阅读说明：本技术 盐湖提锂的方法 (Method for extracting lithium from salt lake ) 是由 高东 徐云玲 徐茶清 曹文玉 李阳 于 2019-09-20 设计创作，主要内容包括：本发明涉及盐湖提锂领域,公开了高效盐湖提锂的方法。包括：(1)将盐湖卤水与锂吸附剂接触吸附进行嵌锂,得到吸附锂的富锂吸附剂；(2)用第一清洗剂对所述富锂吸附剂进行一次洗涤,得到第一清洗液和第一吸附剂；其中,所述第一清洗液返回混入所述盐湖卤水,所述第一清洗剂的流速为6-16BV/h；(3)用第二清洗剂对所述第一吸附剂进行二次洗涤,得到第二清洗液和第二吸附剂；其中,所述第二清洗液返回混入所述清洗剂I,所述第二清洗剂的流速为6-16BV/h；(4)用温水对所述第二吸附剂进行解锂,得到锂溶液,其中解锂时间为20-90min。本发明改进了盐湖卤水提锂的方法,仅通过两次洗涤且回用步骤,解锂直接得到合格的锂溶液,且锂溶液无需套洗回用。(The invention relates to the field of lithium extraction in salt lakes, and discloses a high-efficiency method for extracting lithium in salt lakes. The method comprises the following steps: (1) contacting salt lake brine with a lithium adsorbent for adsorption to embed lithium, so as to obtain a lithium-rich adsorbent for adsorbing lithium; (2) washing the lithium-rich adsorbent once with a first cleaning agent to obtain a first cleaning solution and a first adsorbent; wherein the first cleaning solution is returned and mixed into the salt lake brine, and the flow rate of the first cleaning solution is 6-16 BV/h; (3) washing the first adsorbent for the second time by using a second cleaning agent to obtain a second cleaning solution and a second adsorbent; wherein the second cleaning solution is returned and mixed with the cleaning agent I, and the flow rate of the second cleaning agent is 6-16 BV/h; (4) and (3) carrying out lithium desorption on the second adsorbent by using warm water to obtain a lithium solution, wherein the lithium desorption time is 20-90 min. The invention improves the method for extracting lithium from salt lake brine, and qualified lithium solution can be directly obtained by lithium dissolution through two washing and recycling steps without washing and recycling the lithium solution.)

1. A method for extracting lithium from a salt lake comprises the following steps:

(1) contacting salt lake brine with a lithium adsorbent for adsorption to embed lithium, so as to obtain a lithium-rich adsorbent for adsorbing lithium;

(2) washing the lithium-rich adsorbent once with a first cleaning agent to obtain a first cleaning solution and a first adsorbent; wherein the first cleaning solution is returned and mixed into the salt lake brine, and the flow rate of the first cleaning solution is 6-16 BV/h;

(3) washing the first adsorbent for the second time by using a second cleaning agent to obtain a second cleaning solution and a second adsorbent; wherein the second cleaning solution is returned and mixed with the first cleaning agent, and the flow rate of the second cleaning agent is 6-16 BV/h;

(4) and (3) carrying out lithium desorption on the second adsorbent by using warm water to obtain a lithium solution, wherein the lithium desorption time is 20-90 min.

2. The method of claim 1, wherein in step (1), the lithium intercalation conditions include: the flow rate of the salt lake brine is 1.5-4BV/h, and the adsorption time is 1-5 h;

preferably, in the lithium intercalation process, the extraction rate of lithium in the salt lake brine is 50-95%.

3. The method according to claim 1 or 2, wherein in the step (1), the temperature of the salt lake brine is-15 ℃ to 65 ℃;

preferably, in the salt lake brine, the concentration of the Li element is 150-400mg/kg, and the concentration of the Cl element is 200-300 g/kg; the density of the salt lake brine is 1.2-1.32 g/mL.

4. The method of claim 1, wherein in step (2), the first cleaning agent is water and/or the second cleaning agent;

preferably, the concentration of the Li element in the first cleaning solution is 160-300Mg/kg, and the concentration of the Mg element is 20-30 g/kg; the density of the first cleaning liquid is 1.1-1.2 g/mL.

