A method of treating a lithium-containing glass

Abstract

The present application belongs to the field of solid waste resource processing, and relates to a treatment method of lithium-containing glass, comprising the following steps: S1, crushing the lithium-containing glass to be treated, adding a calcining agent, mixing and then calcining to obtain clinker; S2, crushing the clinker, mixing with a leaching solution, and then performing solid-liquid separation after reaction to obtain filter residue and filtrate; S3, removing impurities, concentrating and precipitating lithium from the filtrate; the calcining agent is composed of potassium salt and fluorine salt, the potassium salt is one or more of K2SO4, KF, KCl and KNO3, and the fluorine salt is one or more of NaF, KF, NH4F and hydroxy aluminum fluoride; the leaching solution is an Al 3+ -containing solution. The present application uses fluorine salt and potassium salt for calcining, achieves the purpose of extracting lithium through the embedding of potassium ions and the de-embedding of lithium ions, effectively utilizes the generated residue, and has high lithium extraction efficiency.

Description

Technical Field

[0001] The invention belongs to the field of solid waste resource treatment and relates to a method for treating lithium-containing glass. Background Art

[0002] Glass-ceramics typically consist of one or more crystalline phases embedded in a glass matrix. Among the various systems in the glass-ceramics family, Li2O-Al2O3-SiO2 (LAS) glass-ceramics is renowned for its exceptional thermal expansion properties, leading to its widespread research and application. Li2O-Al2O3-SiO2 (LAS) glass-ceramics primarily consists of oxides such as Al2O3, Na2O, MgO, K2O, and SiO2, with a Li2O content of approximately 10%. Compared to traditional lithium-containing mineral resources such as spodumene, lepidolite, petalite, and lithophane, LAS has a simpler composition, contains no toxic or difficult-to-separate elements, and is unreactive with acids or alkalis at room temperature. Efficiently recovering lithium from this type of lithium-containing glass waste and realizing its resource utilization would help alleviate the current shortage of lithium resources.

[0003] Chinese invention patent CN 118326174 A discloses a method for recovering lithium from lithium-containing glass powder. The method involves mixing the lithium-containing glass powder with an alkaline substance to produce a mixed material; calcining the mixed material at high temperature to produce a calcined material; and mixing the calcined material with an acid solution for acid leaching. After solid-liquid separation, a lithium-containing leachate is obtained. This patent utilizes alkali calcination to leach valuable lithium from the glass powder. However, the addition of acid during the leaching process may result in the formation of silica gel, making filtration and impurity separation difficult.

[0004] Chinese invention patent CN 117604271 A relates to a resource-based treatment method for lithium-containing glass waste, comprising the following steps: pre-treating the lithium-containing glass waste to be treated to obtain a powder; uniformly mixing the powder with a water-soluble fluoride salt and water to obtain a slurry; adding an inorganic acid to the slurry, and after the reaction is complete, performing solid-liquid separation to obtain a leachate and a leach residue; wherein, during the reaction, the pH value of the slurry is maintained at 0-4 by adding an inorganic acid; adjusting the pH value of the leachate to 5-8 with an alkali and / or alkaline solution, performing solid-liquid separation to obtain a purified liquid and a cryolite product; and subjecting the purified liquid to lithium precipitation treatment, performing solid-liquid separation to obtain a lithium compound product. However, in this prior art, a large amount of wastewater is generated during the acid leaching and alkali pH adjustment process. This wastewater needs to be effectively treated, otherwise it may pollute the water environment, and the subsequent treatment work is large.

[0005] Chinese invention patent CN 118360497 A discloses a method for extracting lithium from spodumene or petalite. The method involves ball mixing the spodumene or petalite with a reconstitution agent to obtain a mixture; calcining the mixture at 500-1000°C for 0.5-10 hours and then ball milling it to obtain a calcined material; mixing the calcined material with water or acid and leaching it for 0.5-10 hours, followed by solid-liquid separation to obtain a leachate and a leached residue. This invention patent utilizes a method of leaching valuable lithium from spodumene or petalite using fluoride salts and sulfates followed by water leaching. However, the formation of LiF in the leached product results in a low leaching rate, with lithium being wasted in the slag phase.

