, the impurity removal effect is good, and the by-product produced has higher purity and better economic value.

Description

Technical Field

[0001] This invention relates to the field of rare metal smelting, and more specifically to a method for extracting metallic gallium using vanadium extraction converter sludge. Background Technology

[0002] Gallium, a rare and dispersed metal, is an important strategic resource. A series of compound semiconductor materials, electron optical materials, novel functional materials, special alloys, and organometallic compounds prepared using gallium metal as a matrix are crucial foundational materials for modern high-tech fields such as computers, communications, aerospace, new energy, medicine and healthcare, and military industries. Approximately 90% of the world's gallium is recovered from the production of alumina, forming a mature industrial chain. Gallium is also enriched during zinc smelting and in coal ash, but the extraction of gallium from these two raw materials has not been industrialized due to the long extraction process and high costs.

[0003] The Panxi region has a wide variety of valuable metals. Gallium is associated with elements such as V, Fe, and Ti in Panxi minerals. Currently, gallium extraction research mainly uses vanadium extraction tailings as raw material. However, due to the complex composition of vanadium extraction tailings, direct acid leaching yields low efficiency, consumes a large amount of acid, and generates a large number of unusable byproducts. Furthermore, the entire process is very long, so this route has not been put into industrial production. CN 106957963 A discloses a method for extracting gallium from vanadium extraction tailings, but this method has also not been industrialized due to its lack of economic viability.

[0004] Therefore, there is an urgent need for an economical and efficient method for extracting gallium. Summary of the Invention

[0005] To address the shortcomings of existing technologies, the present invention aims to provide a method for extracting metallic gallium using vanadium extraction converter sludge.

[0006] To achieve the above objectives, the present invention adopts the following technical solution:

[0007] This invention provides a method for extracting metallic gallium from vanadium-extraction converter sludge, comprising the following steps:

[0008] S1: Leach the vanadium extraction converter sludge with a leaching agent to obtain gallium leaching solution;

[0009] S2: Extract the gallium leaching solution from step S1 to obtain a gallium-containing organic phase;

[0010] S3: Back-extract the gallium-containing organic phase from step S2 to obtain a gallium-containing aqueous phase;

[0011] S4: The gallium-containing aqueous phase in step S3 is processed to obtain a gallium-containing precipitate. The gallium-containing precipitate is dissolved in alkali to obtain a gallium-containing alkaline solution, which is then electrolyzed to obtain metallic gallium.

[0012] Further, in step S1,

[0013] The leaching agent is an oxalic acid solution of 100-300 g / L, the mass ratio of the leaching agent to the vanadium extraction converter sludge is (2-30):1, the leaching temperature is 40-90℃, and the leaching time is 0.5-10 h.

[0014] Furthermore, during the extraction process in step S2, the volume ratio of the organic phase to the aqueous phase is 1:(0.5-10).

[0015] Furthermore, the organic phase includes an extractant and a diluent, wherein the volume of the extractant accounts for less than 60% of the volume of the organic phase, and the amount of the diluent added accounts for at least 40% of the volume of the organic phase.

[0016] Furthermore,

[0017] The extractant is one or more of TBP, P204, N235, P507, TOPO, and neodecanoic acid, and different extractants are combined in any proportion.

[0018] The diluent is sulfonated kerosene or industrial kerosene.

[0019] Further, in step S3, the pH of the back-extraction aqueous phase is 5-10, wherein,

[0020] The solution in the aqueous phase of the back-extraction is one or more of sodium hydroxide, potassium hydroxide, sodium carbonate, sodium bicarbonate, and pure water in any proportion.

[0021] Furthermore, in step S4, the pH of the gallium-containing alkali solution is greater than 9.5, the electrolysis temperature is 25-75℃, and the current density is 100-2000 A / m. 2 .

[0022] Furthermore, during the electrolysis process, the anode material is graphite, stainless steel, or platinum, lead, silver, titanium, tungsten or molybdenum metal or their alloys, and the cathode material is copper-indium alloy or indium-gallium alloy.

[0023] Furthermore, in step S4, the gallium-containing precipitate is gallium hydroxide.

