Method for removing lead from calcified acid leaching vanadium liquid

Abstract

The invention relates to the technical field of vanadium-lead separation, and discloses a lead removal method for calcified acid leaching vanadium liquid, which comprises the following steps: S1, mixing water-soluble sulfide salt and a slow-release agent according to a certain proportion, and replenishing water to prepare a granular lead removal agent; s2, drying the lead removal agent to obtain a granular lead removal agent finished product with a certain size; s3, a lead removal agent finished product is added into the calcified acid vanadium leaching qualified liquid, so that lead in the qualified liquid is subjected to a precipitation reaction; s4, after the reaction is finished, carrying out solid-liquid separation on the qualified liquid to obtain purified qualified liquid; and S5, carrying out vanadium precipitation and drying on the purified qualified liquid to prepare a low-lead APV product. The method is easy to operate, low in cost and high in efficiency, lead ions in the solution can be effectively removed, and the product vanadium pentoxide with the lead content smaller than 0.01% is prepared.

Description

Technical Field

[0001] The invention relates to the technical field of vanadium slag roasting, in particular to a method for removing lead from calcified acid leaching vanadium liquid. Background Art

[0002] As an important strategic element, vanadium is widely used in metallurgy, chemical industry, aerospace and other fields. It can significantly improve the strength, toughness and ductility of steel, and provide important support for ensuring the quality of key national projects. my country is rich in vanadium-titanium magnetite resources. Usually, the iron concentrate blast furnace ironmaking-converter vanadium extraction process is used to obtain vanadium slag. The sodium vanadium extraction and calcification vanadium extraction processes are widely used in production. Panzhihua Iron and Steel uses the vanadium slag calcification vanadium extraction process to prepare vanadium oxide. The process steps of vanadium slag calcification vanadium extraction mainly include calcium salt roasting, acid leaching, impurity removal, vanadium precipitation, melting / reduction and other processes. Among them, roasting-acid leaching is the key step affecting the entire vanadium oxide yield. In order to maximize the leaching effect of vanadium in roasted clinker, the current method of one acid leaching of clinker + two deep acid leaching of tailings is adopted, and the pH value of deep leaching is low (~1.0). Deep leaching under such strong acidic conditions can leach part of the Pb in the material into the solution. Under subsequent solution circulation, the Pb concentration in the leached vanadium solution gradually increases. At present, the qualified solution of Xichang Vanadium Products Factory contains about 0.012g / L of Pb, resulting in the Pb content in the precipitated APV reaching 0.02%, which cannot meet the quality requirements of high-end application fields such as vanadium batteries (Pb < 0.01%).

[0003] Both Russia and my country's Panzhihua Iron and Steel have layouts in the field of calcium-based vanadium extraction, but the current national standard "GB 3283-1987 Vanadium Pentoxide Standard" does not have clear requirements for Pb. The APV produced by calcium-based vanadium extraction and provided as vanadium material for vanadium batteries is an original creation of Panzhihua Iron and Steel. There is still a gap in the research on Pb removal from qualified liquid containing 0.3 to 0.6 mol / L vanadium at home and abroad.

[0004] Patent document CN118147018A discloses a Citrobacter freundii with lead adsorption ability and its extracellular polymers and applications. It relates to the field of microbial lead removal, and utilizes the high tolerance and adsorption rate of Citrobacter freundii FCHC PbA1 and its extracellular polymers to lead, which has broad application prospects in adsorbing and removing lead. However, CN118147018A uses Citrobacter freundii to remove lead, which requires strict control of treatment conditions such as temperature, pH value, nutrients, etc. The control of these conditions may increase the treatment cost, and Citrobacter freundii has a certain adaptability range to the pH value of the environment, and its lead removal effect may be greatly affected under strong acidic conditions.

