Treatment method of clay lithium ore

Abstract

The invention provides a treatment method of clay lithium ore, which is characterized in that auxiliary materials are mixed with the clay lithium ore, so that crystal lattices of the clay lithium ore are converted under the action of high temperature, a connecting bond of Li < + > in the clay ore is broken, and metal cations in the auxiliary materials replace positions before the Li < + >, so that the leaching difficulty is reduced, and the leaching efficiency is improved. And the lithium can be dissolved out by using pure water subsequently. The dissolution amount of impurity metal ions in the obtained leaching solution is small, especially iron, aluminum and the like are basically not dissolved out, the later impurity removal cost is greatly reduced, and lithium loss caused by impurity removal is also avoided; and a regenerated auxiliary material obtained by crystallizing the obtained leachate can be directly recycled, and the recycling rate of the auxiliary material is 88% or above.

Description

Technical Field

[0001] The invention belongs to the field of ore processing, relates to the processing of lithium ore, and in particular to a method for processing clay lithium ore. Background Art

[0002] Globally, with the rapid development of the new energy vehicle industry, the demand for lithium resources has risen sharply, and the mining and extraction technology of lithium resources has also faced unprecedented challenges. Among the many lithium mineral resources, clay lithium ore is an emerging type of lithium resource. Its unique chemical composition and crystal structure are fundamentally different from traditional spodumene and lepidolite. Clay lithium ore usually has a low lithium content and is accompanied by a variety of complex components. It is not suitable for direct use of conventional lithium ore extraction technology, which greatly increases the difficulty of lithium extraction and poses a severe challenge to the existing lithium extraction technology.

[0003] The following prior arts exist for the treatment and recovery of lithium from clay lithium ore:

[0004] CN114684834A discloses a method for extracting lithium from clay-type lithium ore. The method involves mixing lithium clay with soda ash and sodium sulfate, roasting, grinding and leaching. However, the method involves alkali corrosion of equipment and requires a large amount of sodium silicate and sodium aluminate to remove silicon and aluminum, which increases costs.

[0005] CN111893318A discloses a method for extracting lithium from lithium-containing clay. The method adopts a sulfate roasting method, wherein lithium clay is mixed with sulfate to obtain a spherical material, which is then roasted, crushed, and leached. The method produces a large amount of calcium-silicon waste slag, which is difficult to handle. The lithium oxide content in the slag reaches 0.2%, and the method is only applicable to clay ores with a high lithium oxide grade.

[0006] CN113955775A discloses a method for extracting lithium carbonate from lithium-rich clay by an acid-base combined method, wherein the lithium-rich clay is added to a sulfuric acid solution of a certain concentration for leaching, a sodium hydroxide solution is added to the acid leaching residue for alkaline leaching, and carbon dioxide gas is introduced into the alkaline leaching solution to obtain lithium carbonate solid and carbon denominator liquid. The method uses a strong acid that is prone to produce acid mist and corrode equipment, and the acid-base combined method consumes a large amount of resources;

[0007] CN115161496A discloses a method for extracting lithium from lithium clay, wherein lithium clay powder is roasted, the roasted clinker is ground and then leached, and solid-liquid separation is performed to obtain a lithium-containing solution and leached residue, and the leaching agent is specifically limited to sodium hydroxide, potassium hydroxide, a strong acid salt of sodium or a strong acid salt of potassium to obtain a lithium-rich solution. The leaching agent of this method is relatively expensive and a large amount of leaching agent needs to be consumed, resulting in high cost;

[0008] CN114959253A discloses a method for extracting lithium from lithium clay. The lithium clay is pretreated, microwave roasted, heat-insulated, cooled, and ground to obtain a crushed material. The specific conditions of microwave roasting are defined, and then leaching is performed to obtain a lithium-containing leaching solution. The heating equipment of this method is complex and needs to be specially customized, which is costly. In addition, different media have different microwave absorption capabilities and microwave coupling.