5. The method according to claim 1 or 4, wherein in the step (2), the time of the one-time washing is 3-15min, and the temperature of the one-time washing is 1-35 ℃.

6. The method of claim 1, wherein in step (3), the second cleaning agent is water and/or low salt water;

preferably, the concentration of Li element in the low-salt water is 30-120mg/kg, and the total content of cations is not more than 2 g/kg;

preferably, in the second cleaning liquid, the concentration of Li element is 50-250mg/kg, and the total content of cation is not more than 10 g/kg.

7. The method according to claim 1 or 6, wherein in the step (3), the time of the secondary washing is 3-15min, and the temperature of the secondary washing is 1-35 ℃.

8. The method according to claim 1, wherein in the step (4), the flow rate of the warm water is 2-4BV/h, and the temperature of the warm water is 15-95 ℃, preferably 40-90 ℃.

9. The method as claimed in claim 1, wherein the concentration of Li element is 300-700Mg/kg, the concentration of Mg element is 1200-5600Mg/kg, the concentration of B element is 5-20Mg/kg, and the concentration of Na element is 50-150 Mg/kg.

10. The method of any of claims 1-9, wherein the lithium sorbent comprises Li of the formula_xCl·2Al(OH)₃·yH₂O, wherein x is more than or equal to 0.8 and less than or equal to 1.2, and y is more than or equal to 0 and less than or equal to 2, and a binder; wherein the particle diameter of the lithium adsorbent is 1-5mm, and the length of the lithium adsorbent is 1-10 mm;

preferably, the binder is at least one selected from the group consisting of polyamide, polypropylene, ethylene-vinyl acetate copolymer, polyvinyl chloride, polyethylene, polyvinylidene fluoride, polystyrene, acrylonitrile-butadiene-styrene, polymethyl methacrylate, polyoxymethylene, polyolefin ester, polyphenylene oxide, epoxy resin, and phenol resin.

Technical Field

The invention relates to the field of lithium extraction in salt lakes, in particular to a high-efficiency method for extracting lithium in salt lakes.

Background

The salt lake lithium extraction refers to extracting lithium from salt lake brine containing lithium and producing a lithium product. The lithium extraction from the salt lake brine usually comprises the steps of solarization and evaporation of the salt lake, obtaining different salts by stages, purifying the salt solution and the like, and finally separating and extracting the lithium salt from the solution to obtain the required lithium salt product. At present, the lithium carbonate production by extracting lithium from salt lake brine becomes the main attack direction of lithium salt production, and the technological methods for extracting lithium from salt lake brine mainly comprise a precipitation method, an extraction method, an ion exchange adsorption method, a carbonization method, a calcination leaching method, an electrodialysis method and the like. The research on the precipitation method, the extraction method, the ion exchange adsorption method and the carbonization method is relatively extensive and intensive, and is a method for extracting lithium from main salt lake brine. The key of the ion adsorption method is to research an adsorbent with excellent performance, the adsorbent is required to have excellent selective adsorption on lithium so as to eliminate the interference of a large amount of coexisting alkali metal and alkaline earth metal ions in brine, and the adsorption and elution performance of the adsorbent is required to be stable, so that the adsorbent is suitable for large-scale operation and use.