[0024] Furthermore, the mass content of each component in the vanadium extraction converter sludge is as follows: 85-95% Fe2O3, 0-2% SiO2, 1-5% ZnO, and the remainder is any combination of Na2O, MgO, CaCO3, Al2O3, TiO2, V2O5, Cr2O3, MnO, PbO, CuO, NiO, chloride, and sulfide, with a total content of less than 10%.

[0025] Compared with the prior art, the beneficial technical effects of the present invention are as follows:

[0026] The gallium extraction process of this invention is unique, with high gallium content, short process, and good impurity removal effect. At the same time, the generated by-products have high purity and good economic value. Attached Figure Description

[0027] To more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings used in the description of the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0028] Figure 1 This is a schematic flowchart of the method for extracting metallic gallium using vanadium-extraction converter sludge according to the present invention. Detailed Implementation

[0029] To make the objectives, technical solutions, and advantages of the present invention clearer, the embodiments of the present invention will be further described in detail below with reference to specific examples and the accompanying drawings.

[0030] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0031] The main components of the gallium extraction raw material, vanadium extraction converter sludge, involved in this invention, have the following mass content: 85-95% Fe2O3, 0-2% SiO2, 1-5% ZnO, with the remainder being any combination of Na2O, MgO, CaCO3, Al2O3, TiO2, V2O5, Cr2O3, MnO, PbO, CuO, NiO, chlorides, and sulfides, with a total content of less than 10%. The elemental gallium content in the vanadium extraction converter sludge is 200-500 g / t.

[0032] like Figure 1 As shown, the present invention provides a method for extracting metallic gallium using vanadium-extraction converter sludge, comprising the following steps:

[0033] S1: Leach the vanadium extraction converter sludge with a leaching agent to obtain gallium leaching solution.

[0034] The leaching agent is an oxalic acid solution of 100-300 g / L, the mass ratio of the leaching agent to the vanadium extraction converter sludge is (2-30):1, the leaching temperature is 40-90℃, and the leaching time is 0.5-10 h.

[0035] Vanadium extraction converter sludge has small particles during its generation, so it can be directly mixed with oxalic acid without pretreatment. If the sludge particles are too large, they need to be ground to less than 4 mm. Mix the sludge with the oxalic acid particles, then add water to control the initial oxalic acid solution concentration at 100-300 g / L. Alternatively, the sludge can be poured into an oxalic acid solution with a concentration of 100-300 g / L. The mass ratio of leaching agent to sludge (i.e., liquid-solid ratio) should be controlled at (2-30):1. After the addition is complete, heat the mixture to 40-90℃ and leach for 0.5-10 hours. During leaching, the mixture can be stirred, allowed to stand, or the solution can be shaken.

[0036] After leaching, the gallium leaching rate can reach 85-99%. If the gallium leaching rate is less than 85% after the first leaching, the leaching residue can be leached again to ensure that the gallium leaching rate is not less than 85%. The leaching mixture obtained from the two leachings is mixed, and then the leaching mixture is allowed to cool slowly. When the temperature drops below 30°C, the solid and liquid are separated by filtration or sedimentation to obtain the gallium leaching solution.

[0037] S2: Extract the gallium leaching solution from step S1 to obtain a gallium-containing organic phase.

[0038] The gallium leaching solution is extracted, and the solid is washed with deionized water 1-5 times to obtain ferrous oxalate (with water of crystallization) with a purity of over 95%. The wash water can be recycled to the leaching process in step S1 above, forming zero discharge.

[0039] In the extraction process, the volume ratio of the organic phase to the aqueous phase is 1:(0.5-10). The organic phase includes the extractant and the diluent. The volume of the extractant accounts for less than 60% of the organic phase volume, and the amount of diluent added is at least 40% of the organic phase volume. The extractant can be one or more of the following: TBP (tributyl phosphate), P204 (di(2-ethylhexyl) phosphate), N235 (trioctylamine), P507 (2-ethylhexyl phosphate mono-2-ethylhexyl ester), TOPO (tri-n-octylphosphine oxide), and neodecanoic acid. When a mixed extractant is used, different extractants can be combined in any proportion, but the volume of the extractant should be less than 60% of the total organic phase volume. The diluent can be sulfonated kerosene or other types of industrial kerosene.