[0009] CN115287469A discloses a method for selectively extracting lithium from clay-type lithium ore, wherein lithium-rich clay powder is mixed with a lithium ion exchange solution to prepare a slurry, wherein the lithium ion exchange solution is a chloride metal solution, and then an ultrasonic enhanced leaching reaction is carried out to separate a lithium extract and a filter residue; the lithium extract is subjected to extraction, stripping, and oil removal to obtain a lithium chloride refined solution. This method is not universal and has a poor selectivity effect on low-lithium clay ores.

[0010] On the whole, the particularity of clay lithium ore is mainly reflected in its low lithium concentration, which poses a direct obstacle to the traditional direct extraction process. This problem is particularly prominent when dealing with low-grade or even extremely low-grade clay lithium ore. Existing processing technologies often make it difficult to efficiently enrich lithium elements, resulting in low lithium content in lithium extraction mother liquor and relatively high impurity content, which puts tremendous pressure on subsequent enrichment and purification steps. These steps are not only energy-intensive, but also require a large amount of additional additives and other chemical reagents to remove impurities, greatly increasing production costs. According to statistics, using existing technical means, it takes about 100 to 200 tons of raw ore to produce each ton of lithium carbonate product from clay lithium ore. In addition to the necessary amount of additives, the overall raw material cost is high and the economy is poor.

[0011] In view of the above, it is particularly urgent to develop efficient, low-cost, and environmentally friendly lithium extraction technology for low-grade and ultra-low-grade clay lithium ores. Summary of the invention

[0012] In view of the problems existing in the prior art, the purpose of the present invention is to provide a method for treating clay lithium ore, wherein the clay lithium ore is mixed with auxiliary materials, and roasted and leached in sequence to obtain a leachate and a leaching residue; the leachate is crystallized to obtain a regenerated auxiliary material and a lithium precipitation mother liquor. The present invention aims to provide a method that can enrich the lithium ion content in the extract and directly recycle the auxiliary materials by crystallizing the auxiliary materials in order to reduce the amount of auxiliary materials, reduce energy consumption, and reduce costs. The auxiliary materials recycling rate can reach more than 88%.

[0013] To achieve this object, the present invention adopts the following technical solutions:

[0014] In a first aspect, the present invention provides a method for processing clay lithium ore, the processing method comprising:

[0015] The clay lithium ore is mixed with auxiliary materials, the auxiliary materials include metal salts, and roasted and leached in sequence to obtain a leachate and leach residue; the leachate is crystallized to obtain a regenerated auxiliary material and a lithium precipitation mother liquor.

[0016] The present invention uses auxiliary materials to transform the crystal lattice of lithium clay ore under high temperature. + The connecting bonds in the clay mineral are broken, and the metal cations in the auxiliary materials replace Li + The previous position reduces the difficulty of leaching, and the lithium can be dissolved out with pure water later. The amount of impurity metal ions dissolved in the obtained leachate is small, especially iron, aluminum, etc. are basically not dissolved. This is because the present invention uses metal salts for roasting, which is relatively mild, mainly destroying lithium chlorite and a small part of kaolinite, and has little effect on most of the diaspores and most of the kaolinite ores containing more impurities such as iron and aluminum, and cannot meet the requirements of destroying crystals. Therefore, the cost of impurity removal in the later stage can be greatly reduced, and the loss of lithium caused by impurity removal can also be avoided; the regenerated auxiliary materials obtained by crystallization of the obtained leachate can be directly recycled, and the auxiliary material recycling rate is above 88%.

[0017] The following are preferred technical solutions of the present invention, but are not intended to be limitations of the technical solutions provided by the present invention. Through the following technical solutions, the technical objectives and beneficial effects of the present invention can be better achieved and realized.

[0018] As a preferred technical solution of the present invention, the mass percentage of lithium element in the clay lithium ore is 0.1% to 1%, for example, 0.1%, 0.13%, 0.15%, 0.18%, 0.2%, 0.22%, 0.25%, 0.28%, 0.3%, 0.35%, 0.4%, 0.45%, 0.5%, 0.55%, 0.6%, 0.65%, 0.7%, 0.75%, 0.8%, 0.85%, 0.9%, 0.95% or 1.5%, etc.

