A method and system for high boron salt lake water co-production of boron and lithium

Abstract

The application discloses a high-boron salt lake water boron-lithium co-production method and system, comprising the following steps: step one, adopting boron adsorption resin to adsorb and treat high-boron salt lake water, and obtaining boron adsorption resin after adsorption and salt lake water after boron removal; step two, adopting an acid solution to desorb and treat the boron adsorption resin, and obtaining boron desorption liquid; and step three, adjusting the pH of the salt lake water after boron removal to 3-6.5, and adopting an aluminum lithium adsorbent to adsorb and treat the salt lake water after boron removal, and extracting lithium in the salt lake water after boron removal. The application reduces the acid liquid consumption of the subsequent lithium extraction acidification stage by greater than or equal to 60% compared with the traditional process, greatly reduces the acid liquid procurement and transportation cost; at the same time, the yield of the by-product crude boric acid is greater than or equal to 80%, further reduces the unit cost of lithium extraction, finally realizes the comprehensive cost reduction of greater than or equal to 30%, and solves the core pain point of high lithium extraction cost of high-boron salt lake.

Description

Invention Field This invention belongs to the field of resource recycling, specifically relating to a method for co-producing boron and lithium from high-boron salt lake water. Background Technology

[0001] Lithium, as a core material in the new energy industry, has its resource reserves and efficient extraction directly impacting the development of new energy. Lithium extraction from salt lakes, due to its large resource reserves and high cost potential, has become a core technological direction for lithium resource acquisition. However, for carbonate-rich, high-boron salt lakes such as those in Tibet, the presence of carbonates and borates forms a natural pH buffer system, with the pH value remaining stable between 7 and 10, posing a significant challenge to the efficient extraction of lithium resources.

[0002] In existing technologies, aluminum-based adsorbents are commonly used materials for lithium extraction from salt lakes. However, when used in high-boron, high-alkalinity salt lakes, the pH value of the lake water must first be adjusted to a suitable range of 3-6.5, a process that consumes a large amount of acid. The unique geographical environment and scarce resources of the Tibet region mean that the long transportation distances, high costs, and safety risks associated with acid transportation severely restrict large-scale development.

[0003] To address the dependence on acid solutions, the industry has attempted to use bipolar membrane technology to produce its own acid and alkali solutions to replace purchased acid solutions. However, in practice, it has been found that this technology produces a large amount of residual alkali solution, which is difficult to process and the overall process cost remains high, failing to fundamentally solve the cost and compatibility issues. Furthermore, existing processes only focus on lithium extraction, and boron in the salt lake is not effectively recovered, resulting in resource waste and potential environmental hazards.

[0004] Therefore, developing a co-production process that can reduce the cost of lithium acid extraction, recover boron, and produce high-value boric acid as a byproduct has become a key requirement for the comprehensive utilization of high-boron salt lake resources. Summary of the Invention

[0005] To address the shortcomings of existing lithium extraction processes from high-boron salt lakes, such as high acid consumption, high cost, and ineffective boron recovery, this invention provides a boron-lithium co-production process. The core objective is to reduce acid consumption during lithium extraction through pre-treatment to remove boron, while simultaneously preparing boric acid as a byproduct from the recovered boron, thus achieving the dual goals of low-cost lithium resource development and efficient boron resource recovery. This invention is specifically implemented using the following technical solution: A method for co-producing boron and lithium from high-boron salt lake water includes the following steps: Step 1: Boron adsorption resin is used to adsorb high-boron salt lake water to obtain boron adsorption resin and boron-removed salt lake water; Step 2: Desorb the adsorbed boron resin using an acid solution to obtain a boron desorption solution; Step 3: Adjust the pH of the boron-removed salt lake water to 3-6.5, and use an aluminum-based lithium adsorbent for adsorption treatment to extract lithium from the boron-removed salt lake water.

[0006] Optionally, the high-boron salt lake water is salt lake water with a pH value of 8-10; the boron content in the high-boron salt lake water is greater than 100 mg / L.