CN108658100B discloses a new process for producing lithium chloride from salt lake brine by adopting equipment for producing lithium chloride from salt lake brine: the equipment comprises a full-room bed (1), wherein an upper feeding hole (3) is formed in the middle end of the top of the full-room bed (1), a resin inlet (6) and a resin outlet (5) are sequentially formed in the left side of the full-room bed (1) from top to bottom, an upper liquid distributor (8) is fixedly installed at the upper end of an inner cavity of the full-room bed (1), an adsorbent (2) is filled in the middle end of the inner cavity, a lower liquid distributor (7) is fixedly installed at the lower end of the inner cavity of the full-room bed (1), and a lower feeding hole (4) is formed in the middle end of the bottom of the full-room bed (1); the upper part and the lower part of the full-chamber bed (1) are respectively provided with liquid distributors with different liquid distribution functions, and the structural form of the liquid distributor is selectableA movable porous uniform liquid distribution mode; the new process comprises the following steps: A. the operation mode is as follows: the process adopts continuous operation, namely, the scale of the process and the device is optimized through data calculated by the process, and the continuous operation of an industrialized device is realized by optimizing the operation mode; B. the raw materials comprise: (a) salt lake brine, wherein: li⁺Concentration of 0.01-0.2g/L, Mg²⁺The concentration is 30-50g/L, Na⁺The concentration is 30-45g/L, K⁺The concentration is 9-14g/L, the Cl + concentration is 200-300 g/L; (b) the old brine solution after the potassium is extracted from the salt lake brine, wherein: li⁺Concentration of 0.25-0.6g/L, Mg²⁺Concentration of 100-120g/L, Na⁺Concentration 0.1-0.2g/L, Cl^-The concentration is 300-400 g/L; C. the process and the technical equipment are as follows: adopting a self-made aluminum molecular sieve adsorbent as a core adsorbent, adopting a full-chamber bed of a specially designed liquid distributor as core technical equipment, and preparing a qualified lithium chloride solution with a magnesium-lithium ratio of 3:1-6:1 through the steps of adsorption, sectional washing and sectional desorption; D. the product is as follows: by the novel process and the equipment, the qualified lithium chloride liquid with the low magnesium-lithium ratio can be prepared, and the qualified lithium chloride liquid comprises the following components: li⁺Concentration of 0.4-0.9g/L, Mg²⁺0.5-8.0g/L of Na⁺Concentration 0.01-0.2g/L, Cl^-The concentration is 2-20 g/L; E. adsorption equivalent and yield: the primary yield of lithium chloride in brine is more than or equal to 50 percent; the adsorption equivalent of the lithium adsorbent is 1.8-2.7 g/kg; the loss rate in the washing process is 12-30%; F. improving and optimizing process parameters: compared with the traditional adsorption process, the adsorption equivalent of the adsorbent is improved by 15-30%; the washing loss is reduced by 10-25%; the lithium ion concentration of the qualified liquid is improved by 15-30%; G. the qualified liquid containing lithium chloride is extracted from salt lake brine by an ion exchange adsorption lithium extraction process and is obtained preliminarily and delicately, selective adsorption, washing and desorption of lithium chloride are realized from salt lake brine or old brine with the magnesium-lithium ratio of 300:1-600:1 of the old brine after potassium is extracted from the salt lake brine, the qualified liquid containing lithium chloride with the magnesium-lithium ratio of 3:1-6:1 is prepared, and qualified lithium chloride raw materials are provided for subsequent lithium carbonate or other lithium products.

CN108658101A discloses a new process for producing high-purity lithium chloride from salt lake brine, which comprises the following steps: 1) the operation mode is as follows: the process adopts continuous operation, i.e. the scale and the advantages of each device are optimized through data calculated by the processSelecting an operation mode to realize continuous operation; 2) raw materials: (a) salt lake brine, wherein: li⁺Concentration of 0.01-0.20g/L, Mg²⁺The concentration is 30-50g/L, Na⁺The concentration is 30-45g/L, K⁺Concentration 9-14g/L, Cl^-The concentration is 200-300 g/L; (b) the old brine solution after the potassium is extracted from the salt lake brine, wherein: li⁺Concentration of 0.25-0.6g/L, Mg²⁺Concentration 120g/L, Na⁺Concentration 0.1-0.2g/L, Cl^-The concentration is 300-400 g/L; 3) the product is as follows: the innovative process can prepare qualified lithium chloride solution products with the content of more than or equal to 99.5 percent, and comprises the following process procedures of 1-6 and the like; 4) extracting qualified lithium chloride-containing liquid from salt lake brine by an ion exchange adsorption lithium extraction process and performing primary refinement, wherein the qualified lithium chloride-containing liquid is obtained by a process 1, namely extracting potassium from salt lake brine or from salt lake brine, and then obtaining an old brine solution 300:1-600:1, realizing selective adsorption, washing and desorption of lithium chloride, and preparing the magnesium-lithium ratio of 3:1-6:1, and providing qualified lithium chloride raw materials for subsequent lithium carbonate or other lithium products.