[0019] The treatment method of the present invention is particularly suitable for the treatment, recovery and extraction of lithium ions from low-grade or very low-grade (lithium element accounts for 0.1% to 0.5%, such as 0.1%, 0.15%, 0.2%, 0.25%, 0.3%, 0.35%, 0.4%, 0.45% or 0.5%) clay lithium ore.

[0020] Preferably, the clay lithium ore is crushed before the mixing until the particles of 200 mesh account for 30wt% to 80wt%, for example, 30wt%, 35wt%, 40wt%, 45wt%, 50wt%, 55wt%, 60wt%, 65wt%, 70wt%, 75wt% or 80wt%, etc.

[0021] As a preferred technical solution of the present invention, the metal salt includes potassium salt and / or sodium salt, preferably sodium salt.

[0022] Preferably, the sodium salt comprises at least one of sodium sulfate, sodium chloride or sodium carbonate, preferably sodium sulfate.

[0023] Preferably, the potassium salt comprises at least one of potassium sulfate, potassium chloride or potassium carbonate.

[0024] Preferably, the auxiliary materials are crushed before the mixing until the particles of 200 mesh account for 30wt% to 90wt%, for example, 30wt%, 35wt%, 40wt%, 45wt%, 50wt%, 55wt%, 60wt%, 65wt%, 70wt%, 75wt%, 80wt%, 85wt% or 90wt%, etc.

[0025] As a preferred technical solution of the present invention, the mass ratio of the clay lithium ore to the auxiliary material is 1:(0.05-4), for example, 1:0.05, 1:0.1, 1:0.3, 1:0.5, 1:0.8, 1:1, 1:1.3, 1:1.5, 1:1.8, 1:2, 1:2.3, 1:2.5, 1:2.8, 1:3, 1:3.3, 1:3.5, 1:3.8 or 1:4, etc.

[0026] As a preferred technical solution of the present invention, clay lithium ore is mixed with auxiliary materials to obtain raw materials, and the raw materials are molded and then calcined.

[0027] As a preferred technical solution of the present invention, the roasting temperature is 300-1000°C, for example, 300°C, 350°C, 400°C, 450°C, 500°C, 550°C, 600°C, 650°C, 700°C, 750°C, 800°C, 850°C, 900°C, 950°C or 1000°C, and the calcination time is 0.5-3h, for example, 0.5h, 1h, 1.5h, 2h, 2.5h or 3h, etc.

[0028] As a preferred technical solution of the present invention, after the roasting, a roasted material is obtained, and the roasted material is crushed until the particles of 200 mesh account for 30wt% to 80wt%, for example, 30wt%, 35wt%, 40wt%, 45wt%, 50wt%, 55wt%, 60wt%, 65wt%, 70wt%, 75wt% or 80wt%, etc., and then the leaching is carried out.

[0029] Preferably, the leaching is carried out under normal pressure.

[0030] Preferably, the leaching temperature is 20-90°C, for example, 20°C, 25°C, 30°C, 35°C, 40°C, 45°C, 50°C, 55°C, 60°C, 65°C, 70°C, 75°C, 80°C, 85°C or 90°C, and the leaching time is 5-60min, for example, 5min, 10min, 15min, 20min, 25min, 30min, 35min, 40min, 45min, 50min, 55min or 60min, etc.

[0031] Preferably, the leaching agent comprises pure water or a dilute acid aqueous solution with a volume concentration of 5% to 50%, such as 5%, 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45% or 50%, etc., and the acid component in the dilute acid aqueous solution comprises at least one of sulfuric acid, hydrochloric acid, acetic acid, oxalic acid, nitric acid or carbonic acid, preferably pure water.

[0032] The present invention has low requirements on the material of the leaching and roasting equipment and does not corrode the equipment. After leaching with pure water as the leaching agent, the solid-liquid separation of the slurry is simple and the filtration speed is fast. The material requirements on the filtering equipment are low and the equipment is not damaged.

[0033] Preferably, the solid-liquid ratio of the leaching is 1g:(0.5-3)mL, for example, 1g:0.5mL, 1g:0.7mL, 1g:1mL, 1g:1.3mL, 1g:1.5mL, 1g:1.8mL, 1g:2mL, 1g:2.3mL, 1g:2.5mL, 1g:2.8mL or 1g:3mL, etc.

