Device for extracting lithium from salt lake brine at high yield

Abstract

The utility model relates to a device for extracting lithium from salt lake brine with high yield, which comprises an adsorption column, a lithium ion extraction column, a lithium ion extraction column and a lithium ion extraction column, the concentration device is connected to the feed liquid outlet of the adsorption column and is used for concentrating the lithium-containing eluent; the precipitation reactor is connected to the concentration device and is used for carrying out lithium phosphate precipitation reaction on the obtained concentrated solution; the precipitation reactor is connected with a phosphate adding tank and an alkali adding tank; the solid-liquid separation device is connected to the precipitation reactor and is used for separating precipitates obtained after the lithium phosphate precipitation reaction; the high-pressure reverse osmosis membrane is connected to a mother liquor outlet of the solid-liquid separation device and is used for concentrating the obtained mother liquor; an inlet of the cation exchange resin column is connected to the concentration side of the high-pressure reverse osmosis membrane and used for removing divalent or multivalent cations from the concentrated solution, and an outlet of the cation exchange resin column is connected to the phosphate adding tank.

Description

TECHNICAL FIELD

[0001] The utility model relates to the field of salt lake lithium extraction, and particularly relates to a device for extracting lithium from salt lake brine with high yield. BACKGROUND

[0002] Lithium and its compounds are widely used in batteries, medicine, aerospace, chemical industry and national defense due to their excellent performance, and play a crucial role in economic development. Lithium resources mainly come from lithium ore and salt lake brine, and the lithium content in salt lake brine is the highest, accounting for 66% of the world's lithium reserves.

[0003] The salt lake brine lithium extraction process is simple, low in cost, environmentally friendly, and suitable for market demand. Currently, the research object of lithium extraction is mainly salt lake brine. However, in the prior art, a lithium-rich solution is usually obtained from salt lake brine, and then sodium carbonate solution or CO2 is introduced under alkaline conditions to precipitate lithium to obtain lithium carbonate product. The lithium concentration in the lithium precipitation mother liquor of these lithium precipitation technologies is more than 1 g / L, and the lithium loss during the lithium precipitation process is as high as more than 15%. Chinese patent (application number 201811183552.5) discloses a method for extracting lithium carbonate from salt lake brine. The utility model has a low recovery rate of lithium carbonate, which is between 40 and 52%. Chinese patent (application number 201410296274.X) discloses a method for purifying and separating lithium carbonate mixed salt using high-temperature brine. The utility model has a low yield of lithium carbonate, which is about 50%.

[0004] Chinese patent (application number 201910735486.6) discloses a method for extracting lithium from salt lake brine and preparing lithium phosphate and its use. The extraction rate of lithium in the salt lake brine according to the method is > 94%. However, the above-mentioned utility model is limited by the grade of brine and is only suitable for brine with a lithium concentration of 2-5 g / L. This kind of brine is placed in a salt field for more than 3 years, which has a long cycle. Oxalic acid is used to remove calcium, magnesium and other ions in the brine, which not only consumes a large amount of chemicals, but also is not conducive to environmental protection. In addition, a large amount of precipitate generated will carry lithium ions, causing excessive loss of lithium.

[0005] Therefore, it is of great significance to develop a high-yield and environmentally friendly salt lake lithium extraction technology that is not limited by the type and grade of brine in the field of new energy. UTILITY MODEL CONTENTS

[0006] The utility model aims to provide a kind of method for extracting lithium from salt lake brine with high yield, including using lithium extraction adsorbent to adsorb lithium in salt lake brine, then leaching, desorption, obtaining lithium-containing desorption solution, then concentrating lithium-containing desorption solution, obtaining lithium-containing concentrated solution;Phosphate-containing reagent can be added to lithium-containing desorption solution or concentrated solution, and reaction temperature and pH value can be controlled to prepare lithium phosphate.

[0007] A method for high-yield lithium extraction from salt lake brine includes the following steps:

[0008] Step 1: Contact the salt lake brine with the adsorbent to adsorb lithium ions;

[0009] Step 2: The adsorbent obtained in Step 1 is rinsed and eluted to obtain a lithium-containing desorption solution;

[0010] Step 3: The lithium-containing desorption solution obtained in Step 2 is concentrated or not, and a phosphate solution is added to separate the precipitate to obtain lithium phosphate.