[0007] Optionally, the boron adsorption resin in step one is Seplite® LSC-800 resin.

[0008] Optionally, in step one, the adsorption treatment includes loading boron adsorption resin into a column and then adding high-boron salt lake water for column adsorption. The adsorption treatment temperature is 0-50℃, and the flow rate of the high-boron salt lake water is 0.5~50 BV / h.

[0009] Optionally, in step two, the acid solution is a hydrochloric acid solution with a mass concentration of 1%-31%; in the desorption treatment, the acid solution flow rate is 0.1~20 BV / h, the temperature is 5-50℃, and the acid solution volume is 0.1~10 BV.

[0010] Optionally, in step two, the desorbed boron adsorption resin is regenerated using boron-removed salt lake water and then returned to step one for reuse.

[0011] Optionally, in step two, the boron desorption solution is concentrated and crystallized to obtain boric acid.

[0012] Optionally, in step three, the adsorption treatment includes loading the aluminum-based lithium adsorbent into a column and then adding it to the boron-removed salt lake water for column adsorption. The adsorption treatment temperature is 0-50℃, and the flow rate of the boron-removed salt lake water is 0.5~10 BV / h.

[0013] A boron-lithium co-production system for high-boron salt lake water includes: Boron adsorption resin column; The adsorption zone is used to adsorb high-boron salt lake water with boron adsorption resin to obtain adsorbed boron adsorption resin and boron-removed salt lake water. The desorption zone is used to desorb the adsorbed boron adsorption resin with an acid solution to obtain a boron desorption solution. The lithium extraction device is used to adjust the pH of the boron-removed salt lake water to 3-6.5, and then use an aluminum-based lithium adsorbent for adsorption treatment to extract lithium from the boron-removed salt lake water.

[0014] Optionally, the system further includes: The washing area is used to clean the boron adsorption resin after adsorption. The acid washing zone is used to clean the boron adsorption resin after desorption treatment in the desorption zone. The tail liquid transformation zone is used to treat the boron adsorption resin after it has been washed in the acid washing zone with boron-removed salt lake water for top water treatment and degassing, so that the boron adsorption resin can be transformed and regenerated. The system cycles through the boron adsorption resin column in the order of adsorption zone, washing zone, desorption zone, acid washing zone, and tail liquid conversion zone. Preferably, the system further includes a boric acid extraction device for concentrating and crystallizing the boron desorption solution to obtain boric acid.

[0015] By employing the above-described technology, the beneficial effects of the present invention compared to the prior art are as follows: Significantly reduce lithium extraction costs: By pre-treating boron, the acid consumption in the subsequent lithium extraction acidification stage is reduced by ≥60% compared to traditional processes, greatly reducing acid procurement and transportation costs; at the same time, the yield of by-product crude boric acid is ≥80%, further reducing the unit cost of lithium extraction, ultimately achieving a comprehensive cost reduction of ≥30%, solving the core pain point of high lithium extraction costs in high-boron salt lakes.

[0016] Achieving comprehensive resource utilization: This invention not only efficiently extracts lithium resources, but also realizes the recycling of boron, transforming boron, which was originally an impurity, into high-value boric acid byproducts, thereby improving the utilization rate of salt lake resources and avoiding resource waste.

[0017] High process adaptability: It adopts boron removal resin and continuous ion exchange system, which is adapted to the water quality characteristics of high boron salt lake in Tibet (pH 7-10). At the same time, it can withstand special environments such as high altitude and low temperature. The process has strong stability, boron adsorption rate ≥99%, lithium recovery rate ≥90%, and product purity reaches battery grade standard.

[0018] It combines environmental protection and economic efficiency: the preparation of boric acid from the recovered solution does not require the addition of additional reagents, and the resin can be recycled and reused; the acid reuse design in the water washing acid zone further reduces material consumption, and the entire process has no harmful waste emissions, which meets the needs of green chemical development. Attached Figure Description

[0019] To more clearly illustrate the specific embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the specific embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0020] Figure 1 This is a schematic diagram of the system structure of the present invention. Detailed Implementation

[0021] Various exemplary embodiments of the present invention will now be described in detail. This detailed description should not be considered as a limitation of the present invention, but rather as a more detailed description of certain aspects, features, and embodiments of the present invention. It should be understood that the terminology used in this invention is merely for describing particular embodiments and is not intended to limit the present invention.