[0006] Chinese invention patent CN 117448593 A relates to a method for recovering lithium from lithium-containing waste materials. The method comprises the following steps: mixing the lithium-containing waste materials with a roasting additive, then aerobically roasting the resulting mixed powder; leaching the aerobically roasted powder, separating the solid and liquid to obtain a lithium-containing solution; purifying the resulting lithium-containing solution to remove impurities, and then preparing a lithium salt; the roasting additive comprises an alkali metal oxide and / or an alkali metal fluoride. However, during impurity removal in this prior art, aluminum ions are precipitated as aluminum hydroxide, and the aluminum hydroxide adsorbs lithium, resulting in a waste of lithium resources. Summary of the Invention

[0007] The object of the present invention is to provide a method for treating lithium-containing glass to improve the lithium extraction effect of the lithium-containing glass.

[0008] In order to achieve the above object, the present invention adopts the following technical solutions:

[0009] A method for treating lithium-containing glass comprises the following steps:

[0010] S1, crushing the lithium-containing glass to be processed, adding a roasting agent, mixing and roasting to obtain clinker;

[0011] S2, crushing the clinker and mixing it with the dissolution solution, and performing solid-liquid separation after the reaction to obtain a filter residue and a filtrate;

[0012] S3, removing impurities, concentrating and precipitating lithium from the filtrate;

[0013] The calcining agent is composed of a potassium salt and a fluoride salt, wherein the potassium salt is one or more of K2SO4, KF, KCl, and KNO3, and the fluoride salt is one or more of NaF, KF, NH4F, and hydroxyaluminum fluoride;

[0014] The dissolving solution contains Al 3+ of solution.

[0015] In one preferred embodiment, the lithium-containing glass comes from one or more of waste electronic product covers, display screens, and defective products and tailings in the deep processing of lithium-containing glass.

[0016] In one preferred embodiment, the lithium-containing glass includes Al2O3, Li2O and SiO2.

[0017] In one preferred embodiment, the lithium-containing glass includes, by weight, 5-15 parts of Li2O, 39.5-73.0 parts of SiO2, 0.8-30.0 parts of Al2O3, 0-3.0 parts of MgO, 0-2.0 parts of Na2O, 0.1-0.50 parts of CaO, 0-0.5 parts of K2O, and 0-2.0 parts of B2O.

[0018] In one preferred embodiment, in S1, the lithium-containing glass is crushed to a particle size of less than 100 mesh, preferably less than 150 mesh.

[0019] In one preferred embodiment, the mass ratio of the sintering agent to the lithium-containing glass is 0.5-2:1, for example, 1.2:1 or 1.8:1.

[0020] In one preferred embodiment, the mass ratio of the fluoride salt to the lithium-containing glass is not less than 0.2:1, and the mass ratio of the potassium salt to the lithium-containing glass is not less than 0.3.

[0021] A low fluorine content will result in insufficient destruction of the Si-O structure that locks lithium ions, making it difficult to deintercalate and deintercalate lithium ions, reducing the leaching rate. A high fluorine content will severely damage the glass structure, causing a large amount of silicon to enter the solution, forming silica gel during the leaching process and making filtration difficult. Potassium salts primarily play a replacement role, so if the amount of potassium salt is small, the lithium leaching rate will also be low. Too high a potassium salt content will form a glassy state, making it difficult to deintercalate and reducing the leaching rate.

[0022] In one preferred embodiment, in S1, the calcination temperature is 500°C-1000°C, more preferably 700°C-800°C; and the calcination time is 4-8 hours.

[0023] In one preferred embodiment, in S2, the liquid-to-solid ratio of the dissolution liquid to the clinker is 5-20 ml:1 g, preferably 8-15 ml:1 g.

[0024] In one preferred embodiment, in S2, the Al in the dissolution solution 3+ The mass ratio of the raw material to the clinker is 1-4:25, more preferably 2-3:25.

[0025] If the amount of aluminum ions is too small, part of the lithium fluoride will still exist in the solid phase in the slag, resulting in lithium waste; if the amount is too much, the impurity removal process will be too long.

[0026] In one preferred embodiment, in S2, the anions in the dissolution solution include Cl - 、SO4 2- 、NO3 - One or more of the .

[0027] In one preferred embodiment, in S2, the eluent is one or more of Al2(SO4)3, AlCl3, Al(NO3)3, and Al2(SO4)3·18H2O.

[0028] In one preferred embodiment, in S2, the reaction temperature is 70-95°C, preferably 90-95°C; and the reaction time is 1-2h.

[0029] In one preferred embodiment, in S3, impurity removal includes three stages of reaction: the first stage of reaction removes aluminum and fluorine; the second stage of reaction removes fluorine; and the third stage of reaction removes calcium.