[0005] Patent document CN118637764A discloses a method for treating thallium-containing industrial wastewater. The specific steps include: S1, primary treatment: add sulfuric acid to the thallium-containing industrial wastewater, adjust the pH to 1.5-2.5, add hydrogen peroxide, adjust the potential to 450-550mV, maintain at a temperature of 20-30°C for 20-40min, add water glass solution for miscibility, then add composite alkali, adjust the pH to 4.5-5.5, filter press, and obtain the first section of waste residue and the first section of wastewater; S2, secondary treatment: repeat the operation of the primary treatment on the first section of wastewater, filter press, and obtain the second section of waste residue and the second section of wastewater; S3, tertiary treatment: continue to add composite alkali to the second section of wastewater, adjust the pH to 7.0-9.0, filter press, and obtain the third section of waste residue and the third section of wastewater, settle the third section of wastewater, filter press again, obtain the discharged water, combine the three sections of waste residue, and centrally treat. It uses the principle of atomic radius co-precipitation to remove lead and thallium at the same time, with simple steps, low cost, stable effect, and the treated water sample meets the discharge standard, which has practical application value. However, the environment required in CN118637764A does not involve calcified acid leaching vanadium solution under strong acidic conditions, and does not achieve the use of the solution after lead removal to obtain APV.

[0006] Patent document CN118164575A discloses a method for enhancing the adsorption of lead ions by nano-silica gel using anionic surfactants. By controlling the relative amount of the reserve solution, the acid-modified silica gel and the anionic surfactant, the efficient adsorption of lead ions is achieved, and the efficient removal of lead ions is achieved by flotation process. The process is simple, the cost is low, it is suitable for industrial production, and the industrial application prospect is broad. CN118164575A is used for efficient removal of lead ions in a neutral or weakly alkaline environment, while the calcified acid leaching vanadium solution belongs to acidic conditions.

[0007] Therefore, there is a need in the prior art to remove Pb from the calcified acid leaching vanadium solution in order to obtain an APV product whose Pb content meets the requirements of vanadium raw materials for vanadium batteries. Summary of the invention

[0008] In view of this, the purpose of the embodiment of the present invention is to provide a method for removing lead from a calcified acid leaching vanadium solution. The method is simple to operate, low in cost, and high in efficiency. It can effectively remove lead ions in the solution and prepare a product vanadium pentoxide with a lead content of less than 0.01%.

[0009] Based on the above purpose, an embodiment of the present invention provides a method for removing lead from a calcified acid leaching vanadium solution, comprising: S1 mixes water-soluble sulfide salt and slow-release agent in a certain proportion, and then adds water to prepare a granular lead remover; S2 drying the lead remover to obtain a granular lead remover finished product of a certain size; S3 adding the finished lead removal agent to the qualified solution of vanadium leaching by calcification acid to cause the lead in the qualified solution to precipitate; After the reaction in step S4 is completed, the qualified liquid is subjected to solid-liquid separation to obtain a purified qualified liquid; S5: precipitating vanadium and drying the purified qualified liquid to prepare a low-lead APV product.

[0010] According to one embodiment of the present invention, in step S1, the water-soluble sulfide salt includes barium sulfide and sodium sulfide.

[0011] According to one embodiment of the present invention, in step S1, the water replenishment ratio is controlled according to a mass ratio of liquid to solid of 10% to 40%.

[0012] According to one embodiment of the present invention, in step S2, the certain size is a size that passes through a sieve with an aperture of 10 mm and remains on a sieve with a 20-mesh aperture.

[0013] According to an embodiment of the present invention, in step S2, the drying temperature is 50-250°C.

[0014] According to one embodiment of the present invention, in step S3, the amount of the lead removal agent product added is to completely precipitate the Pb in the qualified solution. 2+ Required S 2- 3~10 times of the theoretical amount.

[0015] According to one embodiment of the present invention, in step S3, the precipitation reaction is carried out under stirring for a reaction time of more than 30 minutes.

[0016] According to one embodiment of the present invention, in step S4, the solid-liquid separation includes separation by filtering equipment or natural sedimentation separation.

[0017] According to an embodiment of the present invention, in step S1, the certain ratio is (1:9) to (9:1).

[0018] According to one embodiment of the present invention, in step S5, the lead content in the low-lead APV product is less than 0.01%.

