Efficient treatment method of lithium concentrate and pretreatment method of lithium precipitation mother liquor

Abstract

The invention provides an efficient treatment method for lithium concentrate and a pretreatment method for lithium precipitation mother liquor. The pretreatment method of the lithium precipitation mother liquor comprises the following steps that S11, the lithium precipitation mother liquor is provided, the lithium precipitation mother liquor comprises lithium ions, sulfate radicals or chloride ions, sodium ions and excessive carbonate radicals, and the temperature of the lithium precipitation mother liquor is 70-80 DEG C; s12, calcium oxide is added into the lithium precipitation mother liquor while hot to causticize excessive carbonate radicals in the lithium precipitation mother liquor into hydroxyl radicals, the concentration of calcium ions in the solution is controlled in the causticization process, and when the concentration of the calcium ions reaches 10-20 ppm and the pH reaches 12-13 at the same time, adding of the calcium oxide is stopped; and S13, filtering the causticized lithium precipitation mother liquor to remove calcium carbonate precipitation, and enabling filtrate to enter a subsequent extraction stage.

Description

Technical Field

[0001] This application relates to the field of new energy material preparation, and particularly relates to an efficient treatment method for spodumene concentrate and a pretreatment method for mother liquor after lithium precipitation. Background Art

[0002] The mother liquor after lithium precipitation is the solution discharged after the reaction and precipitation of the lithium-rich solution and the prepared refined sodium carbonate solution in the production process of lithium carbonate. The lithium concentration in the mother liquor after lithium precipitation is generally about 2 g / L. The mother liquor also contains sulfate or chloride ions, sodium ions, and excessive carbonate ions.

[0003] In the lithium sulfate system for lithium extraction from ore and lithium recovery, generally sulfuric acid is used to adjust the pH of the mother liquor after lithium precipitation to about 3 to remove carbonate ions, then alkali is added to adjust it back to neutral, and then salt is removed through evaporation crystallization and freeze crystallization (the potassium-sodium mixed salt will entrain and lose about 0.5% of lithium, the content of metallic lithium in sodium sulfate without washing is about 0.03%, and about 0.015% after washing). While removing salt, the lithium ion concentration in the mother liquor is increased. The lithium ions in the frozen mother liquor can generally be enriched to 12 - 15 g / L, and then the lithium-rich solution can be subjected to secondary lithium precipitation (or it can be returned to the front-end impurity removal for cyclic primary lithium precipitation). The lithium carbonate produced by secondary lithium precipitation is generally industrial-grade lithium carbonate and still needs carbonization purification to prepare battery-grade lithium carbonate (the purification cost is about 4000 yuan / ton). The output of the mother liquor after lithium precipitation accounts for about 15% - 20% of the total output of the lithium carbonate workshop. In addition, there is also mother liquor in secondary lithium precipitation, accounting for about 4% of the total output. The chloride ion content is about 1 - 5 g / L (generally, when the chloride ion reaches 1 g / L, it will corrode conventional MVR equipment), and the potassium ion content is about 30 g / L. As the system cycles continuously, impurities such as chloride ions and potassium need to be removed from the circuit.

[0004] In addition, the property that lithium phosphate has low solubility is also used to recover lithium in the mother liquor after lithium precipitation, but there are problems such as low selling price of lithium phosphate, 100 - 200 ppm lithium loss, phosphorus emission, and uneconomicality.

[0005] Considering improving the comprehensive lithium recovery rate and increasing benefits, many current enterprises are building lithium extraction production lines to recover lithium in the mother liquor after lithium precipitation by organic solvent extraction method to avoid lithium loss caused by salt removal in the backend system.

[0006] The lithium extractants on the market are generally neutral extractants, or chelating extractants, or composite extractants formed by mixing neutral extractants and chelating extractants in a certain proportion. Under certain alkalinity conditions, lithium ions can form a complex with the neutral extractant, and the complex is then extracted by the chelating extractant, thus achieving efficient lithium extraction.