[0030] In one preferred embodiment, the first stage reaction is: adjusting the pH of the filtrate to 5-7, preferably 6-6.5, and performing solid-liquid separation after the reaction to obtain filter residue C and filtrate D; the reaction temperature is 80-95°C.

[0031] In a preferred embodiment, one or both of KOH and NaOH are used to adjust the pH of the filtrate to 5-7.

[0032] The main components of the residue C are aluminum hydroxyfluoride and aluminum hydroxide, and aluminum and fluorine are removed by adjusting the pH.

[0033] In one preferred embodiment, the filter residue C is returned as a roasting agent.

[0034] In one preferred embodiment, the second stage reaction is: adding calcium ions to the filtrate D, performing solid-liquid separation after the reaction, and obtaining filter residue E and filtrate F.

[0035] By adding calcium ions to filtrate D, the F in filtrate F - The concentration was reduced to below 50 ppm.

[0036] In one preferred embodiment, the calcium ions are derived from any one or more of Ca(OH)2, calcium oxide or calcium chloride.

[0037] In one preferred embodiment, the third stage reaction is: adding Na2CO3 or sodium bicarbonate to the filtrate F, performing solid-liquid separation after the reaction, and obtaining filter residue G and filtrate H by solid-liquid separation, and concentrating the filtrate H to precipitate lithium.

[0038] The method of concentrating the precipitated lithium is a common method in the art and will not be described in detail in the present invention.

[0039] By adding Na2CO3 to the filtrate F, the Ca 2+ The concentration dropped to below 10 ppm.

[0040] In one preferred embodiment, the method for treating lithium-containing glass further comprises: washing the filter residue, filter residue C, filter residue E, and filter residue G with water, and returning the washing liquid after washing to prepare the dissolution solution.

[0041] The present invention combines lithium-containing waste glass with a calcining agent containing potassium and fluoride salts and calcines it. Fluoride ions destroy the Si-O structure, allowing potassium ions to intercalate and lithium ions to leach into a soluble phase. The reaction equation to be generated is as follows:

[0042] F - +LiAlSi4O 10 →LiF+AlSi3O8 - +SiO2;

[0043] K + +AlSi3O8 - →KAlSi3O8.

[0044] Based on the combined effect of the two, the efficiency of lithium extraction is improved.

[0045] The filter residue obtained by the present invention can be used as an additive for ceramic materials after washing, drying and grinding; the filter residue C is returned for roasting, and the lithium adsorbed in the precipitation process enters the soluble phase again, and the water washing liquid of all the filter residues can be returned for the dissolution process, which can effectively reduce the loss of lithium, and the repeated use of fluorine in the entire circulation process can reduce the processing cost.

[0046] Compared with the prior art, the present invention has the following beneficial effects:

[0047] (1) When the pH is adjusted, aluminum and fluorine are precipitated in the form of hydroxyaluminum fluoride. The obtained hydroxyaluminum fluoride can be returned as a calcining agent. The lithium loss it carries is dissolved during calcination and re-enters the liquid phase, which can effectively reduce the loss of lithium and realize the recycling of fluorine, thereby reducing the processing cost. The leached product does not contain LiF, and the leaching rate is high.

[0048] (2) The entire process of the present invention adopts fluoride salt and potassium salt roasting to achieve the purpose of lithium extraction through the embedding of potassium ions and the deintercalation of lithium ions. All water washing liquid can be returned to construct the dissolution liquid, effectively reducing the loss of lithium. More importantly, the slag generated in the lithium extraction process can be converted into valuable products, realizing the comprehensive recycling of lithium-containing waste glass, and providing a valuable reference for the effective recycling of lithium resources. BRIEF DESCRIPTION OF THE DRAWINGS

[0049] Figure 1 The present invention is a flow chart of a method for processing lithium-containing glass. DETAILED DESCRIPTION

[0050] The present invention is not limited to the following specific embodiments. Based on the disclosure of the present invention, a person skilled in the art may adopt a variety of other specific embodiments to implement the present invention. Any simple changes or modifications made to the design structure and concept of the present invention fall within the scope of protection of the present invention. It should be noted that the embodiments and features of the embodiments of the present invention may be combined with each other unless they conflict.

[0051] 100 g of lithium-containing waste glass from a panel factory was taken, and the composition (mass fraction wt%) is shown in Table 1 below.