[0022] Furthermore, regarding the numerical ranges in this invention, it should be understood that each intermediate value between the upper and lower limits of the range is also specifically disclosed. Any stated value or intermediate value within a stated range, as well as each smaller range between any other stated value or intermediate value within said range, are also included in this invention. The upper and lower limits of these smaller ranges may be independently included or excluded from the range.

[0023] Unless otherwise stated, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art. While only preferred methods and materials have been described herein, any methods and materials similar to or equivalent to those described herein may be used in the implementation or testing of this invention.

[0024] The terms “include,” “including,” “have,” “contain,” etc., used in this article are all open-ended terms, meaning that they include but are not limited to.

[0025] This invention proposes a process for the co-production of boron and lithium from high-boron salt lakes, comprising the following steps: 1) Pre-treatment for boron removal: High-boron salt lake brine is passed through an adsorption device filled with boron removal resin (provided by our company). The brine flow rate is controlled so that the boron removal resin adsorbs boron from the brine, resulting in boron-removed brine; wherein the boron adsorption rate of the boron removal resin is ≥99%; 2) Resin Desorption and Boron Recovery: After the boron removal resin becomes saturated, hydrochloric acid desorption solution is introduced into the adsorption device for desorption treatment, and the desorption solution is collected; the desorption rate of the boron removal resin is 100%. 3) Boric acid preparation: The eluent collected in step 2 is concentrated, crystallized, and filtered to obtain crude boric acid byproduct, with a crude boric acid yield of ≥80%; 4) Lithium extraction: The pH of the boron-removed brine obtained in step 1 is adjusted to 3-6.5, and then passed into a lithium extraction device filled with aluminum-based lithium adsorbent for lithium adsorption, desorption, and purification to obtain battery-grade lithium products (Li2CO3 purity ≥ 99.5%) with a lithium recovery rate ≥ 90%. 5) Resin regeneration: The boron-removing resin after analysis in step 2 can be directly returned to step 1 for recycling.

[0026] Furthermore, the adsorption device mentioned in step 1 is a fixed bed / moving bed. The system includes four major areas: adsorption zone, washing zone, desorption zone, and top water zone. It can operate synchronously to complete the adsorption and regeneration of resin at the same time.

[0027] Furthermore, in step 2, the mass concentration of the hydrochloric acid eluent is 1%-31%, and the consumption of 100% hydrochloric acid per cubic meter of boron removal resin is 20-30 kg; during the eluent process, the temperature inside the adsorption device is controlled at 5-50℃, and the resin column switching time is 10-200 min.

[0028] Furthermore, in step 4, the acid consumption required for brine acidification after boron removal is reduced by ≥60% compared to the traditional aluminum-based adsorbent process, and the overall cost of lithium extraction from high-boron salt lakes is reduced by ≥30% compared to the existing process.

[0029] The core mechanism of this invention is as follows: Resin adsorption mechanism: Boron removal resin reacts with B(OH)4 in brine - An adsorption reaction occurs, and the reaction equation is:

[0030] Resin desorption mechanism: Hydrochloric acid desorption solution provides H+ + This causes adsorbed boron to detach from the resin, and the reaction formula is:

[0031] Simultaneously, N-methylglucosamine undergoes a protonation reaction:

[0032] Resin regeneration mechanism: Sodium carbonate deprotonates the resin, restoring its adsorption activity. The reaction formula is as follows:

[0033] Sodium carbonate in the lake water deprotonates the resin and restores its activity. This process occurs simultaneously with adsorption. After regenerating the resin with acid, it can directly adsorb boron again without the need for special activation and transformation.

