Method of novel high-sulfate-radical brine aluminum-series lithium extraction adsorbent desorption process

Abstract

The invention belongs to the technical field of adsorption-method lithium extraction, and relates to a novel high-sulfate-radical brine aluminum-series lithium extraction adsorbent desorption process method, which is characterized in that continuous ion exchange equipment is adopted, the continuous ion exchange equipment is adopted, and the continuous ion exchange equipment is adopted to carry out continuous ion exchange on the high-sulfate-radical brine aluminum-series lithium extraction adsorbent desorption process, so that the high-sulfate-radical brine aluminum-series lithium extraction adsorbent desorption process is realized. The continuous ion exchange equipment comprises an adsorption area, a leaching area and an analysis area; the method comprises the following steps: carrying out lithium extraction adsorption on brine in an adsorption area through an adsorption unit of continuous ion exchange equipment; after adsorption, entering a leaching area to complete impurity leaching; desorbing lithium on the adsorbent in the desorption area by using a desorption agent; the desorption area is provided with a plurality of ion exchange columns which enter from the bottom and exit from the top, and comprises a pure water desorption area and a qualified liquid circulation desorption area. The method disclosed by the invention has the advantages that the lithium extraction adsorption and desorption efficiency is relatively high, and sulfate radical poisoning is avoided.

Description

Technical Field

[0001] This invention relates to a novel desorption process for high-sulfate brine aluminum-based lithium extraction adsorbents, belonging to the field of adsorption-based lithium extraction technology. Background Technology

[0002] Lithium is the lightest and lowest density metal in nature, often referred to as "white oil." It has wide applications in batteries, ceramics, pharmaceuticals, construction, and nuclear energy. In particular, with the rapid development of the global new energy industry, the demand for lithium resources in batteries and energy storage has increased significantly. How to obtain higher quality and cheaper lithium resources has become a hot research direction. Lithium resources account for up to 80% of salt lake brines, and more and more researchers are dedicated to studying the extraction of lithium resources from brines.

[0003] Currently, the main methods for lithium extraction from brine include adsorption, high-temperature calcination, and extraction. Among these, adsorption is considered the mainstream method due to its advantages such as good separation effect, environmental friendliness, low cost, and ease of operation. The core of adsorption is the performance of the adsorbent. In addition to considering adsorption capacity and selectivity, the desorption method is also crucial. In some brines with high sulfate levels, aluminum-based lithium extraction adsorbents cannot desorb lithium sulfate from the adsorption sites using normal desorption processes. Instead, the adsorbent directly enters the next adsorption cycle, leading to an accumulation of sulfate ions on the adsorbent and a significant decrease in adsorbent performance, resulting in adsorbent poisoning.

[0004] If the adsorbent cannot completely desorb the adsorbed substances through the desorption process after adsorption is completed and directly enters the next adsorption cycle, the performance of the adsorbent will gradually weaken, and the undesorbed substances will occupy more and more adsorption sites, leading to adsorbent poisoning.

[0005] Chinese patent CN115814465A discloses a method for preventing sulfate poisoning of adsorbents through regeneration using a high-concentration chloride salt solution. However, this method has the following drawbacks: First, the method uses a high concentration of chloride for regeneration, resulting in a large amount of chloride and increased costs. Second, the chloride regeneration process causes some lithium ions on the adsorbent to detach, resulting in lithium loss. Third, adding a regeneration step to the conventional ion-exchange process inevitably increases the process difficulty and affects process efficiency and stability. Therefore, there is an urgent need for a more efficient lithium extraction method that does not cause sulfate poisoning. Summary of the Invention

[0006] The technical problem to be solved by this invention is that when lithium extraction is carried out by adsorption using lithium extraction materials, if the sulfate content in the original brine is high, direct conventional adsorption and desorption will lead to poisoning of the aluminum-based adsorbent, which will affect the lithium extraction adsorption and desorption efficiency.

[0007] To address the shortcomings of existing technologies, this invention aims to provide a novel desorption process for high-sulfate brine aluminum-based lithium extraction adsorbents, which has the advantages of high lithium extraction adsorption and desorption efficiency and no sulfate poisoning.