[0040] Extraction methods are not limited to laboratory equipment or industrial extraction tanks, extraction towers, and centrifugal extractors. After extraction, the substances produced in the extraction process must be filtered as a whole. The filtered solid is washed with deionized water 1-5 times to obtain ferrous oxalate (with water of crystallization) with a purity of over 95%. The wash water is recycled to the leaching process in step S1, resulting in zero discharge. After extraction, over 95% of gallium enters the organic phase, while over 90% of impurities remain in the raffinate.

[0041] S3: Back-extract the gallium-containing organic phase from step S2 to obtain a gallium-containing aqueous phase.

[0042] This invention eliminates the need for washing the gallium-containing organic phase, allowing for direct back-extraction. The pH of the back-extraction aqueous phase is controlled between 5 and 10, achieving a gallium recovery rate of over 95% after back-extraction. The solution in the back-extraction aqueous phase can be one or more of the following in any proportion: sodium hydroxide, potassium hydroxide, sodium carbonate, sodium bicarbonate, and pure water.

[0043] S4: The gallium-containing aqueous phase in step S3 is processed to obtain a gallium-containing precipitate. After the gallium-containing precipitate is dissolved in alkali, it is electrolyzed to obtain metallic gallium.

[0044] The gallium-containing precipitate after back-extraction is gallium hydroxide. This precipitate is dissolved in an alkaline sodium hydroxide solution, or mixed with sodium oxide and slowly added to water. Once the precipitate is completely dissolved, a gallium-containing alkaline solution is obtained, which is then electrolyzed. The pH of the electrolyte (gallium-containing alkaline solution) is controlled above 9.5.

[0045] During electrolysis, the anode material is graphite, stainless steel, or platinum, lead, silver, titanium, tungsten, or molybdenum metals or their alloys, while the cathode material is a copper-indium alloy or an indium-gallium alloy, but not limited to the above electrode types. The electrolysis temperature can be controlled between 25-75℃, and the current and voltage vary depending on the type of electrode, with the current density controlled between 100-2000 A / m. 2 The electrolysis process can be a single-stage or multi-stage electrolysis to ensure a gallium recovery rate of over 98%. The electrolyzed product is metallic gallium conforming to GB / T 1475-2022.

[0046] Example 1

[0047] The main components of the gallium extraction raw material—vanadium extraction converter sludge—in this embodiment are 95% Fe2O3, 2% SiO2, and 1.5% ZnO by mass, with the remainder being a mixture of Na2O, MgO, CaCO3, Al2O3, TiO2, V2O5, Cr2O3, MnO, PbO, CuO, NiO, chlorides, and sulfides, accounting for 1.5% of the total. The elemental gallium content in the vanadium extraction converter sludge is 500 g / t.

[0048] After sieving, all particles of the vanadium extraction converter sludge were smaller than 4mm. The vanadium extraction converter sludge was mixed with oxalic acid particles for 30 minutes, and then water was added. The initial concentration of the oxalic acid solution was controlled at 270g / L, and the liquid-to-solid ratio was 15:1. After the addition was complete, the mixture was heated to 80℃ and leached for 4 hours at a stirring speed of 300rpm.

[0049] After leaching, the gallium leaching rate can reach 99%. After the leaching mixture is slowly cooled to below 30°C, it is separated into solid and liquid components using a filter press to obtain a gallium-containing leachate. This leachate then enters the extraction stage. The solid is washed three times with deionized water to obtain ferrous oxalate (with water of crystallization) with a purity of over 95%, forming a high-value byproduct. The wash water is recycled back into the leaching process, achieving zero discharge.

[0050] In the extraction process, the volume ratio of the organic phase to the aqueous phase is 1:0.5. The active ingredients in the organic phase are TBP and P204 extractant. TBP :V P204 The concentration was 0.5, the diluent was sulfonated kerosene, and the extraction device was an industrial extraction tank. After extraction, the substances produced in the extraction process were filtered out. The filtered solid was washed twice with deionized water to obtain ferrous oxalate (with water of crystallization) with a purity of over 95%, which could be combined with the leaching byproducts. The wash water was recycled back to the leaching process, resulting in zero discharge. After extraction, over 95% of the gallium entered the organic phase, while over 90% of the impurities remained in the raffinate.

[0051] After extraction, back-extraction is performed directly, with the pH of the back-extraction aqueous phase controlled at 7. The gallium recovery rate after back-extraction precipitation can reach 95%. The solution in the back-extraction aqueous phase is a mixture of sodium bicarbonate and pure water.