[0011] In step 1, the brine can be made from chloride-type brine, magnesium sulfate subtype brine, carbonate-type brine, deep underground brine, etc. It can be extracted directly from underground or the surface, or it can be brine that has been evaporated and concentrated to precipitate salt. The lithium concentration in the brine is between 0.02 and 5.0 g / L.

[0012] In step 1, the adsorbent is at least one of aluminum salt adsorbent, titanium adsorbent, or manganese adsorbent.

[0013] In step 2, the lithium concentration in the lithium-containing desorption solution is 0.4–12.0 g / L.

[0014] In step 3, when the lithium ion concentration is 0.4–1.5 g / L, it needs to be concentrated.

[0015] The concentration process uses one or more of the following: reverse osmosis membrane, forward osmosis membrane, electrodialysis, and evaporation device.

[0016] The phosphate solution mentioned refers to one or more combinations of phosphoric acid, disodium hydrogen phosphate, sodium dihydrogen phosphate, sodium phosphate, dipotassium hydrogen phosphate, potassium dihydrogen phosphate, potassium phosphate, diammonium hydrogen phosphate, ammonium dihydrogen phosphate, and ammonium phosphate.

[0017] The phosphate solution concentration is 15–50 wt%, preferably 25–40 wt%.

[0018] The amount of phosphate-containing solution used is calculated based on a phosphate to lithium ion molar ratio of 1:3, and phosphate can be in excess by 3 to 15 wt%.

[0019] The pH value of the phosphate-containing solution can be controlled above 9.0, preferably 10.0 to 14.0.

[0020] The pH value is controlled by adding alkali.

[0021] The alkali mentioned refers to one or more combinations of sodium hydroxide, sodium carbonate, potassium hydroxide, potassium carbonate, ammonia, ammonium carbonate, and ammonium bicarbonate.

[0022] The reaction temperature after adding phosphate solution is controlled at 30-100℃.

[0023] It also includes step 5, in which the mother liquor obtained in step 4 is concentrated using a high-pressure reverse osmosis membrane, and then divalent or polyvalent cations are removed by cation exchange resin. The resulting permeate is then replenished with phosphate and reused.

[0024] An apparatus for high-yield lithium extraction from salt lake brine, comprising:

[0025] Adsorption columns are used to adsorb lithium ions from salt lake brine.

[0026] A concentration device, connected to the feed outlet of the adsorption column, is used to concentrate lithium-containing eluent.

[0027] A precipitation reactor, connected to a concentration device, is used to perform a lithium phosphate precipitation reaction on the obtained concentrate; and a phosphate addition tank and an alkali addition tank are connected to the precipitation reactor.

[0028] A solid-liquid separation device, connected to a precipitation reactor, is used to separate the precipitate after the lithium phosphate precipitation reaction;

[0029] A high-pressure reverse osmosis membrane is connected to the mother liquor outlet of the solid-liquid separation device and is used to concentrate the obtained mother liquor.

[0030] The cation exchange resin column has its inlet connected to the concentration side of the high-pressure reverse osmosis membrane for removing divalent or polyvalent cations from the concentrate, and its outlet connected to the phosphate addition tank.

[0031] The adsorption column is filled with one of aluminum salt adsorbent, titanium adsorbent, or manganese adsorbent.

[0032] The concentration device is one or a combination of several of the following: reverse osmosis membrane, forward osmosis membrane, electrodialysis unit, or evaporation unit.

[0033] The phosphate added to the tank is a solution of any one of phosphoric acid, disodium hydrogen phosphate, sodium dihydrogen phosphate, sodium phosphate, dipotassium hydrogen phosphate, potassium dihydrogen phosphate, potassium phosphate, diammonium hydrogen phosphate, ammonium dihydrogen phosphate, and ammonium phosphate.

[0034] The solid-liquid separation device is one or a combination of centrifugal separation device, sedimentation separation device or membrane separation device.

[0035] The cation exchange resin is filled with sodium-type cation exchange resin.

[0036] Beneficial effects

[0037] Compared with the prior art, the present invention has the following beneficial effects: (1) The present invention has a wider range of applications and is almost not limited by the type and grade of brine. It can be applied to brine with lithium concentration of 0.02 to 5.0 g / L, such as chloride-type salt lake brine, magnesium sulfate subtype salt lake brine, carbonate-type salt lake brine, and deep underground brine. It can be brine directly extracted from underground or the surface, or brine that has been evaporated and concentrated to precipitate salt. (2) The lithium recovery rate is high during the lithium precipitation process, ranging from 93.0% to 99.5%. (3) The preparation process described in the present invention is simple to operate, low in cost, and does not require the consumption of a large amount of chemical reagents, and has no environmental hazards. Attached Figure Description

[0038] Figure 1 This is a flowchart of Example 1, which describes a method for high-yield lithium extraction from salt lake brine.