[0007] For example, the extraction mechanism of the chelating extractant β-diketone compounds is to combine hydroxyl or carbonyl groups with Li⁺ to form a relatively stable chelate structure. β-diketone compounds exist in the keto-enol tautomeric equilibrium in solution. Since the hydrogen on the hydroxyl group in the enol form is more acidic, under alkaline conditions, the conversion of the diketone compound from the keto form to the enol form can be promoted, shifting the reaction equilibrium to the right (as shown in the following reaction formula). The H on the enol form of the diketone exchanges with alkaline earth metals such as Li⁺, and the O on the carbonyl group can form a stable chelate with the alkaline earth metal ions to achieve the purpose of extraction.

[0008]

[0009] Therefore, before the lithium precipitation mother liquor enters the extraction system, it needs to be pretreated, usually by adjusting the pH value to 12 - 13. However, in existing research, the pH regulators are generally flake soda or liquid caustic soda, which have a high cost. Summary of the Invention

[0010] The purpose of the present invention is to solve the above problems and provide an efficient treatment method for lithium concentrate and a pretreatment method for lithium precipitation mother liquor.

[0011] The technical solution of this application is realized as follows: The present invention provides a pretreatment method for lithium precipitation mother liquor, comprising the following steps: S10, Provide the lithium precipitation mother liquor, which includes lithium ions, sulfate or chloride ions, sodium ions, and excessive carbonate ions, and the temperature of the lithium precipitation mother liquor is 70 - 80 °C; S11, While it is hot, add calcium oxide to the lithium precipitation mother liquor to causticize the excessive carbonate inside into hydroxide ions. During the causticization process, control the calcium ion concentration in the solution. When the calcium ion concentration reaches 10 - 20 ppm and at the same time the pH reaches 12 - 13, stop adding calcium oxide; S12, Filter the causticized lithium precipitation mother liquor to remove calcium carbonate precipitation, and the filtrate enters the subsequent extraction stage.

[0012] The present invention further provides an efficient treatment method for lithium concentrate, comprising the following steps: S1, Mix the lithium concentrate with calcium sulfate and calcium carbonate auxiliary materials and then carry out ball milling or vertical milling to form a mixed powder of 200 - 300 mesh; S2, Import the mixed powder into a silo and carry out double - helix stirring. While carrying out the double - helix stirring, add the sodium potassium sulfate crystallization mother liquor. The content of sodium potassium sulfate in the sodium potassium sulfate crystallization mother liquor is 30 wt% - 40 wt%. After double - helix stirring, a wet powder with uniform solid - liquid mixing is formed. The mass of the added sodium potassium sulfate crystallization mother liquor is 20 - 40 wt% of the powder; S3. Introduce the wet powder material into a disk granulator. The wet powder forms pellets with a diameter of 5 - 15 mm through upward throwing and rolling down in the disk granulator and bonding. S4. Introduce the pellets into a cylindrical drying kiln for drying and then into a rotary kiln for roasting and transformation. The roasting temperature is 850 - 1000 °C. S5. After roasting, the pellets are subjected to 4 - stage countercurrent leaching and then separated to obtain lithium - containing brine. Then, the lithium - containing brine is purified by removing impurities and concentrated, and then lithium is precipitated to obtain a mother liquor after lithium precipitation. S6. While it is still hot, add calcium oxide to the mother liquor after lithium precipitation to causticize the excessive carbonate inside into hydroxide. During the causticization process, control the calcium ion concentration in the solution. When the calcium ion concentration reaches 10 - 20 ppm and at the same time the pH reaches 12 - 13, stop adding calcium oxide. S7. Filter the mother liquor after causticization to remove calcium carbonate precipitate, and the filtrate enters the subsequent extraction stage for lithium extraction. S8. Evaporate and crystallize the raffinate obtained after lithium extraction to obtain a sodium potassium sulfate crystallization mother liquor, and return the sodium potassium sulfate crystallization mother liquor to step S2 for reuse.