[0034] As a preferred technical solution of the present invention, the leached residue is washed once and twice in sequence to obtain a first washing liquid and a second washing liquid, respectively.

[0035] Preferably, the detergent for the primary washing and the secondary washing comprises pure water.

[0036] Preferably, the first washing liquid is reused for the leaching.

[0037] Preferably, the second washing liquid is reused for the primary washing.

[0038] As a preferred technical solution of the present invention, the crystallization method includes cooling crystallization or evaporative concentration.

[0039] Preferably, the temperature of the cooling crystallization is 0-25°C, for example, 0°C, 3°C, 5°C, 8°C, 10°C, 13°C, 15°C, 18°C, 20°C, 22°C or 25°C.

[0040] Preferably, the lithium precipitation mother liquor obtained by the cooling crystallization is reused in the leaching as the leaching agent with a volume fraction of 5% to 95% to enrich the concentration of lithium element, for example 5%, 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90% or 95%, etc.

[0041] In the present invention, the impure metal ions in the leachate after cooling and crystallization are relatively small, and can be used as a leaching agent for re-leaching without substantially affecting the leaching yield and effect. By means of such a cooling and crystallization re-leaching method, the purpose of enriching lithium ions is achieved. In addition, due to the low solubility of some impure metal ions, such as Ca 2+ After being saturated in the leachate, it will no longer dissolve and enrich, the flux will be reduced, and the cost of later calcium removal and other impurity removal will be reduced exponentially.

[0042] Preferably, the extract is firstly subjected to impurity removal before the evaporation and concentration.

[0043] In the present invention, since evaporation concentration can improve the lithium ion concentration in the leachate, the lithium ion mother liquor after evaporation concentration crystallization does not need to be used as a leaching agent for cyclic leaching; and in order to improve the purity of the lithium ion mother liquor obtained by evaporation concentration, it is preferred to remove impurities from the leachate before evaporation concentration. The crystallization method of evaporation concentration can further increase the auxiliary material recovery rate to more than 91.5%.

[0044] As a preferred technical solution of the present invention, the regenerated auxiliary material is recycled and mixed with the clay lithium ore.

[0045] Preferably, the regenerated auxiliary material is dried and then reused to be mixed with the clay lithium ore.

[0046] The hydrated metal salt obtained by crystallization and / or the metal salt after further drying in the present invention can be reused. Preferably, the hydrated metal salt crystallization can save process, energy and cost without the need for a drying step, and the effect is the same as that of the dried metal salt.

[0047] Preferably, the drying method includes direct drying and / or hot melt evaporation.

[0048] Preferably, the lithium precipitation mother liquor is subjected to lithium extraction to obtain lithium carbonate.

[0049] Compared with the prior art solutions, the present invention has at least the following beneficial effects:

[0050] The treatment method of clay lithium ore provided by the present invention not only has a high lithium recovery rate, but also can solve the shortcomings of the sulfuric acid method, the impurity metal ions in the leaching mother liquor that are difficult to separate, and can avoid the problems of large amount of limestone, low lithium recovery rate, and difficult recovery in the limestone method. In the present invention, auxiliary materials are recovered and reused by crystallization, and lithium ions can be effectively enriched by circulating the mother liquor. The comprehensive yield (lithium yield) of the present invention from low-grade and above clay lithium ore to lithium carbonate and other lithium products can reach more than 70%, and the comprehensive yield of extremely low-grade clay lithium ore to lithium carbonate and other products can reach more than 63%. The method is simple in process, has wide applicability, is suitable for the unique structure and performance of clay lithium ore, has low investment and high return, high safety, and is environmentally friendly. BRIEF DESCRIPTION OF THE DRAWINGS

[0051] Figure 1 1 is a schematic flow chart of the method for treating clay lithium ore of Example 1;

[0052] Figure 2 It is a schematic flow chart of the method for processing clay lithium ore of Example 3. DETAILED DESCRIPTION

[0053] The technical solution of the present invention is further illustrated below through specific implementation methods.