[0019] The present invention has at least the following beneficial technical effects: The invention uses soluble sulfide as the raw material of the lead remover, adopts a slow-release agent to passivate and encapsulate the sulfide to form a special lead remover for calcified acid leaching vanadium solution, after the sulfide in the lead remover is slowly dissolved in the calcified acid leaching vanadium solution after being encapsulated by the slow-release agent, it combines with the lead ions in the calcified acid leaching vanadium solution to precipitate the lead ions, thereby achieving lead removal from the calcified acid leaching vanadium solution; at the same time, the lead remover obtained after the slow-release agent passivation treatment combines the soluble metal sulfide with V 5+The reaction model is transformed from a liquid-liquid reaction model to a solid-liquid reaction model, which effectively avoids the problem of a large amount of sulfur ions being oxidized to elemental sulfur and losing the lead removal ability. The lead ions in the calcified acid leaching vanadium solution are effectively removed. The vanadium solution after lead removal is helpful for the subsequent preparation of low-lead APV products that meet the requirements of vanadium batteries. The vanadium-lead separation efficiency is high, and no other impurities are introduced to ensure the quality of subsequent vanadium products. It is also simple to operate and requires little equipment. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings in the following description are only some embodiments of the present invention. For ordinary technicians in this field, other embodiments can be obtained based on these drawings without paying creative work.

[0021] Figure 1 A flow chart of an embodiment of a method for removing lead from a calcified acid leaching vanadium solution provided by the present invention; Figure 2 A flow chart for preparing the lead removal agent for acid leaching vanadium solution provided by the present invention; Figure 3 The present invention provides a flow chart for removing lead from qualified liquid. DETAILED DESCRIPTION

[0022] In order to make the objectives, technical solutions and advantages of the present invention more clearly understood, the embodiments of the present invention are further described in detail below in combination with specific embodiments and with reference to the accompanying drawings.

[0023] The terms "including" and "having" and any variations thereof in the specification and claims of the present invention and the above-mentioned drawings are intended to cover non-exclusive inclusions; the terms "first", "second", etc. in the specification and claims of the present invention or the above-mentioned drawings are used to distinguish different objects rather than to describe a specific order. "Multiple" means two or more, unless otherwise clearly and specifically defined.

[0024] In addition, reference to "embodiments" herein means that a particular feature, structure, or characteristic described in conjunction with the embodiments may be included in at least one embodiment of the present invention. The appearance of the phrase in various places in the specification does not necessarily refer to the same embodiment, nor is it an independent or alternative embodiment that is mutually exclusive with other embodiments. It is explicitly and implicitly understood by those skilled in the art that the embodiments described herein may be combined with other embodiments.

[0025] like Figure 1 The present invention provides a method for removing lead from a calcified acid leaching vanadium solution, comprising the following steps: S1 mixes water-soluble sulfide salt and slow-release agent in a certain proportion, and then adds water to prepare a granular lead remover; S2 dries the lead remover to obtain a granular lead remover finished product of a certain size; S3 adding the finished lead removal agent to the qualified solution of vanadium leaching by calcification acid to cause the lead in the qualified solution to precipitate; After the reaction in S4 is completed, the qualified liquid is subjected to solid-liquid separation to obtain a purified qualified liquid; S5 precipitates vanadium and dries the purified qualified liquid to prepare a low-lead APV product.

[0026] Furthermore, in step S1, the water-soluble sulfide salt includes barium sulfide and sodium sulfide.

[0027] Furthermore, in step S1, the water replenishment ratio is controlled according to a mass ratio of liquid to solid of 10% to 40%.

[0028] Further, in step S2, the certain size is a size that passes through a 10 mm pore size sieve while remaining on a 20 mesh sieve.

[0029] Furthermore, in step S2, the drying temperature is 50-250°C.

[0030] Further, in step S3, the amount of lead removal agent added is sufficient to completely precipitate Pb in the qualified solution. 2+ Required S 2- 3~10 times of the theoretical amount.

[0031] Furthermore, in step S3, the precipitation reaction is carried out under stirring for a reaction time of more than 30 minutes.

[0032] Further, in step S4, the solid-liquid separation includes separation by filtering equipment or natural sedimentation separation.

[0033] Further, in step S1, the certain ratio is (1:9) to (9:1).

[0034] Further, in step S5, the lead content in the low-lead APV product is less than 0.01%.