[0013] The advantages or beneficial effects in the above - mentioned technical solutions at least include: In the present invention, by adding the sodium potassium sulfate crystallization mother liquor to the mixed powder material during double - helix stirring, the sodium potassium sulfate crystallization mother liquor is evenly coated on the surface of the mixed powder material to form a core - shell structure. At the same time, the mother liquor can also penetrate into the interior of the mixed powder material, improving the contact tightness and mixing uniformity between the lithium concentrate and potassium and sodium ions, thereby enhancing the effect of the displacement reaction during the roasting process. Compared with the traditional method of first mixing sodium potassium sulfate salt with the concentrate and then adding water for granulation and roasting, the roasting transformation rate can be increased by about 3% - 4%.

[0014] Furthermore, in the present invention, the excessive carbonate in the lithium carbonate mother liquor after lithium precipitation is fully utilized and directly causticized into hydroxide, avoiding the introduction of extra sodium into the system. Then, less by - product sodium sulfate is produced in the subsequent salt discharge, which is beneficial to reducing energy consumption.

[0015] Finally, in the present invention, while adding alkali with calcium oxide, as much carbonate as possible is removed. Actually, the amount of acid used before the mother liquor after lithium precipitation finally enters MVR evaporation and crystallization is reduced. In order to control the calcium ion in the mother liquor not to exceed 20 ppm (too high calcium ion concentration will reduce the use effect of the lithium extractant), there will be 3 - 5 g / L of carbonate remaining in the mother liquor. After extracting lithium, this part of carbonate continues to exist in the raffinate. When acid is adjusted for the raffinate, this part of carbonate will consume more sulfuric acid to be neutralized, and it also avoids scaling on the tube wall during MVR evaporation. If calcium oxide causticization is not used, the general carbonate content in the mother liquor is 13 - 17 g / L, and the amount of sulfuric acid required to neutralize this part of carbonate is much higher than this method. Description of the Drawings

[0016] The accompanying drawings illustrate exemplary embodiments of the present application of the embodiments of the present invention and, together with their description, are used to explain the principles of the present application. These accompanying drawings are included to provide a further understanding of the present application and are included in this specification and form a part of this specification.

[0017] Figure 1 A flowchart of an efficient processing method for spodumene concentrate provided by an embodiment of the present invention is shown. Detailed implementation manners

[0018] Embodiments of the present application will be described in more detail below with reference to the accompanying drawings. Although some embodiments of the present application are shown in the drawings, it should be understood that the present application can be implemented in various forms and should not be construed as limited to the embodiments set forth herein. On the contrary, these embodiments are provided to provide a more thorough and complete understanding of the present application. It should be understood that the accompanying drawings and embodiments of the present application are only for exemplary purposes and are not used to limit the protection scope of the present application.

[0019] It should be noted that, without conflict, the embodiments in the present application and the features in the embodiments can be combined with each other. The present application will be described in detail below with reference to the accompanying drawings and in combination with the embodiments.

[0020] The names of the messages or information exchanged between multiple devices in the embodiments of the present application are only for illustrative purposes and are not used to limit the scope of these messages or information.