[0052] The precipitate after back-extraction was dissolved in a sodium hydroxide alkaline solution until completely dissolved, yielding a gallium-containing solution. This solution was then electrolyzed, with the pH maintained at 9.6. During electrolysis, the anode material was stainless steel, and the cathode material was an indium-gallium alloy. The electrolysis temperature was 45℃, and the current density was 800 A / m³. 2 This electrolysis is a two-stage electrolysis. The crude gallium after the first-stage electrolysis is dissolved in sodium hydroxide solution and then subjected to a second electrolysis. The product after electrolysis is metallic gallium that conforms to GB / T1475-2022. The gallium recovery rate in this process reaches 99%.

[0053] Example 2

[0054] The main components of the gallium extraction raw material—vanadium extraction converter sludge—in this embodiment are 88% Fe2O3, 2% SiO2, and 5% ZnO, with the remainder being a mixture of Na2O, MgO, CaCO3, Al2O3, TiO2, V2O5, Cr2O3, MnO, PbO, CuO, NiO, chlorides, and sulfides, accounting for 5% of the total. The elemental gallium content of the vanadium extraction converter sludge is 280 g / t.

[0055] Larger particles of the vanadium extraction converter sludge, after being sieved, were ball-milled for 30 minutes until they could all pass through a 4mm sieve. The vanadium extraction converter sludge was then poured into a 300g / L oxalic acid solution with a liquid-to-solid ratio of 20:1. After the addition was complete, the mixture was heated to 70℃ and allowed to stand for leaching for 10 hours.

[0056] After leaching, the gallium leaching rate can reach 93%. When the leaching mixture is slowly cooled to below 30°C, solid-liquid separation is achieved through filtration, yielding a gallium-containing leachate. This leachate then enters the extraction stage. The solid is washed once with deionized water to obtain ferrous oxalate (with water of crystallization) with a purity of over 95%. The wash water can be recycled back to the first leaching process, achieving zero discharge.

[0057] In the extraction process, the volume ratio of the organic phase to the aqueous phase is 1:10. The effective components in the organic phase are P2O4, N235, and P5O7 mixed in a 1:1:1 volume ratio, and industrial kerosene is used as the diluent. The extraction device is an extraction tower. After extraction, the substances produced in the extraction process are filtered out. The filtered solid is washed twice with deionized water to obtain ferrous oxalate (with water of crystallization) with a purity of over 95%. The wash water is recycled to the leaching process, resulting in zero discharge. After extraction, 97% of the gallium enters the organic phase, while over 90% of the impurities remain in the raffinate.

[0058] In this embodiment, no washing of the organic phase is required, and back-extraction can be performed directly. The pH of the back-extraction aqueous phase is controlled at 8, and the gallium recovery rate after back-extraction precipitation can reach 97%. The solution in the back-extraction aqueous phase is a mixed solution of sodium hydroxide and pure water.

[0059] The precipitate after back-extraction was mixed with sodium oxide and slowly added to water. After the precipitate was completely dissolved, a gallium-containing solution was obtained, which was then electrolyzed. The pH of the gallium-containing solution was controlled at 10. During electrolysis, the anode material was graphite, and the cathode material was an indium-gallium alloy. The electrolysis temperature was 55℃, and the current density was 1000 A / m. 2 The electrolysis process is a single-stage electrolysis, and the product after electrolysis is metallic gallium that conforms to GB / T1475-2022. The gallium recovery rate in this process reaches 99%.

[0060] Example 3

[0061] The main components of the gallium extraction raw material—vanadium extraction converter sludge—in this embodiment are 85% Fe2O3, 1% ZnO, and the remainder is a mixture of Na2O, MgO, CaCO3, Al2O3, TiO2, V2O5, Cr2O3, MnO, PbO, CuO, NiO, chlorides, and sulfides, accounting for 1.4% of the total. The elemental gallium content of the vanadium extraction converter sludge is 200 g / t.

[0062] Vanadium extraction converter sludge can be directly mixed with oxalic acid. The initial concentration of the oxalic acid solution is controlled at 100 g / L. The liquid-to-solid ratio is 30:1. After feeding is complete, the mixture is heated to 90°C and the slurry is ultrasonically vibrated for 0.5 hours.