[0052] Table 1 Composition of lithium-containing glass

[0053] serial number <![CDATA[Li2O]]> <![CDATA[Na2O]]> <![CDATA[K2O]]> CaO MgO <![CDATA[Al2O3]]> <![CDATA[B2O]]> <![CDATA[SiO2]]> 1 10.4464 0.9847 0.1885 0.3370 0.9568 14.2913 0.9656 68.5411 2 9.9236 1.1610 0.2279 0.3770 1.0872 15.1655 0.9981 66.1832

[0054] Example 1

[0055] according to Figure 1 The flowchart shown is used to process lithium-containing waste glass from a panel factory. The details are as follows:

[0056] (1) Lithium-containing waste glass from a panel factory was crushed to obtain glass powder with a particle size of less than 150 mesh, and the composition was No. 1 as shown in Table 1;

[0057] (2) The glass powder, potassium sulfate, and sodium fluoride were placed in a ball mill at a mass ratio of 1:0.45:0.25 and ball-milled to obtain a mixture.

[0058] (3) The mixed material is placed in a pit furnace and roasted at 700°C for 5 hours. After cooling, it is ball-milled and passed through a 150-mesh sieve to obtain roasted clinker.

[0059] (4) 60 g of calcined clinker was mixed with a dissolution solution. The mass ratio of Al2(SO4)3·18H2O in the clinker and dissolution solution was 1:1, and the liquid-to-solid ratio of the dissolution solution to the clinker was 5 ml:1 g. The reaction temperature was controlled at 90°C, and the leaching was carried out for 1 h. After solid-liquid separation, 300 ml of leachate and leached residue were obtained. The leached residue was washed once with water. The solid-to-liquid ratio of the leached residue to the washing water was 3 ml:1 g, and 50.08 g of washed residue was obtained. The lithium content in the washed residue was tested to be 0.1361%, and the estimated lithium leaching rate was 95.78%.

[0060] (5) Add 2 mol / L NaOH to the leachate at a rate of 1 ml / min, control the reaction temperature to 90°C, adjust the pH of the solution to 6.23, and perform solid-liquid separation to obtain residue C and filtrate D. The obtained residue C is returned to step (3) as a roasting agent. Add 5 g Ca(OH)2 to the filtrate D and react for 30 minutes. After 30 minutes of reaction, solid-liquid separation is performed to obtain residue E and filtrate F. The test results show that the concentration of Al in the filtrate F is 6 ppm, the concentration of F is 48 ppm, and the concentration of Li is 2.5 g / L. Add 10% excess Na2CO3 to the solution and react for solid-liquid separation. The solid-liquid separation obtains residue G and filtrate H. The Ca(OH)2 in the filtrate H is 0. 2+ The concentration is reduced to 7 ppm, and the filtrate H can be used for subsequent lithium concentration and precipitation operations, and the slag produced during the aluminum removal process is returned as a roasting agent.

[0061] After the filter residues C, E, and G are washed with water, the solid and liquid are separated to obtain washed residues and washing liquid. The washing liquid and the washing liquid of step (4) are returned to step (4) together to form an eluate.

[0062] Example 2

[0063] Example 1 was repeated, except that the mass ratio of glass powder, potassium sulfate, and sodium fluoride was adjusted to 1:0.3:0.25. The balanced lithium leaching rate was 93.66%.

[0064] Example 3

[0065] Example 1 was repeated, except that the mass ratio of glass powder, potassium sulfate, and sodium fluoride was adjusted to 1:0.6:0.25, and the balanced lithium leaching rate was 94.30%.

[0066] Comparative Example 1

[0067] Example 1 was repeated, except that the mass ratio of glass powder, potassium sulfate, and sodium fluoride was adjusted to 1:0.45:0.1, and the balanced lithium leaching rate was 50.38%.

[0068] Comparative Example 2

[0069] Example 1 was repeated, except that the mass ratio of glass powder, potassium sulfate, and sodium fluoride was adjusted to 1:0.18:0.25, and the balanced lithium leaching rate was 77.81%.

[0070] Comparative Example 3

[0071] Lithium-containing waste glass from a panel manufacturer was crushed to obtain glass powder with a particle size below 150 mesh. A certain amount of glass powder was ball-milled with potassium sulfate in a mass ratio of 1:0.3 in a ball mill to obtain a mixture. The mixture was then calcined at 750°C in a pit furnace for 5 hours. After cooling, it was ball-milled and passed through a 150-mesh sieve to obtain calcined clinker. 60g of the calcined clinker was mixed with a solution containing a 1:1 mass ratio of Al2(SO4)3·18H2O in the clinker to the solution, and a liquid-to-solid ratio of 10ml:1g of the solution to the clinker. The reaction temperature was controlled at 90°C, the solution was kept warm for 1 hour, and solid-liquid separation was performed. The estimated lithium leaching yield was 37.77%.