However, the existing lithium adsorption and extraction process is complex, the lithium chloride solution obtained by lithium dissolution can meet the product requirements only by being washed and recycled, and the lithium extraction efficiency is low.

Disclosure of Invention

The invention aims to solve the problems of narrow lithium-dissolving temperature range and low lithium-extracting efficiency in the prior art, and provides a method for extracting lithium in a salt lake.

In order to achieve the above object, the present invention provides a method for extracting lithium from a salt lake, comprising:

(1) contacting salt lake brine with a lithium adsorbent for adsorption to embed lithium, so as to obtain a lithium-rich adsorbent for adsorbing lithium;

(2) washing the lithium-rich adsorbent once with a first cleaning agent to obtain a first cleaning solution and a first adsorbent; wherein the first cleaning solution is returned and mixed into the salt lake brine, and the flow rate of the first cleaning solution is 6-16 BV/h;

(3) washing the first adsorbent for the second time by using a second cleaning agent to obtain a second cleaning solution and a second adsorbent; wherein the second cleaning solution is returned and mixed with the first cleaning agent, and the flow rate of the second cleaning agent is 6-16 BV/h;

(4) and (3) carrying out lithium desorption on the second adsorbent by using warm water to obtain a lithium solution, wherein the lithium desorption time is 20-90 min.

Through the technical scheme, the method for extracting lithium from salt lake brine is improved, qualified lithium solution is directly obtained by decomposing lithium through two washing and recycling steps, and the lithium solution is not required to be washed and recycled. Further, the method of the present invention uses an adsorbent having a specific chemical composition and material profile, and the temperature for lithium desorption is achieved in the range of 40-90 ℃, which is higher than that of the conventional art, so that Li is rapidly desorbed from the adsorbent, and thus the amount of water used is reduced.

Drawings

FIG. 1 is a schematic flow chart of a method for extracting lithium from a salt lake provided by the invention;

FIG. 2 is a graph showing the results of the long-period cycle conducted in example 1 of the present invention;

FIG. 3 is a graph showing the results of the long cycle in example 2 of the present invention.

Detailed Description

The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.

The invention provides a method for extracting lithium from a salt lake, which comprises the following steps of:

(1) contacting salt lake brine with a lithium adsorbent for adsorption to embed lithium, so as to obtain a lithium-rich adsorbent for adsorbing lithium;

(2) washing the lithium-rich adsorbent once with a first cleaning agent to obtain a first cleaning solution and a first adsorbent; wherein the first cleaning solution is returned and mixed into the salt lake brine, and the flow rate of the first cleaning solution is 6-16 BV/h;

(3) washing the first adsorbent for the second time by using a second cleaning agent to obtain a second cleaning solution and a second adsorbent; wherein the second cleaning solution is returned and mixed with the first cleaning agent, and the flow rate of the second cleaning agent is 6-16 BV/h;

(4) and (3) carrying out lithium desorption on the second adsorbent by using warm water to obtain a lithium solution, wherein the lithium desorption time is 20-90 min.

In the specific implementation mode provided by the invention, the step (1) is used for extracting lithium from the salt lake brine by an adsorption method, and simultaneously, the extracted brine is discharged outside. Further, the salt lake brine is subjected to microfiltration to remove impurities before being contacted with the lithium adsorbent. The microfiltration may be a method conventional in the art as long as the material obtained by filtration is achieved without affecting the adsorption function of the lithium adsorbent. Preferably, the first cleaning solution obtained in step (2) is also subjected to the microfiltration, and then mixed into the microfiltration salt lake brine.