[0035] In some embodiments, the lead removal agent product preparation process and the lead removal process of the calcified acid leaching vanadium solution are respectively as follows: Figure 2 and Figure 3 As shown. Water-soluble sulfide is used as the raw material of lead remover, and slow-release agent is used to passivate and encapsulate the sulfide to form a special lead remover for acidic vanadium solution. Water-soluble sulfide salts include barium sulfide, sodium sulfide, etc. The slow-release agent does not react with the V in the qualified solution. 5+Reaction, insoluble in acid qualified liquid. Weigh a certain amount of water-soluble sulfide salt and slow-release agent and mix them in a ratio of (1:9) to (9:1). Add water to the mixed water-soluble sulfide and slow-release agent according to the mass ratio of liquid to solid of 10-40% to make a granular lead remover. There is no special requirement for the shape of the granular lead remover, and it can be granulated according to the existing granulation equipment. Then the granular lead remover is dried to obtain a granular lead remover product with suitable hardness. The size range of the lead remover finished product particles is that they can pass through a sieve with an aperture of 10 mm and remain above a 20-mesh sieve, that is, the diameter of the particles is greater than the mesh size of the 20-mesh sieve but not more than 10 mm. The temperature of drying the lead remover does not exceed 50-250°C. After drying, a granular lead remover product with suitable hardness is obtained. There is no requirement for the hardness of the lead remover finished product, and it can be packed without breaking. There is no requirement for the drying time, and the lead remover can be packed. Take a certain amount of calcified acid leaching vanadium liquid (the ingredients are shown in Table 1), add the finished lead removal agent, make the lead in the qualified liquid precipitate, and the reaction time is greater than 30 minutes under stirring conditions. There is no requirement for the standing time after the precipitation reaction, which is set according to the site conditions. After standing, the qualified liquid is separated into solid and liquid. There is no requirement for the method of solid-liquid separation. If conditions permit, solid-liquid separation can be carried out on filtering equipment such as plate and frame filters, or natural sedimentation separation can be carried out. If natural sedimentation separation is adopted, a filter screen needs to be set to separate the solid and liquid of the upper qualified liquid again. The vanadium precipitation step after obtaining the purified qualified liquid is consistent with the vanadium precipitation step of the ordinary qualified liquid, but it needs to be operated independently in the actual production process to prevent the ordinary qualified liquid without lead removal from contaminating the purified qualified liquid.

[0036] The composition of the qualified solution for calcified acid leaching of vanadium is shown in Table 1 below.

[0037] Table 1 Typical components of calcified acid leaching vanadium solution / g·L -1

[0038] In some embodiments, the production can be implemented in the following manner: First, add 3 to 10 times the amount of Pb 2+ The theoretical amount of lead sulfide precipitated 2- , and the stirring is completed when the pump is used to transport the liquid to the qualified liquid tank and the qualified liquid is pumped into the qualified liquid tank. The reactions involved in the whole process are: MS=M 2+ +S 2- (Formula 1) Pb 2+ +S 2- =PbS↓(Formula 2) 5S 2- +34H + +H2V 10 O 284- =10V 2+ +18H2O+5S↓(Formula 3) The present invention adds the lead remover to the acidic vanadium solution, and the sulfur ions are slowly released into the solution, and then the reactions in Formula 2 and Formula 3 occur. The sulfide in the lead remover is wrapped in the slow-release agent and slowly dissolved in the vanadium solution, which avoids the rapid release of sulfur ions in a local area and the rapid reaction in Formula 1. A small amount of sulfur ions in a local area form precipitation with lead ions, and the remaining part of the sulfur ions react with pentavalent vanadium to convert H2V 10 O 28 4- Restore to VO 2+ Through passivation treatment, water-soluble sulfides and V 5+ The reaction model is transformed from a liquid-liquid reaction model to a solid-liquid reaction model, effectively avoiding a large amount of S 2- Local advance and V 5+ The reaction generates VO 2+ , S 2- It is oxidized to elemental sulfur and loses its ability to combine with lead ions and precipitate, thus losing its lead removal ability. The finished lead remover is a product in which sulfur ions and V react evenly and slowly in the solution. 5+ , Pb 2+ reaction, although there will be S 2- With V 5+ The reaction reduces vanadium, but the lead removal agent of the present invention is used in trace amounts, with little vanadium loss. The vanadium liquid after lead removal is used to prepare low-lead APV products (lead < 0.01%) to meet the requirements of low-lead APV products for vanadium batteries, which has certain technical advantages. In addition, the selective precipitation process does not introduce other impurities, which will not affect the quality of subsequent vanadium products.

[0039] The present invention is further explained below in conjunction with specific embodiments and comparative examples.