[0021] Referring to Figure 1 , an embodiment of the present invention provides an efficient processing method for spodumene concentrate, including the following steps: S1. Mix spodumene concentrate with calcium sulfate and calcium carbonate auxiliary materials, and then perform ball milling or vertical milling to form a mixed powder with a particle size of 200 - 300 mesh; S2. Introduce the mixed powder into a silo and perform double - helix stirring. While performing double - helix stirring, add a sodium potassium sulfate crystallization mother liquor, where the sodium potassium sulfate content in the sodium potassium sulfate crystallization mother liquor is 30wt% - 40wt%. After double - helix stirring, a wet powder with uniform solid - liquid mixing is formed, and the mass of the added sodium potassium sulfate crystallization mother liquor is 20 - 40wt% of the powder; S3. Introduce the wet powder into a disk granulator, and the wet powder forms pellets with a diameter of 5 - 15 mm through upward throwing and rolling and falling adhesion in the disk granulator; S4. Introduce the pellets into a cylindrical drying kiln for drying and then enter a rotary kiln for roasting and transformation, and the roasting temperature is 850 - 1000 °C; S5. The roasted pellets are separated by four-stage countercurrent leaching to obtain lithium-containing brine. Then, the lithium-containing brine is purified by impurity removal and concentration, and then lithium precipitation is carried out to obtain a mother liquor after lithium precipitation; S6. While it is hot, calcium oxide is added to the mother liquor after lithium precipitation to causticize the excessive carbonate therein into hydroxide. During the causticization process, the calcium ion concentration in the solution is controlled. When the calcium ion concentration reaches 10-20 ppm and at the same time the pH reaches 12-13, the addition of calcium oxide is stopped; S7. The mother liquor after lithium precipitation after causticization is filtered to remove calcium carbonate precipitate, and the filtrate enters the subsequent extraction stage for lithium extraction; S8. The raffinate obtained after lithium extraction is evaporated and crystallized to obtain a potassium sodium sulfate crystallization mother liquor, and the potassium sodium sulfate crystallization mother liquor is returned to step S2 for reuse.

[0022] In step S1, the lepidolite concentrate and the roasting aid are mixed according to a mass ratio of lepidolite concentrate:CaSO4·2H2O:CaCO3 = 1:0.2-0.6:0-0.45, and then ball milled or vertical milled to form a mixed powder of 200-300 mesh.

[0023] In step S2, the potassium sodium sulfate crystallization mother liquor is the potassium sodium sulfate crystallization mother liquor generated during the evaporation of the raffinate in step S8. The potassium sodium sulfate crystallization mother liquor is added to the double helix stirrer in batches while it is hot. Since the potassium sodium sulfate content in the potassium sodium sulfate crystallization mother liquor is high and the composition is uniform, it can be uniformly mixed with the mixed powder and coated on the surface of the mixed powder to form a core-shell structure. Further, since the potassium sodium sulfate crystallization mother liquor has a certain temperature, the potassium sodium sulfate crystallization mother liquor can further penetrate into the interior of the mixed powder.

[0024] As a further improvement, in step S2, in multiple embodiments thereof, the mass of the added potassium sodium sulfate crystallization mother liquor is 20 wt%, 22 wt%, 25 wt%, 27 wt%, 30 wt%, 32 wt%, 35 wt%, 37 wt% and 40 wt% of the mixed powder. Preferably, the mass of the added potassium sodium sulfate crystallization mother liquor is 25-30 wt% of the mixed powder. Preferably, the potassium sodium sulfate content in the potassium sodium sulfate crystallization mother liquor is 33 wt%-36 wt%. It can be understood that if the mass of the added potassium sodium sulfate crystallization mother liquor is too much, the viscosity will be high and pellets cannot be formed subsequently; while if the mass of the added potassium sodium sulfate crystallization mother liquor is too little, a uniform core-shell structure cannot be formed.

[0025] In step S3, after the preliminary mixing in step S2, the wet powder material can be quickly transferred to the disk granulator for granulation. In the prior art, generally, water spraying and mixing granulation are required in this step; in this case, by adding the sodium potassium sulfate crystallization mother liquor in step S2, the wet powder material formed by the water contained therein can be directly subjected to disk granulation without additional water spraying. In addition, since it is a wet powder material in this case, there will be no dust pollution to the environment and no impact on the health of the operators, nor will there be any loss caused by the dry powder material floating in the air.