[0034] Acid-saving mechanism: When high-boron brine is directly acidified, approximately 2 equivalents of H are required per mole of boron. + (1 equivalent reduction of B(OH)4) - (1 equivalent to overcome the buffering effect); after pre-boron removal, the buffering effect of the brine is weakened, acidification only needs to neutralize its own alkalinity, the acid consumption is reduced and is unrelated to the boron content, and the acid saving benefit is quantified as 2 times the molar amount of boron.

[0035] Based on the above method, the present invention also proposes a boron-lithium co-production system for high-boron salt lake water, which adopts a continuous ion exchange system and includes: a boron adsorption resin column; The adsorption zone is used to adsorb high-boron salt lake water with boron adsorption resin to obtain adsorbed boron adsorption resin and boron-removed salt lake water. The washing area is used to clean the boron adsorption resin after adsorption. The desorption zone is used to desorb the adsorbed boron adsorption resin with an acid solution to obtain a boron desorption solution. The acid washing zone is used to clean the boron adsorption resin after desorption treatment in the desorption zone. The tail liquid transformation zone is used to treat the boron adsorption resin after it has been washed in the acid washing zone with boron-removed salt lake water for top water treatment and degassing, so that the boron adsorption resin can be transformed and regenerated. The system circulates the boron adsorption resin column in the order of adsorption zone, washing zone, desorption zone, acid washing zone, and tail liquid transformation zone. The lithium extraction device is used to adjust the pH of the boron-removed salt lake water to 3-6.5, and then use an aluminum-based lithium adsorbent for adsorption treatment to extract lithium from the boron-removed salt lake water.

[0036] Preferably, the system further includes a boric acid extraction device for concentrating and crystallizing the boron desorption solution to obtain boric acid.

[0037] Example 1: Fixed-bed boron-lithium co-production process This embodiment uses brine from a high-boron salt lake in Tibet as raw material. The specific components were analyzed as follows:

[0038] The specific steps of the fixed-bed boron-lithium co-production process are as follows: Pre-boron removal treatment: Take 50 mL Seplite® LSC-800 boron removal resin and pack it into a chromatography column (inner diameter × height is 2.5 cm × 30 cm). At a temperature of 25°C, pass salt lake brine into the chromatography column at a flow rate of 1 BV / h until the resin adsorption is saturated. The saturated adsorption capacity of the resin is 5.51 g / L.

[0039] Resin eluent and boron recovery: At 25°C, 41.6 mL of 3% hydrochloric acid eluent (corresponding to 25 kg of hydrochloric acid per cubic meter of resin) was passed into the saturated adsorption column at a flow rate of 1 BV / h for eluent extraction. Pure water was then passed through as the driving force, and the final total volume of the eluent collected was 100 mL. The boron content in the eluent was 2756.4 mg / L, and the resin eluent extraction rate was calculated to be 100%.

[0040] Boric acid preparation: The eluent was concentrated in a rotary evaporator until the boron concentration in the system was 20 g / L (concentrated to 10%-15% of the original volume); after concentration, it was cooled to 10-15 °C for crystallization, and the crude boric acid product was obtained by filtration. The yield of crude boric acid was calculated to be 82.5%. The initial boron concentration of the eluent was about 2-3 g / L, and the pH was between 1 and 2.

[0041] Lithium extraction: The pH of the boron-removed brine was adjusted to 4.5 with hydrochloric acid. At 25°C, the brine was passed through a chromatography column packed with aluminum-based lithium adsorbent (provided by the company) at a flow rate of 1 BV / h for adsorption, desorption, and purification. The final product was Li2CO3 with a purity of 99.6% and a lithium recovery rate of 91.2%. The amount of hydrochloric acid consumed per liter of brine for acid adjustment in this stage was 33 ml, which is 66.33% lower than that of the traditional direct acidification process.

[0042] Resin regeneration: The boron removal resin after analysis has regained its adsorption activity and can be recycled for boron removal treatment.