[0008] The technical solution provided by this invention is as follows:

[0009] A novel desorption process for lithium extraction from high-sulfate brine using an aluminum-based adsorbent is disclosed, employing a continuous ion exchange apparatus comprising an adsorption zone, a rinsing zone, and a desorption zone. The method includes the following steps: in the adsorption zone, the brine is passed through the adsorption unit of the continuous ion exchange apparatus for lithium adsorption; after adsorption, the brine enters the rinsing zone for impurity rinsing; in the desorption zone, a desorbent is used to desorb the lithium from the adsorbent. The desorption zone is equipped with multiple ion exchange columns, all with bottom-inlet and top-outlet configurations, including a pure water desorption zone and a qualified liquid circulation desorption zone. The pure water desorption zone has two columns connected in parallel, with a pure water tank at the inlet and a qualified liquid circulation tank at the outlet. The qualified liquid circulation desorption zone has four columns connected in parallel, with qualified liquid circulation tanks at both the inlet and outlet.

[0010] Furthermore, the adsorption zone adopts a six-parallel, three-series configuration, all with bottom inlet and top outlet. The inlet is the original brine tank, and the outlet is the tail brine tank, with a total brine inlet flow rate of 160~240mL / min.

[0011] Furthermore, the rinsing zone consists of five tubes connected in series, with the inlet at the top and the outlet at the bottom. The inlet is a qualified liquid circulation tank, and the outlet is a raw brine tank. The rinsing flow rate is 30~50mL / min.

[0012] Furthermore, the continuous ion exchange equipment also includes a top feed zone, with the top feed water entering from below and exiting from above. The inlet is a tail brine tank, and the outlet is a pure water tank. The top feed flow rate is 20~40mL / min.

[0013] Furthermore, the continuous ion exchange equipment is also equipped with a qualified liquid discharge zone. The qualified liquid circulation tank is circulated into the qualified liquid discharge tank by a peristaltic pump, and the discharge flow rate is 100~140mL / min.

[0014] Furthermore, the aluminum-based lithium extraction adsorbent includes various doped or modified molecular sieve lithium extraction adsorbents synthesized from lithium salts and aluminum salts as raw materials.

[0015] Furthermore, the brine is one or more of the following: raw brine from salt lakes, brine from oil and gas fields, and old brine from salt production.

[0016] Furthermore, the rinsing water is one or more of the following: circulating qualified liquid in the qualified liquid circulation tank, pure water, and tap water.

[0017] Furthermore, the top feed water is one or more of the following: adsorbed tail brine, pure water, and tap water.

[0018] Furthermore, the continuous ion exchange equipment includes 15-30 ion exchange columns arranged in a sequential rotating manner. Each ion exchange column has an upper outlet and a lower outlet, and both the inlet and outlet are connected to a central rotary valve.

[0019] Beneficial effects

[0020] After adsorption is complete, the desorption solution used in this invention is circulated to increase the flow rate of the desorbed water without increasing the total amount of desorbed water. This results in more thorough desorption of the lithium-extraction adsorbent each time. Compared to the normal desorption process, the desorption efficiency of the adsorbent for lithium sulfate will continuously decrease until it reaches about 30% of the initial desorption capacity and then plateaus. This desorption process can ensure that the lithium-extraction adsorbent will not suffer from sulfate poisoning, and the adsorption capacity will be stably maintained at more than 90% of the initial adsorption capacity. Attached Figure Description

[0021] Figure 1 These are process flow diagrams for embodiments 1-3 of the present invention.

[0022] Figure 2 This is the process flow diagram for Comparative Example 1.

[0023] Figure 3 This is the process flow diagram for Comparative Example 2.

[0024] Figure 4 This is a process flow diagram of Embodiment 4 of the present invention.

[0025] Figure 5 This is the process flow diagram for Comparative Example 3;

[0026] Figure 6 The changes in the adsorption capacity of the adsorbent after a period of experimentation using the methods of Example 2 and Comparative Example 1;

[0027] Figure 7 The changes in the adsorption capacity of the adsorbent after a period of experimentation using the methods of Example 4 and Comparative Example 3 are shown. Detailed Implementation

[0028] This invention relates to a novel desorption process for a high-sulfate brine aluminum-based lithium extraction adsorbent, belonging to the field of adsorption-based lithium extraction technology. After adsorption, the desorption solution is circulated, increasing the flow rate of the desorbed water without increasing the total amount of desorbed water. This ensures more thorough desorption of the lithium extraction adsorbent each time, preventing sulfate poisoning.