[0072] Example 4

[0073] Lithium-containing waste glass from a panel factory was crushed to obtain glass powder with a particle size of less than 150 mesh; the composition was as shown in Table 1, No. 2. The glass powder was ball-milled with potassium chloride and sodium fluoride in a mass ratio of 1:0.3:0.4 in a ball mill to obtain a mixture. The mixture was then calcined at 750°C in a pit furnace for 5 hours. After cooling, the mixture was ball-milled and passed through a 150-mesh sieve to obtain a calcined clinker. 60g of the calcined clinker was mixed with an eluate solution. The mass ratio of Al2(SO4)3·18H2O in the clinker to the eluate solution was 1:1, and the liquid-to-solid ratio of the eluate to the clinker was 10ml:1g. The reaction temperature was controlled at 90°C, the leaching was maintained at this temperature for 1 hour, and solid-liquid separation was performed. The estimated lithium leaching rate was 98.92%. Other modifications were the same as in Example 1.

[0074] Example 5

[0075] Lithium-containing waste glass from a panel factory was crushed to obtain glass powder with a particle size of less than 150 mesh. The glass powder was ball-milled with potassium fluoride and sodium fluoride in a mass ratio of 1:0.4:0.4 in a ball mill to obtain a mixture. The mixture was then calcined at 750°C in a pit furnace for 5 hours. After cooling, the mixture was ball-milled and passed through a 150-mesh sieve to obtain a calcined clinker. 60g of the calcined clinker was mixed with a solution. The mass ratio of Al2(SO4)3·18H2O in the solution was 1:1, and the liquid-to-solid ratio of the solution to the clinker was 15ml:1g. The reaction temperature was controlled at 95°C, the solution was kept warm for 1 hour, and solid-liquid separation was performed. The estimated lithium leaching yield was 97.63%. Other modifications were the same as in Example 1.

[0076] Example 6

[0077] Lithium-containing waste glass from a panel manufacturer was crushed to obtain glass powder with a particle size of less than 150 mesh. The glass powder was ball-milled with potassium fluoride in a mass ratio of 1:0.3 in a ball mill to obtain a mixture. The mixture was then calcined at 750°C in a pit furnace for 5 hours. After cooling, the mixture was ball-milled and passed through a 150-mesh sieve to obtain a calcined clinker. 60g of the calcined clinker was mixed with a solution, with a mass ratio of Al2(SO4)3·18H2O between the clinker and the solution being 1:1, and a liquid-to-solid ratio of 20ml:1g of the solution to the clinker. The reaction temperature was controlled at 90°C, the solution was kept warm for 1 hour, and solid-liquid separation was performed. The estimated lithium leaching yield was 91.12%. Other modifications were the same as in Example 1.

[0078] Comparative Example 4

[0079] Lithium-containing waste glass from a panel factory was crushed to obtain glass powder with a particle size of less than 150 mesh. The glass powder was ball-milled with potassium chloride in a mass ratio of 1:0.3 in a ball mill to obtain a mixture. The mixture was then calcined at 750°C in a pit furnace for 5 hours. After cooling, the mixture was ball-milled and passed through a 150-mesh sieve to obtain a calcined clinker. 60g of the calcined clinker was mixed with a dissolution solution. The mass ratio of Al2(SO4)3·18H2O in the clinker to the dissolution solution was 1:1, and the liquid-to-solid ratio of the dissolution solution to the clinker was 10ml:1g. The reaction temperature was controlled at 90°C, the leaching was maintained at this temperature for 1 hour, and solid-liquid separation was performed. The estimated lithium leaching yield was 48.55%. Other modifications were the same as in Example 4.

[0080] Comparative Example 5

[0081] Lithium-containing waste glass from a panel factory was crushed to obtain glass powder with a particle size of less than 150 mesh. A certain amount of glass powder was ball-milled with sodium fluoride in a mass ratio of 1:0.4 in a ball mill to obtain a mixture. The mixture was then calcined at 750°C in a pit furnace for 5 hours. After cooling, the mixture was ball-milled and passed through a 150-mesh sieve to obtain calcined clinker. 60g of the calcined clinker was mixed with a dissolution solution. The mass ratio of Al2(SO4)3·18H2O in the clinker to the dissolution solution was 1:1, and the liquid-to-solid ratio of the dissolution solution to the clinker was 10ml:1g. The reaction temperature was controlled at 90°C, the leaching was maintained at this temperature for 1 hour, and solid-liquid separation was performed. The estimated lithium leaching yield was 80.07%. Other aspects were the same as in Example 4.