[0043] Example 2 Pre-boron removal treatment: Take 50 mL Seplite® LSC-800 boron removal resin and pack it into a chromatography column (inner diameter × height is 2.5 cm × 30 cm). At a temperature of 30°C, pass salt lake brine into the chromatography column at a flow rate of 0.5 BV / h until the resin is saturated.

[0044] Resin eluent and boron recovery: At 30°C, 30 mL of 10% hydrochloric acid eluent was introduced into the saturated adsorption column at a flow rate of 10 BV / h for eluent analysis. Subsequently, pure water was introduced as the driving force, and the total volume of the eluent collected was 100 mL.

[0045] Boric acid preparation: The eluent was concentrated in a rotary evaporator until the boron concentration in the system was 20 g / L (concentrated to 10%-15% of the original volume); after concentration, it was cooled to 10-15 °C for crystallization, and filtered to obtain crude boric acid product. The yield of crude boric acid was calculated to be 81.2%. The initial boron concentration of the eluent was about 2-3 g / L, and the pH was between 1 and 2.

[0046] Lithium extraction: The pH of the boron-removed brine was adjusted to 5 with hydrochloric acid. The brine was then passed through a chromatography column packed with aluminum-based lithium adsorbent (provided by the company) at a flow rate of 0.5 BV / h at 30°C for adsorption, desorption, and purification. The final product was Li2CO3 with a purity of 99.4% and a lithium recovery rate of 90.9%. The consumption of brine acidification was reduced by 65.5% compared to the traditional direct acidification process.

[0047] Resin regeneration: The boron removal resin after analysis has regained its adsorption activity and can be recycled for boron removal treatment.

[0048] Example 3 Pre-boron removal treatment: Take 50 mL Seplite® LSC-800 boron removal resin and pack it into a chromatography column (inner diameter × height is 2.5 cm × 30 cm). At a temperature of 20°C, pass salt lake brine into the chromatography column at a flow rate of 10 BV / h until the resin is saturated.

[0049] Resin eluent and boron recovery: At 20°C, 10 mL of 31% hydrochloric acid eluent was introduced into the saturated adsorption column at a flow rate of 0.5 BV / h for eluent analysis. Subsequently, pure water was introduced as the driving force, and the total volume of the eluent collected was 100 mL.

[0050] Boric acid preparation: The eluent was concentrated in a rotary evaporator until the boron concentration in the system was 20 g / L (concentrated to 10%-15% of the original volume); after concentration, it was cooled to 10-15 °C for crystallization, and filtered to obtain crude boric acid product. The yield of crude boric acid was calculated to be 80.3%. The initial boron concentration of the eluent was about 2-3 g / L, and the pH was between 1 and 2.

[0051] Lithium extraction: The pH of the boron-removed brine was adjusted to 5 with hydrochloric acid. The brine was then passed through a chromatography column packed with aluminum-based lithium adsorbent (provided by the company) at a flow rate of 5 BV / h at 30°C for adsorption, desorption, and purification. The final product was Li2CO3 with a purity of 99.2% and a lithium recovery rate of 90.5%. The consumption of brine acidification was reduced by 64.9% compared with the traditional direct acidification process.

[0052] Resin regeneration: The boron removal resin after analysis has regained its adsorption activity and can be recycled for boron removal treatment.

[0053] Example 4 This embodiment proposes a boron-lithium co-production system for high-boron salt lake water. The specific components of the treated salt lake water are as follows:

[0054] The system employs a continuous ion exchange system, with each of the 16 resin columns packed with 35 mL of boron-removing resin. Figure 1 As shown, the areas are divided by function: The adsorption zone comprises six resin columns (1, 2, 3, 4, 5, and 6 in the diagram), with two parallel feed columns and three in series. These columns are used to adsorb high-boron salt lake water using boron adsorption resin, yielding adsorbed boron-adsorbed resin and boron-removed salt lake water. The salt lake water enters the adsorption zone via a raw solution tank and a raw solution buffer tank. The boron-removed salt lake water then enters a qualified solution tank.