[0029] The scope of protection of this invention should not be considered limited to specific embodiments. Any improvements and substitutions made based on the same concept of this invention shall also be protected by this invention.

[0030] Example 1

[0031] A novel desorption process for lithium extraction from aluminum-based brine using high-sulfate brines is disclosed. This process comprises four steps: adsorption, rinsing, desorption, and top-feeding. These four steps are performed sequentially and cyclically, and include the following steps:

[0032] 1) Adsorption: The pH of the brine is adjusted to 5-6. The entire adsorption process is carried out in a continuous ion exchange device, which consists of 30 ion exchange columns arranged in sequence, numbered 1-30. Columns 1-18 are the adsorption zones. Columns 1-6 are the brine inlet, and columns 13-18 are the brine outlet. The outlet of column 1 and the inlet of column 12 form a series path, and the outlet of column 12 and the inlet of column 13 form a series path, i.e., 1-12-13 form a triple series path. Similarly, five series paths are formed: 2-11-14, 3-10-15, 4-9-16, 5-8-17, and 6-7-18, for a total of six series paths. The raw brine enters the adsorption unit at a certain flow rate to complete the lithium extraction adsorption process.

[0033] 2) Rinsing: The entire rinsing process is carried out in a continuous ion exchange device. Columns 26-30 are the rinsing zone. Column 26 is the rinsing water inlet, and column 30 is the rinsing water outlet. Columns 26-30 form a series path with the water flowing from top to bottom. The rinsing water enters the rinsing unit at a certain flow rate to complete the impurity washing process.

[0034] 3) Desorption: The entire desorption process takes place in a continuous ion exchange unit, a qualified liquid circulation tank, and a qualified liquid discharge tank. Ion exchange columns 20-25 are the desorption zone, where a desorbent is used to desorb lithium from the adsorbent. Ion exchange columns 20-21 are the pure water desorption zone; the lower inlet of columns 20 and 21 is the pure water desorption inlet, and the upper inlet is the pure water desorption outlet. The pure water desorption outlet flows into the qualified liquid circulation tank. Ion exchange columns 22-25 are the qualified liquid circulation desorption zone; both the inlet and outlet of columns 22-25 are in the qualified liquid circulation tank. The qualified liquid discharge zone uses pumps to transfer the qualified liquid from the circulation tanks to the qualified liquid discharge tank. The flow rates of the pumps in the pure water desorption zone, the qualified liquid discharge tank, and the qualified liquid circulation tank are maintained at a constant speed to complete the entire lithium desorption process.

[0035] 4) Top Feeding: The entire top feeding process takes place in the continuous ion exchange equipment. Column 19 is the top feeding zone. The lower inlet of ion exchange column 19 is the top feeding inlet, and the upper inlet is the top feeding outlet. Top feeding water enters the top feeding unit at a certain flow rate to complete the top feeding process. The top feeding inlet is the tail brine tank, and the outlet is the pure water tank. For a 30-column system, this is column 19; for a 20-column system, it is column 11.

[0036] Aluminum-based lithium extraction adsorbents are molecular sieve lithium extraction adsorbents synthesized from lithium and aluminum salts as basic raw materials, including various doped or modified ones. These adsorbents use lithium chloride and aluminum chloride as raw materials, controlling the molar ratio of lithium to aluminum to approximately 2. The reaction is carried out using a co-precipitation method, and the reaction endpoint is controlled at pH 7 using sodium hydroxide solution titration, yielding a lithium chloride and aluminum chloride complex, LiAl-LDHS, which is the aluminum-based lithium extraction adsorbent. The brine is a complex brine solution containing lithium ions with a high sulfate content (below 60 g / L), such as raw brine from salt lakes, oil and gas field brine, and old brine from salt production. The leaching water is an inorganic solution with low conductivity (below 20 mS / cm), such as circulating qualified liquid in a qualified liquid circulation tank, pure water, or tap water. The desorbent is an inorganic solution with low conductivity (below 20 mS / cm), such as circulating qualified liquid in a qualified liquid circulation tank, pure water, or tap water. The feed water is an inorganic solution, such as adsorbed tail brine, pure water, or tap water. The ion exchange equipment consists of 15-30 ion exchange columns arranged in a sequential rotating manner. Each ion exchange column has an upper outlet and a lower outlet, both of which are connected to a central rotary valve. Different corresponding ports can be connected to form a passage according to process requirements. Valves or pumps control the on / off state and flow rate between the ion exchange columns and the pipelines.