[0082] Comparative Example 6

[0083] Lithium-containing waste glass from a panel manufacturer was crushed to obtain glass powder with a particle size of less than 150 mesh. A certain amount of the glass powder was ball-milled with sodium sulfate and sodium fluoride in a mass ratio of 1:0.3:0.4 to obtain a mixture. The mixture was then calcined in a pit furnace at 750°C for 5 hours. After cooling, the mixture was ball-milled and passed through a 150-mesh sieve to obtain a calcined clinker. Other conditions were the same as in Example 4. The calculated lithium leaching rate was 75.25%.

[0084] By comparison, it can be seen that the lithium leaching rate of glass calcined with potassium salt alone is low, and more lithium remains in the slag phase when calcined with fluoride salt alone. Potassium fluoride is relatively effective because it has the effects of both fluoride ions and potassium ions, but the cost of using potassium fluoride is relatively expensive and there must be an excess of one of the potassium ions or fluoride ions, resulting in waste. After the fluoride ions destroy the Si-O structure, the replacement effect of sodium ions is very poor, and the effect on the lithium leaching rate is very small. Under the same conditions, potassium ions have a significant improvement in the lithium leaching rate, which is close to complete leaching. In order to maximize the lithium leaching rate, the use of a mixed fluoride salt and potassium salt for calcination can effectively achieve this goal, and it can maximize the atomic utilization rate and thus reduce costs.

[0085] It should be noted that the above embodiments are merely examples for the purpose of clearly illustrating the present invention and are not intended to limit the embodiments of the present invention. A person skilled in the art would be able to make other variations or modifications based on the above description. It is not possible to enumerate all embodiments here. Any obvious variations or modifications arising from the technical solution of the present invention remain within the scope of protection of the present invention.

Claims

1. A method for treating lithium-containing glass, characterized in that: The steps include: S1, crushing the lithium-containing glass to be processed, adding a roasting agent, mixing and roasting to obtain clinker; S2, crushing the clinker and mixing it with the dissolution solution, and performing solid-liquid separation after the reaction to obtain a filter residue and a filtrate; S3, removing impurities, concentrating and precipitating lithium from the filtrate; The calcining agent is composed of a potassium salt and a fluoride salt, wherein the potassium salt is one or more of K2SO4, KCl, and KNO3, and the fluoride salt is one or more of NaF, NH4F, and hydroxyaluminum fluoride; The dissolving solution contains Al 3+ of solution; The mass ratio of the calcining agent to the lithium-containing glass is 0.5-2:1; The mass ratio of fluoride salt to lithium-containing glass shall not be less than 0.2:1, and the mass ratio of potassium salt to lithium-containing glass shall not be less than 0.

3.

2. The processing method according to claim 1, characterized in that The lithium-containing glass includes Al2O3, Li2O and SiO2.

3. The processing method according to claim 1, characterized in that In S1, the calcination temperature is 500° C.-1000° C., and the calcination time is 4-8 hours.

4. The processing method according to claim 1, characterized in that In S2, the liquid-solid ratio of the dissolution liquid to the clinker is 5-20ml:1g; the Al in the dissolution liquid 3+ The mass ratio of crude oil to clinker is 1-4:

25.

5. The processing method according to claim 1, characterized in that In S2, the eluent is one or more of Al2(SO4)3, AlCl3, Al(NO3)3, and Al2(SO4)3·18H2O.

6. The processing method according to claim 1, characterized in that In S2, the reaction temperature is 70-95°C and the reaction time is 1-2h.

7. The processing method according to any one of claims 1 to 6, characterized in that: In S3, impurity removal includes three reactions: the first reaction removes aluminum and fluorine, the second reaction removes fluorine, and the third reaction removes calcium.

8. The processing method according to claim 7, characterized in that: The first stage of the reaction is: adjusting the pH of the filtrate to 5-7, and performing solid-liquid separation after the reaction to obtain filter residue C and filtrate D; the second stage of the reaction is: adding calcium ions to the filtrate D, and performing solid-liquid separation after the reaction to obtain filter residue E and filtrate F; the third stage of the reaction is: adding Na2CO3 or sodium bicarbonate to the filtrate F, and performing solid-liquid separation after the reaction to obtain filter residue G and filtrate H, and the filtrate H is concentrated to precipitate lithium.

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