[0039] Figure 2 This is a diagram of the device in this patent.

[0040] The components include: 1. Adsorption column; 2. Concentration device; 3a. Phosphate addition tank; 3b. Alkali addition tank; 4. Precipitation reactor; 5. Solid-liquid separation device; 6. High-pressure reverse osmosis membrane; and 7. Cation exchange resin column. Detailed Implementation

[0041] The main processes and implementation procedures of this patent are detailed below:

[0042] (1) The brine from the salt lake is fed into a device containing a lithium extraction adsorbent for adsorption. After the adsorption is completed, the lithium extraction adsorbent is rinsed and desorbed, and the lithium-containing desorbed liquid is collected.

[0043] (2) The lithium-containing desorption solution is sent to a concentration unit for concentration to obtain a lithium-containing concentrate;

[0044] (3) The lithium-containing desorption solution or lithium-containing concentrate is sent into the lithium precipitation device, a phosphate-containing solution is added, and the reaction pH and reaction temperature are controlled. The reaction precipitate is collected as lithium phosphate.

[0045] (4) After the lithium phosphate is separated, the mother liquor obtained is concentrated by high pressure reverse osmosis membrane, and then divalent or polyvalent cations are removed by cation exchange resin. The permeate is then replenished with phosphate and reused.

[0046] Optionally, the brine may be a brine made from chloride-type brine, magnesium sulfate subtype brine, carbonate-type brine, or deep underground brine, etc. It may be extracted directly from underground or the surface, or it may be brine that has been evaporated and concentrated to precipitate salt. The lithium concentration in the brine is between 0.02 and 5.0 g / L.

[0047] Optionally, the lithium extraction adsorbent may be at least one of aluminum salt adsorbent, titanium adsorbent, or manganese adsorbent.

[0048] Optionally, the lithium concentration in the lithium-containing desorption solution is 0.4–12.0 g / L; wherein, the lithium-containing desorption solution with a lithium concentration of 0.4–1.5 g / L is sent to a concentration device; the lithium-containing desorption solution with a lithium concentration of 1.5–12.0 g / L can be sent to a concentration device or directly sent to a lithium precipitation device.

[0049] Optionally, the concentration device may be one or more combinations of reverse osmosis membrane, forward osmosis membrane, electrodialysis, and evaporation device.

[0050] Optionally, the lithium concentration in the lithium-containing concentrate is 1.5 to 20.0 g / L.

[0051] Optionally, the phosphate-containing solution may be one or more combinations of phosphoric acid, disodium hydrogen phosphate, sodium dihydrogen phosphate, sodium phosphate, dipotassium hydrogen phosphate, potassium dihydrogen phosphate, potassium phosphate, diammonium hydrogen phosphate, ammonium dihydrogen phosphate, and ammonium phosphate.

[0052] The concentration of the phosphate-containing solution is 15–50 wt%.

[0053] More preferably, the concentration of the phosphate-containing solution is 25–40 wt%.

[0054] The amount of phosphate-containing solution used is calculated based on a phosphate to lithium ion molar ratio of 1:3, and phosphate can be in excess by 3 to 15 wt%.

[0055] More preferably, the phosphate group may be in excess by 5-10 wt%.

[0056] Optionally, the pH value can be controlled above 9.0.

[0057] Further preferably, the pH value can be controlled between 10.0 and 14.0.

[0058] Optionally, the pH control is achieved by adding one or more of sodium hydroxide, sodium carbonate, potassium hydroxide, potassium carbonate, ammonia, ammonium carbonate, and ammonium bicarbonate.

[0059] Optionally, the reaction temperature is controlled between 30 and 100°C.

[0060] Further preferably, the reaction temperature is controlled at 60–90°C.

[0061] Optionally, the lithium yield during the lithium precipitation process is between 93.0% and 99.5%.

[0062] The lithium phosphate described in this invention has a purity of not less than 90%.