[0040] Example 1 Measure 100g of barium sulfide (barium sulfide content 50%) and 100g of sustained-release agent, mix them evenly, spray 50ml of tap water, and use a small granulator to granulate; after granulation, bake at 100℃ for 3 hours, and after cooling, obtain 200.3g of lead remover and sieve (+40 mesh ~ -6mm sieve) to obtain lead remover. Take 1L of qualified calcified acid leaching vanadium solution in a beaker (containing Pb0.012g equivalent to: 5.79*10 - 5 mol), room temperature, stirring control 300r / min, add 0.3g lead remover (containing S 2- 0.014g is equivalent to: 44.3*10 -5 mol,S 2-:Pb=7.63mol:1mol), react for 2 hours, filter and obtain a purified liquid, the Pb content in the purified liquid is reduced from 0.012g / L to 0.0003g / L; The qualified liquid is precipitated with vanadium to obtain APV, which is dried. The Pb content in the APV is reduced from 0.02% to 0.005%, and an APV with a Pb content of less than 0.01% is obtained.

[0041] Example 2 Measure 100g of barium sulfide (barium sulfide content 50%) and 100g of sustained-release agent, mix them evenly, spray 50ml of tap water, and use a small granulator to granulate; after granulation, bake at 100℃ for 3 hours, and after cooling, obtain 200.3g of lead remover and sieve (+40 mesh ~ -6mm sieve) to obtain lead remover. Take 1L of qualified calcified acid leaching vanadium solution in a beaker (containing Pb0.012g equivalent to: 5.79*10 - 5 mol), room temperature, stirring control 300r / min, add 0.15g lead remover (containing S 2- 0.007g is equivalent to: 22.15*10 -5 mol,S 2- :Pb=3.81mol:1mol), react for 2 hours, filter and obtain purified liquid, the Pb content in the purified liquid is reduced from 0.012g / L to 0.0005g / L; The qualified liquid is precipitated with vanadium to obtain APV, which is dried. The Pb content in the APV is reduced from 0.02% to 0.009%, and an APV with a Pb content of less than 0.01% is obtained.

[0042] Example 3 Measure 100g sodium sulfide (sodium sulfide content 95%) and 100g slow-release agent, mix evenly, spray 50ml tap water, and use a small granulator to granulate; after granulation, bake at 100℃ for 3 hours, cool and obtain 200.21g lead remover, sieve (+40 mesh ~ -6mm sieve) to obtain lead remover. Take 1L qualified solution of calcified acid leaching vanadium solution in a beaker (containing Pb0.012g equivalent to: 5.79*10 - 5 mol), room temperature, stirring control 300r / min, add 0.06g lead remover (containing S 2- 0.012g is equivalent to: 36.5*10 -5 mol,S 2- :Pb=6.30mol:1mol), react for 2 hours, filter and obtain a purified liquid, the Pb content in the purified liquid is reduced from 0.012g / L to 0.0002g / L; The qualified solution is precipitated with vanadium to obtain APV, which is dried and the Pb content is reduced from 0.02% to 0.004%, obtaining an APV with a Pb content of less than 0.01%.

[0043] Example 4 Measure 100g sodium sulfide (sodium sulfide content 95%) and 100g slow-release agent, mix evenly, spray 50ml tap water, and use a small granulator to granulate; after granulation, bake at 100℃ for 3 hours, cool and obtain 200.21g lead remover, sieve (+40 mesh ~ -6mm sieve) to obtain lead remover. Take 1L qualified solution of calcified acid leaching vanadium solution in a beaker (containing Pb0.012g equivalent to: 5.79*10 - 5 mol), room temperature, stirring control 300r / min, add 0.03g lead remover (containing S 2- 0.006g is equivalent to: 18.3*10 -5 mol,S 2- :Pb=3.15mol:1mol), react for 2 hours, filter to obtain purified liquid, the Pb content in the purified liquid is reduced from 0.012g / L to 0.0005g / L; The qualified solution is precipitated with vanadium to obtain APV, which is dried and the Pb content is reduced from 0.02% to 0.008%, obtaining an APV with a Pb content of less than 0.01%.