[0054] It should be clear to those skilled in the art that the embodiments are only intended to help understand the present invention and should not be considered as specific limitations of the present invention.

[0055] The main component contents of the clay lithium ore used in the following examples and comparative examples are shown in Table 1.

[0056] Table 1

[0057]

[0058]

[0059] Example 1

[0060] This embodiment provides a method for processing clay lithium ore, such as Figure 1 As shown, the processing method includes:

[0061] (1) crushing the clay lithium ore A until the particles of 200 mesh account for 55wt% to obtain a crushed material;

[0062] (2) crushing the auxiliary material sodium sulfate until the particles of 200 mesh account for 60wt% to obtain a crushed auxiliary material;

[0063] (3) mixing the obtained crushed material with crushing auxiliary materials in a mass ratio of 1:0.5 to obtain a raw meal;

[0064] (4) After the raw material is formed, it is placed in a high-temperature furnace for roasting, and the roasting temperature is controlled to be 750° C. and the time is 1 hour to obtain a roasted material;

[0065] (5) crushing the obtained roasted material until the particles of 200 mesh account for 55wt% to obtain clinker;

[0066] (6) leaching the obtained clinker under normal pressure, controlling the leaching temperature to be maintained at 40° C., the time to be 30 min, using pure water as the leaching agent, and having a leaching solid-liquid ratio of 1 g:1.2 mL, to obtain a leaching solution and a leaching residue; washing the leaching residue once and twice with pure water having a solid-liquid ratio of 1 g:0.7 mL, respectively, to obtain a first washing solution and a second washing solution, the first washing solution being reused in the leaching, and the second washing solution being reused in the first washing;

[0067] (7) Cooling and crystallizing the obtained leaching solution at 0° C. to obtain sodium sulfate decahydrate and lithium precipitation mother liquor. The sodium sulfate decahydrate is reused as a regeneration auxiliary material for preparing raw materials. The lithium precipitation mother liquor is reused as the leaching agent with a volume fraction of 50% for the leaching to enrich the concentration of lithium elements until a lithium precipitation mother liquor with a stable lithium ion content of 4 g / L is obtained.

[0068] Example 2

[0069] This embodiment provides a method for treating clay lithium ore. In step (7) of the treatment method, the obtained sodium sulfate decahydrate is dried or hot-melt evaporated to obtain anhydrous sodium sulfate, which is reused as a regenerated auxiliary material to prepare raw materials. Except for the above, other conditions are exactly the same as those in Example 1.

[0070] Example 3

[0071] This embodiment provides a method for processing clay lithium ore, such as Figure 2 As shown, the processing method step (7) includes:

[0072] The obtained leachate is impurity-removed and then evaporated and concentrated to obtain sodium sulfate decahydrate and lithium precipitation mother liquor. The sodium sulfate decahydrate is directly dried to obtain sodium sulfate, which is reused as a regeneration auxiliary material for preparing raw materials, and the lithium precipitation mother liquor is directly used to extract lithium ions.

[0073] Example 4

[0074] This embodiment provides a method for processing clay lithium ore, in which clay lithium ore B is used instead of clay lithium ore A in step (1). Except for the above, other conditions are the same as those in Example 1.

[0075] Example 5

[0076] This embodiment provides a method for treating clay lithium ore, wherein clay lithium ore C is used in place of clay lithium ore A in step (1). Except for the above, other conditions are the same as those in Example 1.

[0077] Example 6

[0078] This embodiment provides a method for processing clay lithium ore. In the processing method, in step (3), the mass ratio of crushed material to crushing auxiliary material is adjusted from 1:0.5 to 1:0.02. Except for the above, other conditions are exactly the same as those in Example 1.

[0079] Example 7

[0080] This embodiment provides a method for processing clay lithium ore. In the processing method, in step (3), the mass ratio of crushed material to crushing auxiliary material is adjusted from 1:0.5 to 1:1. Except for the above, other conditions are exactly the same as those in Example 1.

[0081] Example 8

[0082] This embodiment provides a method for treating clay lithium ore. In the treatment method, in step (4), the roasting temperature is adjusted from 750° C. to 300° C. Except for the above, other conditions are exactly the same as those in Example 1.