[0063] Based on the above process, the device structure provided by this patent is as follows: Figure 2 As shown, it includes:

[0064] Adsorption column 1 is used for the adsorption of lithium ions in salt lake brine;

[0065] Concentration device 2 is connected to the feed outlet of adsorption column 1 and is used to concentrate lithium-containing eluent.

[0066] Precipitation reactor 4 is connected to concentration device 2 and is used to carry out lithium phosphate precipitation reaction on the obtained concentrate; and phosphate addition tank 3a and alkali addition tank 3b are connected to precipitation reactor 4.

[0067] Solid-liquid separation device 5 is connected to precipitation reactor 4 and is used to separate the precipitate after the lithium phosphate precipitation reaction;

[0068] High-pressure reverse osmosis membrane 6 is connected to the mother liquor outlet of solid-liquid separation device 5 and is used to concentrate the obtained mother liquor;

[0069] The cation exchange resin column 7 has its inlet connected to the concentration side of the high-pressure reverse osmosis membrane 6 for removing divalent or polyvalent cations from the concentrate, and its outlet connected to the phosphate addition tank 3.

[0070] The adsorption column 1 is filled with one of aluminum salt adsorbent, titanium adsorbent or manganese adsorbent.

[0071] The concentration device 2 is one or a combination of several of the following: reverse osmosis membrane, forward osmosis membrane, electrodialysis unit, or evaporation unit.

[0072] The phosphate addition tank 3 contains a solution of any one of the following: phosphoric acid, disodium hydrogen phosphate, sodium dihydrogen phosphate, sodium phosphate, dipotassium hydrogen phosphate, potassium dihydrogen phosphate, potassium phosphate, diammonium hydrogen phosphate, ammonium dihydrogen phosphate, and ammonium phosphate.

[0073] The solid-liquid separation device 5 is one or a combination of centrifugal separation device, sedimentation separation device or membrane separation device.

[0074] The cation exchange resin 7 is filled with sodium-type cation exchange resin.

[0075] Example 1

[0076] The brine used in this embodiment is a chloride-type brine, containing sodium, calcium, lithium, boron, and chloride ions at concentrations of 89.0 g / L, 20.5 g / L, 0.02 g / L, 0.21 g / L, and 199.5 g / L, respectively. Figure 1 The diagram shows the flow of this embodiment. The method of this embodiment includes the following steps:

[0077] The brine was fed into a device containing an aluminum-based adsorbent for adsorption. After adsorption, the brine was washed and desorbed in sequence, and the lithium-containing desorbed liquid was collected with a lithium concentration of 0.4 g / L.

[0078] The lithium-containing desorption solution was fed into a reverse osmosis membrane unit for concentration to obtain a lithium-containing concentrate with a lithium concentration of 1.5 g / L.

[0079] The lithium-containing concentrate was fed into a lithium precipitation device and heated to 60°C. A 25 wt% phosphoric acid solution was added, ensuring a 5 wt% phosphate excess. The pH was adjusted to 10.0 with sodium hydroxide solution. The solution was filtered, washed with hot water, separated, and dried to obtain a white powder, which is lithium phosphate with a purity of 90.1%. The separated mother liquor was concentrated using a high-pressure reverse osmosis membrane, and then passed through a cation exchange resin to remove divalent or polyvalent cations (mainly Mg2+), resulting in a solution mainly composed of excess phosphate with increased concentration. After replenishing with phosphate, the solution was reused.

[0080] The lithium recovery rate during the lithium precipitation process was 93.3%.

[0081] Example 2

[0082] This embodiment uses a magnesium sulfate subtype salt lake brine, in which the concentrations of the main ions sodium, magnesium, lithium, boron, chloride, and sulfate are 91.0 g / L, 30.9 g / L, 0.3 g / L, 0.35 g / L, 190.4 g / L, and 25.1 g / L, respectively. The specific operating steps are as follows:

[0083] The brine was fed into a device containing a manganese-based adsorbent for adsorption. After adsorption, the brine was washed and desorbed in sequence, and the lithium-containing desorbed liquid was collected with a lithium concentration of 0.8 g / L.

[0084] The lithium-containing desorption solution was sequentially fed into a reverse osmosis membrane, a forward osmosis membrane, an electrodialysis unit, and an evaporation unit for concentration to obtain a lithium-containing concentrate with a lithium concentration of 20.1 g / L.