[0063] After the first leaching, the gallium leaching rate can reach 85%. After the leaching mixture is slowly cooled to below 30°C, solid-liquid separation is achieved through filtration, yielding a gallium-containing leachate. This leachate then enters the extraction stage. The solid is washed five times with deionized water to obtain ferrous oxalate (with water of crystallization) with a purity of over 99%. The wash water can be recycled back to the first leaching process, achieving zero discharge.

[0064] In the extraction process, the volume ratio of the organic phase to the aqueous phase is 1:5. The active ingredients in the organic phase are TOPO and P507 mixed in a 1:1 volume ratio, and the diluent is industrial kerosene. A centrifugal extractor is used. After extraction, the substances produced in the extraction process are filtered out. The filtered solid is washed five times with deionized water to obtain ferrous oxalate (with water of crystallization) with a purity of over 95%. The wash water is recycled to the leaching process, resulting in zero discharge. After extraction, 95% of the gallium enters the organic phase, while over 90% of the impurities remain in the raffinate.

[0065] In this embodiment, no washing of the organic phase is required, and back-extraction can be performed directly. The pH of the back-extraction aqueous phase is controlled at 5, and the gallium recovery rate after back-extraction precipitation can reach 99%. The solution in the back-extraction aqueous phase is a mixed solution of sodium carbonate and pure water.

[0066] The precipitate after back-extraction was mixed with sodium oxide and slowly added to water. After the precipitate was completely dissolved, a gallium-containing solution was obtained, which was then electrolyzed. The pH of the gallium-containing solution was controlled at 9.7. During electrolysis, the anode material was a lead-silver alloy, and the cathode material was an indium-gallium alloy. The electrolysis temperature was 25℃, and the current density was 2000 A / m. 2 The electrolysis process is a single-stage electrolysis, and the product after electrolysis is metallic gallium that conforms to GB / T1475-2022. The gallium recovery rate in this process reaches 98%.

[0067] Example 4

[0068] The main components of the gallium extraction raw material—vanadium extraction converter sludge—in this embodiment are 90% Fe2O3, 1.5% SiO2, and 3% ZnO, with the remainder being a mixture of Na2O, MgO, CaCO3, Al2O3, TiO2, V2O5, Cr2O3, MnO, PbO, CuO, NiO, chlorides, and sulfides, accounting for 5.5% of the total. The elemental gallium content of the vanadium extraction converter sludge is 300 g / t.

[0069] Larger particles of the vanadium extraction converter sludge, after being sieved, were ball-milled for 10 minutes until they could all pass through a 4mm sieve. The vanadium extraction converter sludge was then poured into a 300g / L oxalic acid solution with a liquid-to-solid ratio of 2:1. After the addition was complete, the mixture was heated to 40℃ and leached with stirring for 8 hours.

[0070] After the first leaching, the gallium leaching rate can reach 80%. After the leaching mixture is slowly cooled to below 30°C, solid-liquid separation is achieved through filtration, yielding a gallium-containing leaching solution and leaching residue. The leaching residue undergoes a second leaching process using the same procedure, achieving a gallium leaching rate of up to 97%. The two leaching solutions are then mixed and proceed to the extraction stage. The remaining solid is washed once with deionized water to obtain ferrous oxalate (with water of crystallization) with a purity of over 95%. The wash water can be recycled back to the first leaching process, achieving zero discharge.

[0071] In the extraction process, the volume ratio of the organic phase to the aqueous phase is 1:3. The active ingredient in the organic phase is TBP, and the diluent is sulfonated kerosene. The extraction device is an industrial extraction tank. After extraction, the substances produced in the extraction process are filtered out. The filtered solid is washed once with deionized water to obtain ferrous oxalate (with water of crystallization) with a purity of over 95%. The wash water is recycled to the leaching process, resulting in zero discharge. After extraction, 98% of the gallium enters the organic phase, while over 90% of the impurities remain in the raffinate.

[0072] In this embodiment, no washing of the organic phase is required, and back-extraction can be performed directly. The pH of the back-extraction aqueous phase is controlled at 10, and the gallium recovery rate after back-extraction precipitation can reach 97%. The solution in the back-extraction aqueous phase is a mixed solution of potassium hydroxide and pure water.