[0037] Example 2

[0038] The brine used in this experiment was raw brine from a salt lake. A conventional aluminum-based adsorbent was used. The concentrations of the main ions in the brine, namely lithium, sodium, potassium, calcium, magnesium, boron, and sulfate, were 0.65 g / L, 25 g / L, 0.5 g / L, 200 g / L, 2.5 g / L, 0.4 g / L, and 12 g / L, respectively. The pH of the salt lake brine was 8.2, and the pH was adjusted to 5.5 using hydrochloric acid. The continuous ion exchange equipment uses 30 columns, each containing 400ml of adsorbent. The rotation interval is 10 minutes. Columns 1-18 are the adsorption zones, using a six-parallel, three-series configuration, all with bottom-in, top-outflow. The inlet is the raw brine tank, and the outlet is the tail brine tank, with a total brine inflow rate of 200mL / min. Column 19 is the top feed zone, with top feed water entering from the bottom and exiting from the top. The inlet is the tail brine tank, and the outlet is the pure water tank, with a top feed flow rate of 30mL / min. Columns 20-21 are the pure water desorption zones, two in parallel, both with top-in, bottom-outflow. The inlet is the pure water tank, and the outlet is the qualified liquid circulation tank. The total pure water desorption flow rate is 160 mL / min; zones 22-25 are the qualified liquid circulation desorption zones, four in parallel, all with bottom inlet and top outlet, and both inlet and outlet are qualified liquid circulation tanks, with a total circulation flow rate of 600 mL / min; zones 26-30 are the rinsing zones, five in series, with top inlet and bottom outlet, the inlet is the qualified liquid circulation tank, and the outlet is the original brine tank, with a rinsing flow rate of 40 mL / min; a separate qualified liquid discharge zone is set up, controlled by a peristaltic pump, which circulates the qualified liquid from the circulation tank to the qualified liquid discharge tank, with a discharge flow rate of 120 mL / min.

[0039] Example 3

[0040] The brine used in this experiment was raw brine from a salt lake. A conventional aluminum-based adsorbent was used. The concentrations of the main ions in the brine, namely lithium, sodium, potassium, calcium, magnesium, boron, and sulfate, were 0.4 g / L, 30 g / L, 10 g / L, 0.7 g / L, 10 g / L, 1.2 g / L, and 30 g / L, respectively. The pH of the salt lake brine was 8.2, and the pH was adjusted to 5 using hydrochloric acid. The continuous ion exchange equipment uses 30 columns, each containing 400ml of adsorbent. The rotation interval is 10 minutes. Columns 1-18 are the adsorption zones, using a six-parallel, three-series configuration, all with bottom-in, top-out flow. The inlet is the raw brine tank, and the outlet is the tail brine tank, with a total brine inflow rate of 250ml / min. Column 19 is the top feed zone, with top feed water entering from the bottom and exiting from the top. The inlet is the tail brine tank, and the outlet is the pure water tank, with a top feed flow rate of 30ml / min. Columns 20-21 are the pure water desorption zones, two in parallel, both with top-in, bottom-out flow. The inlet is the pure water tank, and the outlet is the qualified liquid circulation zone. The total pure water desorption flow rate is 160 ml / min; tanks 22-25 are the circulating desorption zone, four in parallel, all with bottom inlet and top outlet, and both inlet and outlet are qualified liquid circulation tanks, with a total circulation flow rate of 600 ml / min; tanks 26-30 are the rinsing zone, five in series, with top inlet and bottom outlet, the inlet is the qualified liquid circulation tank, and the outlet is the original brine tank, with a rinsing flow rate of 40 ml / min; a separate qualified liquid discharge zone is set up, controlled by a peristaltic pump, which circulates the qualified liquid from the circulation tank to the qualified liquid discharge tank, with a discharge flow rate of 120 ml / min.