[0026] In step S4, experimental data show that, under the condition that other conditions are the same, compared with granulating by first mixing the sodium potassium sulfate salt with the concentrate and then adding water for granulation and roasting, the roasting transformation rate can be increased by about 3-4% by adding the sodium potassium sulfate crystallization mother liquor for granulation.

[0027] Preferably, the step of introducing the pellets into a cylindrical drying kiln for drying and then entering a rotary kiln for roasting transformation at a roasting temperature of 850-1000 °C specifically includes: introducing the pellets into a cylindrical drying kiln for drying and then entering a rotary kiln for roasting transformation at a roasting temperature of 900-950 °C. More preferably, the step of introducing the pellets into a cylindrical drying kiln for drying and then entering a rotary kiln for roasting transformation at a roasting temperature of 850-1000 °C specifically includes: introducing the pellets into a cylindrical drying kiln for drying and then entering a rotary kiln for roasting transformation at a roasting temperature of 910-930 °C.

[0028] Experimental data show that, under the condition that the dosage of potassium and sodium salts and the roasting temperature and other remaining conditions are the same, compared with granulating by first mixing the sodium potassium sulfate salt with the concentrate and then adding water for granulation and roasting, the roasting transformation rate can be increased by about 3-4% by adding the sodium potassium sulfate solution for granulation.

[0029] Specifically, refer to the following example and comparative data: Example 1: Mix lithium concentrate with calcium sulfate and calcium carbonate auxiliary materials according to the ratio of lithium concentrate:CaSO4·2H2O:CaCO3 = 1:0.5:0.2, and then carry out ball milling or vertical milling to form 250-mesh (D90) mixed powder; then introduce the mixed powder into a silo and carry out double-screw stirring. While carrying out double-screw stirring, add the sodium potassium sulfate crystallization mother liquor in 10 times within 5 minutes. The sodium potassium sulfate content in the sodium potassium sulfate crystallization mother liquor is 30 wt%. After double-screw stirring, a wet powder material with uniform solid-liquid mixing is formed. The mass of the added sodium potassium sulfate crystallization mother liquor is 28 wt% of the mixed powder; introduce the wet powder material into a disk granulator, and the wet powder forms 5-15-mm pellets through upward throwing and rolling and falling bonding in the disk granulator; introduce the pellets into a cylindrical drying kiln for drying and then enter a rotary kiln for roasting transformation at a roasting temperature of 900 °C for 1 hour.

[0030] Example 2: It is basically the same as Example 1, except that the roasting temperature is 910 °C.

[0031] Example 3: It is basically the same as Example 1, except that the roasting temperature is 920 °C.

[0032] Example 4: It is basically the same as Example 1, except that the roasting temperature is 950 °C.

[0033] Example 5: It is basically the same as Example 3, except that the content of potassium and sodium sulfate in the potassium and sodium sulfate crystallization mother liquor is 35 wt%.

[0034] Example 6: It is basically the same as Example 3, except that the content of potassium and sodium sulfate in the potassium and sodium sulfate crystallization mother liquor is 40 wt%.

[0035] Comparative Example 1: The lithium concentrate is mixed with calcium sulfate and calcium carbonate auxiliary materials according to the ratio of lithium concentrate:CaSO4·2H2O:CaCO3 = 1:0.5:0.2, and potassium and sodium sulfate powder (where the dosage of potassium and sodium sulfate is the same as that in Example 1) is added for ball milling or vertical milling to form 250-mesh mixed powder; the wet powder is introduced into a disk granulator, and water is sprayed during the granulation process. The wet powder forms 5-15 mm pellets through the upward throwing and rolling and falling adhesion of the disk granulator; the pellets are introduced into a cylindrical drying kiln for drying and then enter a rotary kiln for roasting and transformation. The roasting temperature is 900 °C and the time is 1 hour.

[0036] Comparative Example 2: It is basically the same as Comparative Example 1, except that the roasting temperature is 910 °C.

[0037] Comparative Example 3: It is basically the same as Comparative Example 1, except that the roasting temperature is 920 °C.