[0055] The washing area includes three resin columns, 7, 8, and 9 in the diagram, which are used to wash the adsorbed boron-adsorbing resin with water. The desorption zone, including three resin columns (10, 11, and 12 in the figure), is used to desorb the adsorbed boron resin with an acid solution to obtain a boron desorption solution. The acid washing zone includes two resin columns, 13 and 14 in the figure, which are used to clean the boron adsorption resin after the desorption zone is desorbed. The tail liquid transformation zone includes a qualified liquid top water column (Figure 15) and an exhaust column (Figure 16), which are used to use the boron-removed salt lake water to perform top water and exhaust treatment on the boron adsorption resin after the acid washing zone is cleaned, so as to transform and regenerate the boron adsorption resin. The system sequentially switches between the adsorption zone, washing zone, desorption zone, water washing acid zone, and tail liquid transformation zone for each boron adsorption resin column according to the numbering sequence 1 to 16 in the figure, thereby achieving continuous ion-exchange treatment.

[0056] The system also includes a lithium extraction device, which adjusts the pH of the boron-removed salt lake water to 3-6.5, and uses an aluminum-based lithium adsorbent for adsorption treatment to extract lithium from the boron-removed salt lake water.

[0057] A boric acid extraction device is used to concentrate and crystallize boron desorption solution to obtain boric acid.

[0058] The specific processing procedure is as follows: Resin columns are switched sequentially according to their numbers 1-16 in the diagram, with a column switching time of 20 minutes. The experimental environment temperature is controlled at 25℃. The desorption zone uses an eluent prepared from a mixture of 6% hydrochloric acid and pure water. The process includes the following steps: Pre-boron removal treatment: First, at positions 1 to 6 of the adsorption zone of each resin column, brine from the salt lake is fed into the adsorption zone at a rate of 64 mL in a "top-in, bottom-out" manner. The process is continuous, and the boron content of the adsorption tail liquid is measured to be 18.68~22.54 mg / L, with the boron adsorption rate remaining stable at 99%.

[0059] In the washing area, the resin column is top-washed at position 7, and the water is discharged into the raw material buffer tank. Then it is washed at positions 8 and 9, and the water is discharged outside.

[0060] In the desorption zone, the resin column is topped with water at position 10, and the effluent is discharged. Then, desorption solution is introduced at positions 11 and 12, and the effluent is sent to the desorption solution tank. Specifically, 14.5 mL of a mixture of 6% hydrochloric acid and 42 mL of pure water is introduced for desorption. 41.5 mL of the desorption solution is collected, and the boron content of the eluent is analyzed to be 3848~4021 mg / L, with a resolution ≥99%. In the acid washing zone, the resin column is washed at positions 13 and 14. The acid solution that is pushed out of the acid washing zone is collected and reused in the preparation of the desorption solution to reduce acid consumption.

[0061] In the tail liquid transition zone, the resin column is sequentially treated with boron-removed brine lake water at positions 15 and 16 to perform top water and air removal on the boron adsorption resin after it has been washed in the acid washing zone. After regeneration, it is switched back to position 1 to complete the cycle.

[0062] The boric acid extraction device concentrates the desorbed liquid, cools and crystallizes it, filters and dries it to obtain crude boric acid product, with a yield of 85.3%.

[0063] The lithium extraction unit acidifies the boron-removed brine to pH 4.5 and then passes it into the lithium extraction unit for lithium extraction. The final Li2CO3 product has a purity of 99.7% and a lithium recovery rate of 92.5%. Statistics show that the amount of hydrochloric acid consumed per liter of brine for acidification in this stage is 26.9 ml (31%), which is 72.7% lower than the traditional direct acidification process, and the overall lithium extraction cost is reduced by 35%.

[0064] Comparative Example 1 This example uses brine from a high-boron salt lake in Tibet as raw material. The specific components were analyzed as follows:

[0065] The brine was acidified using 31% hydrochloric acid, with 98.8 ml of 31% hydrochloric acid consumed per liter of brine. Lithium was then extracted directly using an aluminum-based adsorbent, resulting in a Li2CO3 product with a purity of 99.7% and a lithium recovery rate of 91%.