[0041] Example 4

[0042] The brine used in this experiment was brine from a salt lake as raw material, and a conventional aluminum-based adsorbent was used. The concentrations of the main ions in the brine, namely lithium ions, sodium ions, potassium ions, calcium ions, magnesium ions, boron ions, and sulfate ions, were 0.45 g / L, 90 g / L, 10 g / L, 0.2 g / L, 15 g / L, 0.7 g / L, and 40 g / L, respectively, and the pH of the salt lake brine was 5.2. The continuous ion exchange equipment uses 20 columns, each containing 400ml of adsorbent. The rotation interval is 10 minutes. Columns 1-10 are the adsorption zone, using a five-column, two-column configuration, all with bottom-inlet and top-outlet flow. The inlet is the raw brine tank, and the outlet is the tail brine tank, with a total brine inlet flow rate of 220ml / min. Column 11 is the top feed zone, with top feed water entering from the bottom and exiting from the top. The inlet is the tail brine tank, and the outlet is the pure water tank, with a top feed flow rate of 30ml / min. Columns 12-13 are the pure water desorption zone, two in parallel, both with top-inlet and bottom-outlet flow. The inlet is the pure water tank, and the outlet is the qualified liquid circulation zone. The total pure water desorption flow rate is 160 ml / min; tanks 14-16 are the circulating desorption zone, three in parallel, all with bottom inlet and top outlet, and both inlet and outlet are qualified liquid circulation tanks, with a total circulation flow rate of 500 ml / min; tanks 17-20 are the rinsing zone, four in series, with top inlet and bottom outlet, the inlet is the qualified liquid circulation tank, and the outlet is the original brine tank, with a rinsing flow rate of 40 ml / min; a separate qualified liquid discharge zone is set up, controlled by a peristaltic pump, which circulates the qualified liquid from the circulation tank to the qualified liquid discharge tank, with a discharge flow rate of 120 ml / min.

[0043] Comparative Example 1

[0044] The difference from Example 2 is that the desorption process is different. Zones 20-25 are still desorption zones, using a two-parallel, three-series configuration with top inlet and bottom outlet. The inlet is a pure water tank, and the outlet is a qualified liquid tank. The inlet of the rinsing zone is a qualified liquid tank, and the outlet is a raw brine tank.

[0045] Comparative Example 2

[0046] The difference from Example 3 is as follows: A regeneration process is used. Zones 1-16 are adsorption zones, employing a four-in-four-out configuration, all with bottom-inlet and top-outlet flow. The inlet is the original brine tank, and the outlet is the tail brine tank, with a total inlet flow rate of 250 ml / min. Zone 17 is the top feed zone, with top feed water entering from the bottom and exiting from the top. The inlet is the tail brine tank, and the outlet is the pure water tank, with a top feed flow rate of 30 ml / min. Zones 18-23 are desorption zones, employing a two-in-three-out configuration, with top-inlet and bottom-outlet flow. The inlet is the pure water tank, and the outlet... The inlet is the qualified liquid tank, and the total pure water desorption flow rate is 160 ml / min; Nos. 24-27 are the rinsing zone, with four in series, top inlet and bottom outlet, the inlet is the qualified liquid tank, and the outlet is the regenerated liquid tank, with a rinsing flow rate of 40 ml / min; Nos. 28-30 are the regeneration zone, with three in series, top inlet and bottom outlet, the inlet is the regenerated liquid tank, and the outlet is the original brine tank, the regenerated liquid is a sodium chloride solution with a sodium ion concentration of 90 g / L, and the regeneration flow rate is 40 ml / min.

[0047] Comparative Example 3

[0048] The difference from Example 4 is that the desorption process is different. Zones 12-16 are still desorption zones, with 12-14-16 connected in series and 13-15 connected in series, with top inlet and bottom outlet. The inlet is a pure water tank and the outlet is a qualified liquid tank. The inlet of the rinsing zone is a qualified liquid tank and the outlet is a raw brine tank.

[0049] After a period of experimentation using the methods of Example 2 and Comparative Example 1, the adsorption capacity of the adsorbent changed as follows: Figure 6 As shown.

[0050] from Figure 6 As can be seen, after 38 cycles of the experiment, the adsorption capacity of Example 2 can be maintained at around 3 g / L. In contrast, the normal desorption process of Comparative Example 1 suffers from sulfate poisoning of the adsorbent, and the adsorption capacity continues to decrease after ten cycles, eventually dropping to 1.2 g / L. This indicates that the new desorption process can effectively solve the problem of sulfate poisoning of the adsorbent.

[0051] The methods described in Example 3 and Comparative Example 2 were compared.