[0085] The lithium-containing concentrate was fed into a lithium precipitation device and heated to 90°C. A 40 wt% disodium hydrogen phosphate solution was added to ensure a 10 wt% phosphate excess. The pH was adjusted to 14.0 with sodium carbonate solution. The solution was filtered, washed with hot water, and dried to obtain a white powder, which is lithium phosphate with a purity of 98.3%. The separated mother liquor was concentrated using a high-pressure reverse osmosis membrane, and then passed through a cation exchange resin to remove divalent or polyvalent cations (mainly Mg2+), resulting in a solution mainly composed of excess phosphate with increased concentration. After replenishing with phosphate, the solution was reused.

[0086] The lithium recovery rate during the lithium precipitation process was 99.5%.

[0087] Example 3

[0088] This embodiment uses a carbonate-type salt lake brine, in which the concentrations of the main ions sodium, magnesium, lithium, boron, chloride, carbonate, and bicarbonate are 39.0 g / L, 1.3 g / L, 0.15 g / L, 0.75 g / L, 58 g / L, 2.1 g / L, and 1.4 g / L, respectively. The specific operating steps are as follows:

[0089] The brine was fed into a device containing a titanium-based adsorbent for adsorption. After adsorption, the brine was washed and desorbed in sequence, and the lithium-containing desorbed solution was collected with a lithium concentration of 12.2 g / L.

[0090] The lithium-containing desorption solution was directly fed into a lithium precipitation device and heated to 80°C. A 30 wt% sodium dihydrogen phosphate solution was added to ensure an 8 wt% phosphate excess. The pH was adjusted to 12.0 with potassium hydroxide solution. The solution was filtered, washed with hot water, and dried to obtain a white powder, which is lithium phosphate with a purity of 98.5%. The separated mother liquor was concentrated using a high-pressure reverse osmosis membrane, and then passed through a cation exchange resin to remove divalent or polyvalent cations (mainly Mg2+), resulting in a solution mainly composed of residual phosphate with increased concentration. After replenishing with phosphate, the solution was reused.

[0091] The lithium recovery rate during the lithium precipitation process was 99.2%.

[0092] Example 4

[0093] This embodiment uses a brine that has been evaporated and concentrated to precipitate salt. The concentrations of the main ions magnesium, sodium, lithium, boron, and chloride ions in the brine are 118 g / L, 2.0 g / L, 5.0 g / L, 3.0 g / L, and 300 g / L, respectively. The specific operating steps are as follows:

[0094] The brine was fed into a device containing an aluminum-based adsorbent for adsorption. After adsorption, the brine was washed and desorbed in sequence, and the lithium-containing desorbed liquid was collected with a lithium concentration of 1.2 g / L.

[0095] The lithium-containing desorption solution was sequentially fed into a reverse osmosis membrane and an electrodialysis unit for concentration to obtain a lithium-containing concentrate with a lithium concentration of 10.3 g / L.

[0096] The lithium-containing desorption solution was directly fed into a lithium precipitation device and heated to 70°C. A 35 wt% sodium phosphate solution was added to ensure a 7 wt% phosphate excess. The pH was adjusted to 13.0 with potassium carbonate solution. The solution was filtered, washed with hot water, and dried to obtain a white powder, which is lithium phosphate with a purity of 93.1%. The separated mother liquor was concentrated using a high-pressure reverse osmosis membrane, and then passed through a cation exchange resin to remove divalent or polyvalent cations (mainly Mg2+), resulting in a solution mainly composed of excess phosphate with increased concentration. After replenishing with phosphate, the solution was reused.

[0097] The lithium recovery rate during the lithium precipitation process was 99.0%.

[0098] Example 5

[0099] The difference between this embodiment and Embodiment 3 is that the brine is fed into a device containing a manganese-based adsorbent for adsorption. After adsorption, rinsing and desorption are performed sequentially, and the lithium-containing desorbate is collected with a lithium concentration of 6.2 g / L. The lithium recovery rate during the lithium precipitation process is 98.3%.

[0100] All other conditions are exactly the same as in Example 3.

[0101] Example 6

[0102] The difference between this embodiment and Embodiment 5 is that the lithium-containing desorption solution is directly fed into the lithium precipitation apparatus and heated to 80°C. A mixed solution of dipotassium hydrogen phosphate, potassium dihydrogen phosphate, and potassium phosphate (30 wt%) is added to ensure an 8 wt% excess of phosphate. The pH is adjusted to 11.0 with ammonia solution, filtered, washed with hot water, and dried to obtain a white powder, which is lithium phosphate with a purity of 98.1%. The lithium yield during the precipitation process is 98.0%.