In a particular embodiment provided herein, the lithium sorbent comprises Li, formula_xCl·2Al(OH)₃·yH₂O, wherein x is more than or equal to 0.8 and less than or equal to 1.2, and y is more than or equal to 0 and less than or equal to 2, and a binder; wherein the particle diameter of the lithium adsorbent is 1-5mm, and the length of the lithium adsorbent is 1-10 mm; preferably, the binder is at least one selected from the group consisting of polyamide, polypropylene, ethylene-vinyl acetate copolymer, polyvinyl chloride, polyethylene, polyvinylidene fluoride, polystyrene, acrylonitrile-butadiene-styrene, polymethyl methacrylate, polyoxymethylene, polyolefin ester, polyphenylene oxide, epoxy resin, and phenol resin. Preferably, the content of the adsorption material is 70 to 90 wt% based on the total amount of the lithium adsorbent.

In the specific embodiment provided by the present invention, preferably, in step (1), the lithium intercalation conditions include: the flow rate of the lithium absorbent is 1.5-4BV/h, and the contact time is 1-5 h. In the present invention, BV represents the filling volume of the lithium absorbent, and 1.5-4BV/h represents the volume amount of brine flow rate, which is 1.5-4 times the volume of the lithium absorbent per hour. The same applies hereinafter.

In the specific embodiment provided by the present invention, preferably, in the step (1), the temperature of the salt lake brine is-15 ℃ to 65 ℃.

In the specific embodiment provided by the invention, preferably, during the lithium intercalation process, the extraction rate of lithium in the salt lake brine is controlled to be 50-95%. In the method provided by the invention, the conditions are limited in each step so that the method can finally realize direct qualification of the obtained lithium solution on the whole without recycling, for example, the extraction rate of lithium in the salt lake brine is controlled within the range in the step (1).

In the specific embodiment provided by the invention, preferably, in the salt lake brine, the concentration of the Li element is 150-400mg/kg, and the concentration of the Cl element is 200-300 g/kg; the density of the salt lake brine is 1.2-1.32 g/mL. In addition, the salt lake brine may also contain other cations, such as Mg, Na, K and Ca, preferably, the content of the other cations may be 80-99g/kg of Mg element, 0.8-2g/kg of Na element, 0.3-1g/kg of K element and 20-200Mg/kg of Ca element.

The method for extracting lithium from the salt lake is preferably carried out in an adsorption tower. And the lithium adsorbent is filled in the adsorption tower, and in the lithium embedding process, the salt lake brine enters from the bottom of the adsorption tower after being subjected to precision filtration and then exits from the top of the adsorption tower. The following washing process and delithiation process are also carried out in the adsorption column.

In the specific embodiment provided by the invention, the steps (2) and (3) are used for carrying out two-step washing on the lithium-rich adsorbent. Wherein, the lithium-rich adsorbent obtained in the step (1) is subjected to a first washing step in the step (2), namely, the first washing step. Preferably, the time of the one-time washing is 3-15min, and the temperature of the one-time washing is 1-35 ℃. The first washing effect is ensured. And (3) the first cleaning solution obtained after the primary washing can be recycled for washing, and is mixed with salt lake brine for absorbing and embedding lithium in the step (1). Is beneficial to improving the lithium extraction efficiency. Preferably, the concentration of the Li element in the first cleaning solution is 160-300Mg/kg, and the concentration of the Mg element is 20-30 g/kg; the density of the first cleaning liquid is 1.1-1.2 g/mL. Preferably, in the step (2), the first cleaning agent is water and/or the second cleaning solution. Preferably the second cleaning fluid is a liquid that is,

in the invention, the first cleaning agent can enter from the bottom of the adsorption tower and exit from the top of the adsorption tower. Wherein the first cleaning agent is preferably water or a second cleaning solution. The salt content of the solution in the pores filled with the adsorbent in the adsorption tower can be reduced by one-time washing.

In the specific embodiment provided by the invention, the step (3) is used for carrying out a second washing step, namely a secondary washing step, on the lithium-rich adsorbent. Preferably, in the step (3), the time of the secondary washing is 3-15min, and the temperature of the secondary washing is 1-35 ℃.