[0083] Example 9

[0084] This embodiment provides a method for treating clay lithium ore. In the treatment method, in step (4), the roasting temperature is adjusted from 750° C. to 900° C. Except for the above, other conditions are exactly the same as those in Example 1.

[0085] Example 10

[0086] This embodiment provides a method for treating clay lithium ore. In the treatment method, in step (5), the leaching agent is replaced by pure water with dilute sulfuric acid with a volume concentration of 15%. Except for the above, other conditions are exactly the same as those in Example 1.

[0087] Embodiment 11

[0088] This embodiment provides a method for treating clay lithium ore. In the treatment method, in step (2), the auxiliary material is replaced by potassium sulfate instead of sodium sulfate. Except for the above, other conditions are exactly the same as those in Example 1.

[0089] Comparative Example 1

[0090] This comparative example provides a method for treating clay lithium ore, wherein the method does not use auxiliary materials such as sodium sulfate. Except for the above, other conditions are exactly the same as those in Example 1.

[0091] Comparative Example 2

[0092] This comparative example provides a method for treating clay lithium ore, which adopts the sulfuric acid method of the prior art, and the method comprises:

[0093] S1. The clay lithium ore A is crushed until the particles of 200 mesh account for 55wt% to obtain a crushed material;

[0094] S2. The crushed material and 90% sulfuric acid were mixed at a mineral acid ratio of 1g:1g and then calcined at 250°C for 2h;

[0095] S3. The resulting roasted material was crushed until the particles of 200 mesh accounted for 55wt% to obtain clinker;

[0096] S4. The obtained clinker was leached at normal pressure, the temperature was controlled at 95 ° C, the time was 120min, the leaching agent was pure water, the leaching solid-liquid ratio was 1g: 5mL, and the lithium-containing mother liquor and leaching residue were obtained;

[0097] The treatment processes of the embodiments and comparative examples were monitored, and the recovery rate of lithium and the recovery rate of auxiliary materials were calculated based on the obtained products. The obtained results are recorded in Table 1.

[0098] Table 1

[0099]

[0100] It can be seen from Table 1 that:

[0101] Comparative Examples 1, 2, and 3 show that the auxiliary materials have little effect on the experimental results whether they are dehydrated or not after cooling and crystallizing, but hydrated sodium sulfate may cause material blockage when mixed, and evaporation and concentration can obtain a higher concentration of lithium precipitation mother liquor, but it is necessary to remove impurities in advance, otherwise it will cause scaling, reduce the recovery rate of auxiliary materials, and also reduce equipment performance;

[0102] By comparing Examples 1, 4, and 5, it is found that the process flow is widely applicable and is helpful for increasing the lithium ion concentration of clay lithium ores of different grades;

[0103] Comparison of Examples 1, 6, and 7 shows that the amount of auxiliary materials used has a greater influence on the lithium yield. When the mass ratio of crushed material to crushed auxiliary materials is 1:0.5, the lithium yield tends to stabilize. Further reduction of the mass ratio does not significantly increase the lithium yield and reduces the auxiliary material yield.

[0104] Comparative Examples 1, 8, and 9 show that the lithium yield increases with increasing temperature, and the lithium yield reaches a maximum at 750°C. Further increasing the temperature does not increase the lithium yield much, but more impurity metal ions are dissolved.

[0105] Comparing Examples 1 and 10, it is found that using dilute acid as a leaching agent helps to improve the lithium yield, but the concentration of impurity metal ions dissolved also increases;

[0106] Comparing with Examples 1 and 11, the solubility of potassium sulfate at 0°C is 7.4, 40°C is 14.8, and 60°C is 18.2. The solubility of sodium sulfate at 0°C is 4.9, 40°C is 48.8, and 60°C is 45.3. The cooling crystallization of sodium sulfate can take away more water, and the concentration effect is more obvious.