[0044] Example 5 Measure 40ml of ammonia sulfide (ammonia sulfide content 25%) and 100g of sustained-release agent, mix them evenly, and use a small granulator to granulate; after granulation, bake at 60℃ for 12 hours, cool and obtain 110.3g of lead remover, sieve (+40 mesh ~ -6mm sieve) to obtain lead remover. Take 1L of qualified calcified acid leaching vanadium solution in a beaker (containing Pb0.012g equivalent to: 5.79*10 -5 mol), room temperature, stirring control 300r / min, add 0.44g lead remover (containing S 2- 0.0188g is equivalent to: 58.8*10 -5 mol,S 2- :Pb=10.16mol:1mol), react for 2 hours, filter; obtain purified liquid, the Pb content in the purified liquid is reduced from 0.012g / L to 0.0001g / L; The qualified solution is precipitated with vanadium to obtain APV, which is dried and the Pb content is reduced from 0.02% to 0.001%, thereby obtaining APV with a Pb content of less than 0.01%.

[0045] The above are exemplary embodiments disclosed in the present invention, but it should be noted that various changes and modifications may be made without departing from the scope disclosed in the embodiments of the present invention as defined in the claims. The functions, steps and / or actions of the method claims according to the disclosed embodiments described herein do not need to be performed in any particular order. In addition, although the elements disclosed in the embodiments of the present invention may be described or required in individual form, they may also be understood as multiple unless explicitly limited to the singular.

[0046] It should be understood that, as used herein, the singular forms "a", "an" are intended to include the plural forms as well, unless the context clearly supports an exception. It should also be understood that, as used herein, "and / or" refers to any and all possible combinations including one or more of the associated listed items.

[0047] The serial numbers of the embodiments disclosed in the above embodiments of the present invention are only for description and do not represent the advantages or disadvantages of the embodiments.

[0048] A person skilled in the art should understand that the discussion of any of the above embodiments is only exemplary and is not intended to imply that the scope of the disclosure of the embodiments of the present invention (including the claims) is limited to these examples; under the concept of the embodiments of the present invention, the technical features in the above embodiments or different embodiments can also be combined, and there are many other changes in different aspects of the above embodiments of the present invention, which are not provided in detail for the sake of simplicity. Therefore, any omissions, modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the embodiments of the present invention should be included in the protection scope of the embodiments of the present invention.

Claims

1. A method for removing lead from a calcified acid leaching vanadium solution, characterized in that: include: S1 mixes water-soluble sulfide salt and slow-release agent in a certain proportion, and then adds water to prepare a granular lead remover; S2 drying the lead remover to obtain a granular lead remover finished product of a certain size; S3 adding the finished lead removal agent to the qualified solution of vanadium leaching by calcification acid to cause the lead in the qualified solution to precipitate; After the reaction in step S4 is completed, the qualified liquid is subjected to solid-liquid separation to obtain a purified qualified liquid; S5: precipitating vanadium and drying the purified qualified liquid to prepare a low-lead APV product.

2. The lead removal method for calcified acid leaching vanadium solution according to claim 1, characterized in that: In step S1, the water-soluble sulfide salt includes barium sulfide and sodium sulfide.

3. The method for removing lead from calcified acid leaching vanadium solution according to claim 1, characterized in that: In step S1, the water replenishment ratio is controlled according to the mass ratio of liquid to solid being 10% to 40%.

4. The method for removing lead from calcified acid leaching vanadium solution according to claim 1, characterized in that: In step S2, the certain size is a size that passes through a 10 mm pore size sieve and remains on a 20 mesh sieve.

5. The method for removing lead from calcified acid leaching vanadium solution according to claim 1, characterized in that: In step S2, the drying temperature is 50-250°C.

6. The method for removing lead from calcified acid leaching vanadium solution according to claim 1, characterized in that: In step S3, the amount of the lead removal agent product added is sufficient to completely precipitate the Pb in the qualified solution. 2+ Required S 2- 3~10 times of the theoretical amount.

7. The method for removing lead from calcified acid leaching vanadium solution according to claim 1, characterized in that: In step S3, the precipitation reaction is carried out under stirring for a reaction time of more than 30 minutes.

8. The method for removing lead from calcified acid leaching vanadium solution according to claim 1, characterized in that: In step S4, the solid-liquid separation includes separation by filtering equipment or natural sedimentation separation.

9. The method for removing lead from calcified acid leaching vanadium solution according to claim 1, characterized in that: In step S1, the certain ratio is (1:9) to (9:1).

10. The method for removing lead from calcified acid leaching vanadium solution according to claim 1, characterized in that: In step S5, the lead content in the low-lead APV product is less than 0.01%.

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