In the specific embodiment provided by the present invention, preferably, in the step (3), the second cleaning agent is water and/or low-salt water. The low salt water is used for external introduction. Preferably, the concentration of Li element in the low-salt water is 30-120mg/kg, and the total content of cations is not more than 2 g/kg.

The second cleaning solution obtained in the step (3) of the method provided by the invention is preferably recycled and used as the first cleaning agent in the step (2). Preferably, in the second cleaning liquid, the concentration of Li element is 50-250mg/kg, and the total content of cation is not more than 10 g/kg.

In the invention, the second cleaning agent can enter from the top of the adsorption tower and exit from the bottom of the adsorption tower. Wherein the second cleaning agent is preferably water and/or low salt water.

In the specific embodiment provided by the invention, the step (4) is used for carrying out the lithium-dissolving process, and preferably, in the step (4), the flow rate of the warm water is 2-4BV/h, and the temperature of the warm water is 15-95 ℃, and preferably 40-90 ℃. I.e. the temperature for the lithium dissociation is 15-95 ℃, preferably 40-90 ℃, more preferably 55-80 ℃.

In the step (4) of the invention, water can enter from the top of the adsorption tower and exit from the bottom.

In the specific embodiment provided by the invention, the lithium solution obtained in the step (4) can be directly a qualified low magnesium-lithium ratio solution. Preferably, in the lithium solution, the concentration of the Li element is 300-700Mg/kg, the concentration of the Mg element is 1200-5600Mg/kg, the concentration of the B element is 5-20Mg/kg, and the concentration of the Na element is 50-150 Mg/kg.

The steps (1) to (4) of the lithium extraction method provided by the invention are a cycle. After the step (4) is finished, the second adsorbent can be regenerated to become a lithium adsorbent which can be contacted with salt lake brine for adsorbing and extracting lithium. In this way, the step of extracting lithium can be performed a plurality of times.

The present invention will be described in detail below by way of examples.

Example 1

The salt lake brine comprises the following elements in percentage by weight: the Li concentration is 220Mg/kg, the Cl concentration is 240g/kg, the Mg concentration is 84g/kg, and the Na concentration is 1.57 g/kg; the density was 1.32 g/mL.

Lithium adsorbent: the chemical formula of the adsorbing material is LiCl.2Al (OH)₃·1.5H₂O, the adsorbent material accounts for 79% by weight, and the binder is epoxy resin. The lithium adsorbent has an outer diameter of 1.5mm and a length of 1.5 mm. The preparation method refers to the method disclosed in CN 201711031879.6.

The total weight of the lithium adsorbent packed in the adsorption column was 22.3 tons (volume 31 m)³)。

The salt lake brine is subjected to lithium extraction according to the following three processes of lithium absorption (lithium intercalation), washing (cleaning) and lithium desorption:

and (3) lithium intercalation process: after passing through a precision filter, salt lake brine enters from the bottom of an adsorption tower and exits from the top of the adsorption tower, the flow rate is 2.5B.V./h, the duration is 3.5h, and the temperature is 20 ℃; obtaining a lithium-rich adsorbent in the adsorption tower;

and (3) cleaning:

primary washing: a second cleaning solution (composition: total cation content is 8.4g/kg, Li concentration is 218mg/kg) pre-stored in the previous cycle enters from the bottom of the adsorption tower and exits from the top, the flow rate is 10BV/h, the duration is 6min, the temperature is 20 ℃, and the lithium-rich adsorbent is cleaned; obtaining a first adsorbent and a first cleaning solution; the first cleaning solution (the composition is that the Li concentration is 248mg/kg, the total cation content is 24.5g/kg, and the density is 1.1g/mL) is recycled and mixed into the salt lake brine for the process of embedding lithium;

and (3) secondary washing: feeding pure water from the top and discharging pure water from the bottom, wherein the flow rate is 10BV/h, the duration time is 6min, and the temperature is 20 ℃; the obtained second cleaning solution enters a storage tank to be reserved for next circulation and reuse for one-time washing;

and (3) a lithium removing process: pure water enters from the top of the adsorption tower and exits from the bottom of the adsorption tower, the flow rate is 2.5BV/h, the duration is 60min, and the temperature of the pure water is 55 ℃. A lithium solution was obtained.