[0066] Obviously, the above embodiments are merely illustrative examples for clear explanation and are not intended to limit the implementation. Those skilled in the art will recognize that other variations or modifications can be made based on the above description. It is neither necessary nor possible to exhaustively list all possible implementations here. However, obvious variations or modifications derived therefrom are still within the scope of protection of this invention.

Claims

1. A method for co-producing boron and lithium from high-boron salt lake water, characterized in that, Includes the following steps: Step 1: Boron adsorption resin is used to adsorb high-boron salt lake water to obtain boron adsorption resin and boron-removed salt lake water; Step 2: Desorb the adsorbed boron resin using an acid solution to obtain a boron desorption solution; Step 3: Adjust the pH of the boron-removed salt lake water to 3-6.5, and use an aluminum-based lithium adsorbent for adsorption treatment to extract lithium from the boron-removed salt lake water.

2. The method for co-producing boron and lithium from high-boron salt lake water according to claim 1, characterized in that, The high-boron salt lake water has a pH value of 8-10 and a boron content greater than 100 mg / L.

3. The method for co-producing boron and lithium from high-boron salt lake water according to claim 1, characterized in that, The boron adsorption resin used in step one is Seplite® LSC-800 resin.

4. The method for co-producing boron and lithium from high-boron salt lake water according to claim 1, characterized in that, In step one, the adsorption treatment includes loading boron adsorption resin into a column and then adding high-boron salt lake water for column adsorption. The adsorption treatment temperature is 0-50℃, and the flow rate of the high-boron salt lake water is 0.5~50 BV / h.

5. The method for co-producing boron and lithium from high-boron salt lake water according to claim 1, characterized in that, In step two, the acid solution is a hydrochloric acid solution with a mass concentration of 1%-31%; in the desorption process, the flow rate of the acid solution is 0.1~20 BV / h, the temperature is 5-50℃, and the amount of acid solution used is 0.1~10 BV.

6. The method for co-producing boron and lithium from high-boron salt lake water according to claim 1, characterized in that, In step two, the desorbed boron adsorption resin is returned to step one for reuse.

7. The method for co-producing boron and lithium from high-boron salt lake water according to claim 1, characterized in that, In step two, the boron desorption solution is concentrated and crystallized to obtain boric acid.

8. The method for co-producing boron and lithium from high-boron salt lake water according to claim 1, characterized in that, In step three, the adsorption treatment includes loading an aluminum-based lithium adsorbent into a column and then adding it to the boron-removed salt lake water for column adsorption. The adsorption treatment temperature is 0-50℃, and the flow rate of the boron-removed salt lake water is 0.5~10 BV / h.

9. A high-boron salt lake water boron-lithium co-production system, characterized in that, include: Boron adsorption resin column; The adsorption zone is used to adsorb high-boron salt lake water with boron adsorption resin to obtain adsorbed boron adsorption resin and boron-removed salt lake water. The desorption zone is used to desorb the adsorbed boron adsorption resin with an acid solution to obtain a boron desorption solution. The lithium extraction device is used to adjust the pH of the boron-removed salt lake water to 3-6.5, and then use an aluminum-based lithium adsorbent for adsorption treatment to extract lithium from the boron-removed salt lake water.

10. The high-boron salt lake water boron-lithium co-production system according to claim 9, characterized in that, The system also includes: The washing area is used to clean the boron adsorption resin after adsorption. The acid washing zone is used to clean the boron adsorption resin after desorption treatment in the desorption zone. The tail liquid transformation zone is used to treat the boron adsorption resin after it has been washed in the acid washing zone with boron-removed salt lake water for top water treatment and degassing, so that the boron adsorption resin can be transformed and regenerated. The system sequentially switches the boron adsorption resin column in the order of adsorption zone, washing zone, desorption zone, acid washing zone, and tail liquid conversion zone. Preferably, the system further includes a boric acid extraction device for concentrating and crystallizing the boron desorption solution to obtain boric acid.

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