[0073] The precipitate after back-extraction was mixed with sodium oxide and slowly added to water. After the precipitate was completely dissolved, a gallium-containing solution was obtained, which was then electrolyzed. The pH of the gallium-containing solution was controlled at 10.5. During electrolysis, the anode material was a titanium alloy, and the cathode material was a copper-indium alloy. The electrolysis temperature was 75℃, and the current density was 100 A / m. 2 The electrolysis process is a single-stage electrolysis, and the product after electrolysis is metallic gallium that conforms to GB / T1475-2022. The gallium recovery rate in this process reaches 99%.

[0074] It should be noted that the components or steps in the above embodiments can be interchanged, substituted, added, or deleted. Therefore, the combinations formed by these reasonable permutations and transformations should also fall within the protection scope of this invention, and the protection scope of this invention should not be limited to the above embodiments.

[0075] Those skilled in the art should understand that the discussion of any of the above embodiments is merely exemplary and is not intended to imply that the scope of the invention (including the claims) is limited to these examples. Within the framework of the invention, technical features of the above embodiments or different embodiments can be combined, and many other variations of the different aspects of the invention as described above exist, which are not provided in the details for the sake of brevity. Therefore, any omissions, modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the invention should be included within the protection scope of the invention.

Claims

1. A method for extracting metallic gallium from vanadium-extraction converter sludge, characterized in that, The vanadium extraction converter sludge comprises 85-95% Fe2O3 by mass, and the content of elemental gallium in the vanadium extraction converter sludge is 200-500 g / t. The method includes the following steps: S1: Leach the vanadium extraction converter sludge with an oxalic acid solution of 100-300 g / L to obtain gallium leaching solution; S2: Extract the gallium leaching solution from step S1 to obtain a gallium-containing organic phase and ferrous oxalate; S3: Back-extract the gallium-containing organic phase from step S2 to obtain a gallium-containing aqueous phase; S4: The gallium-containing aqueous phase in step S3 is processed to obtain a gallium-containing precipitate. The gallium-containing precipitate is dissolved in alkali to obtain a gallium-containing alkaline solution, which is then electrolyzed to obtain metallic gallium.

2. The method according to claim 1, characterized in that, In step S1, The mass ratio of leaching agent to vanadium extraction converter sludge is (2-30):1, the leaching temperature is 40-90°C, and the leaching time is 0.5-10h.

3. The method according to claim 1, characterized in that, In the extraction process of step S2, the volume ratio of the organic phase to the aqueous phase is 1:(0.5-10).

4. The method according to claim 3, characterized in that, The organic phase includes an extractant and a diluent, wherein the volume of the extractant accounts for less than 60% of the volume of the organic phase, and the amount of the diluent added accounts for at least 40% of the volume of the organic phase.

5. The method according to claim 4, characterized in that, The extractant is one or more of TBP, P204, N235, P507, TOPO, and neodecanoic acid, and different extractants are combined in any proportion. The diluent is sulfonated kerosene or industrial kerosene.

6. The method according to claim 1, characterized in that, In step S3, the pH of the back-extraction aqueous phase is 5-10, wherein, The solution in the aqueous phase of the back-extraction is one or more of sodium hydroxide, potassium hydroxide, sodium carbonate, sodium bicarbonate, and pure water in any proportion.

7. The method according to claim 1, characterized in that, In step S4, the pH of the gallium-containing alkali solution is greater than 9.5, the electrolysis temperature is 25-75°C, and the current density is 100-2000 A / m. 2 .

8. The method according to claim 7, characterized in that, During the electrolysis process, the anode material is graphite, stainless steel, or platinum, lead, silver, titanium, tungsten or molybdenum metal or their alloys, and the cathode material is copper-indium alloy or indium-gallium alloy.

9. The method according to claim 7, characterized in that, In step S4, the gallium-containing precipitate is gallium hydroxide.

10. The method according to claim 1, characterized in that, The vanadium extraction converter sludge also includes the following components by mass: 0-2% SiO2, 1-5% ZnO, and the remainder being any combination of Na2O, MgO, CaCO3, Al2O3, TiO2, V2O5, Cr2O3, MnO, PbO, CuO, NiO, chlorides, and sulfides, with a total content of less than 10%.

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