[0107] In Comparative Example 1, lithium ions are basically not dissolved when the clay lithium ore is directly calcined without adding auxiliary materials;

[0108] In Comparative Example 2, the existing acid roasting process is used. Although the lithium ion yield can reach more than 90%, it has high requirements on the equipment material, and a large amount of impurity metal ions are dissolved. The concentration method can only be a method of first removing impurities and then evaporating and concentrating. The equipment investment is large and the operating energy consumption is high.

[0109] The preferred embodiments of the present invention are described in detail above. However, the present invention is not limited to the specific details in the above embodiments. Within the technical concept of the present invention, a variety of simple modifications can be made to the technical solution of the present invention, and these simple modifications all belong to the protection scope of the present invention.

[0110] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner without contradiction. In order to avoid unnecessary repetition, the present invention will not further describe various possible combinations.

[0111] In addition, various embodiments of the present invention may be arbitrarily combined, and as long as they do not violate the concept of the present invention, they should also be regarded as the contents disclosed by the present invention.

Claims

1. A method for processing clay lithium ore, characterized in that: The processing method comprises: The clay lithium ore is mixed with auxiliary materials, the auxiliary materials include metal salts, and roasted and leached in sequence to obtain a leachate and leach residue; the leachate is crystallized to obtain a regenerated auxiliary material and a lithium precipitation mother liquor.

2. The processing method according to claim 1, characterized in that: The mass percentage of lithium element in the clay lithium ore is 0.1% to 1%; Preferably, the clay lithium ore is crushed before the mixing until the particles of 200 mesh account for 30wt% to 80wt%.

3. The processing method according to claim 1 or 2, characterized in that: The metal salt includes potassium salt and / or sodium salt; Preferably, the sodium salt comprises sodium sulfate; Preferably, the auxiliary materials are crushed before mixing until the particles of 200 meshes account for 30 wt% to 90 wt%.

4. The processing method according to any one of claims 1 to 3, characterized in that: The mass ratio of the clay lithium ore to the auxiliary material is 1:(0.05-4).

5. The processing method according to any one of claims 1 to 4, characterized in that: The clay lithium ore is mixed with auxiliary materials to obtain raw materials, and the raw materials are molded and then roasted.

6. The processing method according to any one of claims 1 to 5, characterized in that: The calcination temperature is 300-1000° C. and the calcination time is 0.5-3 hours.

7. The processing method according to any one of claims 1 to 6, characterized in that: After the calcination, a calcined material is obtained, the calcined material is crushed until the particles of 200 meshes account for 30wt% to 80wt%, and then the leaching is performed; Preferably, the leaching is carried out under normal pressure; Preferably, the leaching temperature is 20-90°C and the leaching time is 5-60 minutes; Preferably, the leaching agent comprises pure water or a dilute acid aqueous solution with a volume concentration of 5% to 50%; the acid component in the dilute acid aqueous solution comprises at least one of sulfuric acid, hydrochloric acid, acetic acid, oxalic acid, nitric acid or carbonic acid; Preferably, the solid-liquid ratio of the leaching is 1 g: (0.5-3) mL.

8. The processing method according to any one of claims 1 to 7, characterized in that: The leached residue is washed once and twice in sequence to obtain a first washing liquid and a second washing liquid respectively; Preferably, the detergent for the first washing and the second washing comprises pure water; Preferably, the first washing liquid is reused for the leaching; Preferably, the second washing liquid is reused for the primary washing.

9. The processing method according to any one of claims 1 to 8, characterized in that: The crystallization method includes cooling crystallization or evaporation concentration; Preferably, the cooling crystallization temperature is 0 to 25°C; Preferably, the lithium precipitation mother solution obtained by the cooling crystallization is used as the leaching agent with a volume fraction of 5% to 95% for the leaching to enrich the concentration of lithium element; Preferably, the extract is firstly subjected to impurity removal before the evaporation and concentration.

10. The processing method according to any one of claims 1 to 3, characterized in that: The regenerated auxiliary material is recycled and mixed with the clay lithium ore; Preferably, the regenerated auxiliary material is dried and then reused to be mixed with the clay lithium ore; Preferably, the drying method includes direct drying and / or hot melt evaporation; Preferably, the lithium precipitation mother liquor is subjected to lithium extraction to obtain lithium carbonate.

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