[0038] The roasting data of Examples 1-3 and Comparative Examples 1-3 are compared as follows: Table 1 shows the data of pellet roasting and transformation

[0039] In step S5, the lithium-containing brine separated after the 4-stage countercurrent leaching, the steps of removing impurities, purifying, concentrating, and precipitating lithium from the lithium-containing brine are all existing technologies and will not be elaborated here.

[0040] After the above treatment, the lithium precipitation mother liquor contains lithium ions, sulfate or chloride ions, sodium ions, and excessive carbonate ions, and the temperature of the lithium precipitation mother liquor is 70-80 °C.

[0041] In step S6, compared with using sodium hydroxide (flake caustic or liquid caustic) to supplement alkali, inexpensive calcium oxide can significantly reduce the production auxiliary material cost.

[0042] In addition, in step S6, the excessive carbonate ions in the lithium carbonate precipitation mother liquor are fully utilized and directly causticized into hydroxide ions, avoiding introducing extra sodium into the system. Then, less by-product sodium sulfate is generated in the back-end salt discharge, which is beneficial to reducing energy consumption.

[0043] In step S6, while supplementing alkali with calcium oxide, as much carbonate ions as possible are removed. Actually, the amount of acid used before the lithium precipitation mother liquor finally enters MVR evaporation crystallization is reduced. To control the calcium ion content in the mother liquor not to exceed 20 ppm (too high calcium ion concentration will reduce the use effect of lithium extractant), 3-5 g / L of carbonate ions will remain in the mother liquor. After lithium extraction, this part of carbonate ions continues to exist in the raffinate. When adjusting the acid of the raffinate, this part of carbonate ions will consume more sulfuric acid to be neutralized, and it also avoids scaling on the tube wall during MVR evaporation. If calcium oxide causticization is not used, the general carbonate ion content in the mother liquor is 13-17 g / L, and the amount of sulfuric acid required to neutralize this part of carbonate ions is much higher than this method.

[0044] In step S7, the steps of filtering the causticized lithium precipitation mother liquor to remove calcium carbonate precipitate, and the filtrate entering the subsequent extraction stage for lithium extraction are also prior arts and will not be elaborated here.

[0045] In step S8, the step of evaporating and crystallizing the raffinate to obtain a sodium potassium sulfate crystallization mother liquor specifically includes: Evaporating and concentrating the raffinate at 60-80 °C to 40-50% of the volume of the raffinate and precipitating a small amount of salts to obtain a sodium potassium sulfate crystallization mother liquor.

[0046] In other embodiments, it may further include: After drying the washed calcium carbonate precipitate, it is returned to the pyrometallurgical section in S1 as a roasting auxiliary material for batching and roasting.

[0047] The present invention creatively reuses the calcium carbonate residue completely in the lepidolite roasting production line, which is equivalent to zero cost of calcium oxide.

[0048] Those skilled in the art should understand that the above embodiments are only for clearly explaining the present application and do not limit the scope of the present application. For those skilled in the art, other changes or modifications can be made based on the above disclosure, and these changes or modifications are still within the scope of the present application.

Claims

1. A pretreatment method for lithium precipitation mother liquor, characterized in that, It includes the following steps: S11. Provide a lithium precipitation mother liquor, which includes lithium ions, sulfate or chloride ions, sodium ions, and excessive carbonate ions. The temperature of the lithium precipitation mother liquor is 70 - 80 °C; S12. While it is hot, add calcium oxide to the lithium precipitation mother liquor to causticize the excessive carbonate ions inside into hydroxide ions. During the causticization process, control the calcium ion concentration in the solution. When the calcium ion concentration reaches 10 - 20 ppm and at the same time the pH reaches 12 - 13, stop adding calcium oxide; S13. Filter the causticized lithium precipitation mother liquor to remove calcium carbonate precipitate, and the filtrate enters the subsequent extraction stage.