The above process is shown in Table 1.

TABLE 1

The extraction rate of lithium in the salt lake brine in the lithium intercalation process is 77.2 percent, and the average volume of the qualified lithium solution obtained in one cycle period is 74.2m³The Li concentration is 690Mg/kg, the Mg concentration is 1725Mg/kg, the Na concentration is 79Mg/kg, and the B concentration is 8 Mg/kg.

This process was cycled through 1800 cycles and the results are shown in fig. 2, where both the amount of lithium intercalation (i.e., the amount of Li ions adsorbed by 1kg of lithium adsorbent) and the amount of lithium deintercalation (i.e., the amount of Li ions desorbed by 1kg of lithium adsorbent) remained at relatively stable levels during the long cycle. The method provided by the invention can realize effective, continuous and stable adsorption and desorption of the lithium extracted from the salt lake.

Example 2

The conditions for the lithium extraction process according to the method of example 1 are shown in Table 2.

TABLE 2

The extraction rate of lithium in brine in the lithium intercalation process is 54.2 percent, and the average volume of qualified lithium solution obtained in one cycle is 73.9m³Li concentration 459Mg/kg, Mg concentration 1612Mg/kg, Na concentration 67Mg/kg, and B concentration 6 Mg/kg.

This process was cycled through 620 cycles, and the results are shown in FIG. 3, where both the amount of lithium intercalation and the amount of lithium deintercalation remained at relatively stable levels during the long cycle.

Example 3

The conditions for the lithium extraction process according to the method of example 1 are shown in Table 3.

TABLE 3

The extraction rate of brine lithium in the lithium intercalation process is 83.2 percent, and the average volume of qualified lithium solution obtained in one cycle period is 59.0m³Li concentration 729Mg/kg, Mg concentration 1855Mg/kg, Na concentration 80Mg/kg, and B concentration 8 Mg/kg.

Example 4

The conditions for the lithium extraction process according to the method of example 1 are shown in Table 4.

TABLE 4

The extraction rate of brine lithium in the lithium intercalation process is 88.6 percent, and the average volume of the qualified lithium solution obtained in one cycle period is 90.0m³The Li concentration was 521Mg/kg, the Mg concentration was 1776Mg/kg, the Na concentration was 79Mg/kg, and the B concentration was 9 Mg/kg.

Comparative example 1

The procedure of example 1 was followed except that the lithium adsorbent was irregular and small in particle shape and the conditions of the lithium extraction process were as shown in Table 5.

TABLE 5

Lithium solution needs to be recycled to get acceptable.

The extraction rate of brine lithium in the lithium intercalation process is 69.2 percent, and the average volume of the qualified lithium solution obtained in one cycle is 63.5m³The Li concentration was 588Mg/kg, the Mg concentration was 1966Mg/kg, the Na concentration was 110Mg/kg, and the B concentration was 9 Mg/kg.

Comparative example 2

The conditions of the lithium extraction process according to the method of comparative example 1 are shown in Table 6.

TABLE 6

The extraction rate of lithium in brine in the lithium intercalation process is 42.5 percent, and the average volume of qualified lithium solution obtained in one cycle is 50.2m³Li concentration 302Mg/kg, Mg concentration 1715Mg/kg, Na concentration 106Mg/kg, and B concentration 8 Mg/kg.

As can be seen from the results of the above examples, comparative examples and tables 1 to 6, the method provided by the invention can be used for solving the lithium process at a higher temperature (55-80 ℃), and compared with the comparative example, the steps of the lithium extraction process are saved, the lithium solution is not required to be recycled, the qualified high-concentration lithium solution can be directly obtained, and the extraction rate of the lithium in the brine is high, and the single-cycle yield is high. And the long-period operation of the examples 1 and 2 can have good long-period stability. Whereas the process of the comparative example cannot be run for a long period.

The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall within the scope of the invention.