[0103] All other conditions are exactly the same as in Example 5.

[0104] Example 7

[0105] The difference between this embodiment and Embodiment 4 is that the lithium concentration of the brine used, after evaporation and concentration to precipitate salts, is 2.1 g / L. The lithium-containing desorption solution is directly fed into a lithium precipitation apparatus and heated to 80°C. A mixed solution of diammonium hydrogen phosphate, ammonium dihydrogen phosphate, and ammonium phosphate (30 wt%) is added to ensure a 6 wt% excess of phosphate. The pH is adjusted to 11.0 using a mixed solution of ammonium carbonate and ammonium bicarbonate. After filtration, washing with hot water, and drying, a white powder is obtained, which is lithium phosphate with a purity of 93.1%. The lithium yield during the precipitation process is 98.5%.

[0106] All other conditions are exactly the same as in Example 4.

[0107] Comparative Example 1

[0108] The difference between this embodiment and Example 1 is that a sodium carbonate solution with a mass fraction of 25 wt% is added to the lithium-containing concentrate to obtain lithium carbonate with a purity of 90.1%, wherein the lithium yield during the lithium precipitation process is 35.0%.

[0109] All other conditions are exactly the same as in Example 1.

[0110] Comparative Example 2

[0111] The difference between this embodiment and Example 2 is that a sodium carbonate solution with a mass fraction of 25 wt% was added to the lithium-containing concentrate to obtain lithium carbonate with a purity of 95.6%, wherein the lithium yield during the lithium precipitation process was 80.2%.

[0112] All other conditions are exactly the same as in Example 2.

[0113] The main technical indicators of each embodiment of this utility model are shown in Table 1.

[0114] Table 1

[0115]

Claims

1. A device for high-yield lithium extraction from salt lake brine, characterized in that, The application relates to a lithium extraction method from salt lake brine, comprising the following steps: (1) an adsorption column (1) is used for adsorbing lithium ions from salt lake brine; (2) a concentration device (2) is connected to the outlet of the adsorption column (1) and is used for concentrating lithium-containing eluent; (3) a precipitation reactor (4) is connected to the concentration device (2) and is used for carrying out lithium phosphate precipitation reaction on the obtained concentrated solution; a phosphate adding tank (3a) and an alkali adding tank (3b) are connected to the precipitation reactor (4); (4) a solid-liquid separation device (5) is connected to the precipitation reactor (4) and is used for separating the precipitate after the lithium phosphate precipitation reaction; (5) a high-pressure reverse osmosis membrane (6) is connected to the mother liquor outlet of the solid-liquid separation device (5) and is used for concentrating the obtained mother liquor; and (6) a cation exchange resin column (7) is connected to the concentrated side of the high-pressure reverse osmosis membrane (6) and is used for removing divalent or multivalent cations from the concentrated solution, and the outlet of the cation exchange resin column (7) is connected to the phosphate adding tank (3). The adsorption column (1) is filled with one of an aluminum salt adsorbent, a titanium-based adsorbent or a manganese-based adsorbent. The concentration device (2) is one or a combination of reverse osmosis membranes, forward osmosis membranes, electrodialyzers or evaporation devices. The phosphate adding tank (3) is filled with a solution of any one of phosphoric acid, disodium hydrogen phosphate, sodium dihydrogen phosphate, sodium phosphate, dipotassium hydrogen phosphate, potassium dihydrogen phosphate, potassium phosphate, diammonium hydrogen phosphate, ammonium dihydrogen phosphate or ammonium phosphate. The solid-liquid separation device (5) is one or a combination of centrifugal separation devices, sedimentation separation devices or membrane separation devices. The cation exchange resin column (7) is filled with sodium type cation exchange resin.

2. The apparatus for high recovery of lithium from salt lake brine according to claim 1, characterized in that, ​ 3. The apparatus for high recovery of lithium from salt lake brine of claim 1, wherein, ​ 4. The apparatus for high recovery of lithium from salt lake brine of claim 1, wherein, ​ 5. The apparatus for high recovery of lithium from salt lake brine of claim 1, wherein, ​ 6. The apparatus for high recovery of lithium from salt lake brine of claim 1, wherein, ​

Images