2. An efficient treatment method for lithium concentrate, characterized in that, It includes the following steps: S1. Mix lithium concentrate with calcium sulfate and calcium carbonate auxiliary materials, and then carry out ball milling or vertical milling to form a mixed powder of 200 - 300 meshes; S2. Import the mixed powder into a silo and carry out double - helix stirring. While carrying out the double - helix stirring, add a sodium sulfate - potassium crystallization mother liquor. The content of sodium sulfate - potassium in the sodium sulfate - potassium crystallization mother liquor is 30 wt% - 40 wt%. After double - helix stirring, a wet powder with uniform solid - liquid mixing is formed. The mass of the added sodium sulfate - potassium crystallization mother liquor is 20 - 40 wt% of the powder; S3. Import the wet powder into a disk granulator. The wet powder is bonded into pellets of 5 - 15 mm through the upward throwing and rolling and falling of the disk granulator; S4. Import the pellets into a cylindrical drying kiln for drying and then enter a rotary kiln for roasting and transformation. The roasting temperature is 850 - 1000 °C; S5. After the roasted pellets are leached by four - stage counter - current leaching, a lithium - containing brine is separated. Then, after the lithium - containing brine is purified and concentrated by impurity removal, lithium precipitation is carried out to obtain a lithium precipitation mother liquor; S6. While it is hot, add calcium oxide to the lithium precipitation mother liquor to causticize the excessive carbonate ions inside into hydroxide ions. During the causticization process, control the calcium ion concentration in the solution. When the calcium ion concentration reaches 10 - 20 ppm and at the same time the pH reaches 12 - 13, stop adding calcium oxide; S7. Filter the causticized lithium precipitation mother liquor to remove calcium carbonate precipitate, and the filtrate enters the subsequent extraction stage for lithium extraction; S8. Evaporate and crystallize the raffinate after lithium extraction to obtain a sodium sulfate - potassium crystallization mother liquor, and return the sodium sulfate - potassium crystallization mother liquor to step S2 for reuse.

3. The high-efficiency treatment method of spodumene concentrate according to claim 2, characterized in that The washed calcium carbonate precipitate, after being dried, is returned to the pyrometallurgical section as a roasting auxiliary material for batching and roasting.

4. The high-efficiency treatment method of spodumene concentrate according to claim 2, characterized in that In step S4, the step of importing the pellets into a cylindrical drying kiln for drying and then entering a rotary kiln for roasting and transformation, with a roasting temperature of 850 - 1000 °C, specifically includes: Import the pellets into a cylindrical drying kiln for drying and then enter a rotary kiln for roasting and transformation, with a roasting temperature of 900 - 950 °C.

5. The high-efficiency treatment method of spodumene concentrate according to claim 2, wherein: In step S4, the step of importing the pellets into a cylindrical drying kiln for drying and then entering a rotary kiln for roasting and transformation, with a roasting temperature of 850 - 1000 °C, specifically includes: Import the pellets into a cylindrical drying kiln for drying and then enter a rotary kiln for roasting and transformation, with a roasting temperature of 910 - 930 °C.

6. The high-efficiency treatment method of spodumene concentrate according to claim 2, wherein: In step S8, the step of evaporating and crystallizing the raffinate to obtain a sodium sulfate - potassium crystallization mother liquor specifically includes: The raffinate is evaporated and concentrated at 60-80 °C to 40-50% of the volume of the raffinate, and a small amount of salts are precipitated to obtain a potassium sodium sulfate crystallization mother liquor.

7. The high-efficient treatment method of spodumene concentrate according to claim 2, wherein: In step S8, the potassium sodium sulfate content in the potassium sodium sulfate crystallization mother liquor is 33 wt% - 36 wt%.

8. The high-efficient treatment method of spodumene concentrate according to claim 2, characterized in that: In step S2, the mass of the potassium sodium sulfate crystallization mother liquor added is 25-30 wt% of the powder material.

Images