[0052]

[0053] As can be seen from the table above, after twenty cycles of comparative experiments, both methods can operate stably. The adsorption capacity and desorption capacity of the example can be stabilized at 2.3 g / L and 2.1 g / L, respectively, which are slightly larger than those of Comparative Example 2 (2.1 g / L and 1.8 g / L). Example 3 uses a regeneration process, and the amount of sodium chloride required for regeneration is about 550 g / h, which is relatively expensive for industrial applications. Since the qualified liquid tank in Example 3 increases the amount of desorbed water through circulation desorption without increasing the total amount of desorbed water, and the qualified liquid is discharged through a qualified liquid discharge pipeline, the pure water consumption is the same as that of Comparative Example 2.

[0054] After a period of experimentation using the methods of Example 4 and Comparative Example 3, the adsorption capacity of the adsorbent changed as follows: Figure 7 As shown.

[0055] from Figure 7 It can be seen that after 20 cycles of the experiment, the adsorption capacity of Example 4 can be maintained at about 2.5 g / L. In contrast, the normal desorption process of Comparative Example 3 suffers from sulfate poisoning of the adsorbent, and the adsorption capacity continues to decrease after 8 cycles until it drops to 0.8 g / L. This shows that the new desorption process can effectively solve the problem of sulfate poisoning of the adsorbent.

Claims

1. A method for desorption of a novel aluminum-based lithium extraction adsorbent from high-sulfate brine, characterized in that, The method employs a continuous ion exchange apparatus, which includes an adsorption zone, a rinsing zone, and a desorption zone. The method comprises the following steps: in the adsorption zone, brine is passed through the adsorption unit of the continuous ion exchange apparatus for lithium adsorption; after adsorption, it enters the rinsing zone for impurity rinsing; in the desorption zone, a desorbent is used to desorb the lithium from the adsorbent. The desorption zone is equipped with multiple ion exchange columns, all with bottom-inlet and top-outlet configurations, including a pure water desorption zone and a qualified liquid circulation desorption zone. The pure water desorption zone has two parallel configurations, with a pure water tank at the inlet and a qualified liquid circulation tank at the outlet. The qualified liquid circulation desorption zone has four parallel configurations, with qualified liquid circulation tanks at both the inlet and outlet.

2. The method for desorption of the novel high-sulfate brine aluminum-based lithium extraction adsorbent according to claim 1, characterized in that, The adsorption zone adopts a six-parallel, three-series configuration, all with bottom inlet and top outlet. The inlet is the original brine tank, and the outlet is the tail brine tank. The total brine inlet flow rate is 160~240mL / min.

3. The method for desorption of the novel high-sulfate brine aluminum-based lithium extraction adsorbent according to claim 1, characterized in that, The rinsing zone has five tubes connected in series, with the inlet at the top and the outlet at the bottom. The inlet is a qualified liquid circulation tank, and the outlet is a raw brine tank. The rinsing flow rate is 30~50mL / min.

4. The method for desorption of the novel high-sulfate brine aluminum-based lithium extraction adsorbent according to claim 1, characterized in that, The continuous ion exchange equipment also includes a top feed zone, with the top feed entering from below and exiting from above. The inlet is a tail brine tank, and the outlet is a pure water tank. The top feed flow rate is 20~40mL / min.

5. The method for desorption of the novel high-sulfate brine aluminum-based lithium extraction adsorbent according to claim 1, characterized in that, The continuous ion exchange equipment is also equipped with a qualified liquid discharge zone. The qualified liquid circulation tank is circulated into the qualified liquid discharge tank by a peristaltic pump, and the discharge flow rate is 100~140mL / min.

6. The method for desorption of the novel high-sulfate brine aluminum-based lithium extraction adsorbent according to claim 1, characterized in that, The aluminum-based lithium extraction adsorbent comprises various doped or modified molecular sieve lithium extraction adsorbents synthesized from lithium salts and aluminum salts as raw materials.

7. The method for desorption of the novel high-sulfate brine aluminum-based lithium extraction adsorbent according to claim 1, characterized in that, The brine is one or more of the following: original brine from salt lakes, brine from oil and gas fields, and old brine from salt production.

8. The method for desorption of the novel high-sulfate brine aluminum-based lithium extraction adsorbent according to claim 1, characterized in that, The rinsing water is one or more of the following: circulating qualified liquid in the qualified liquid circulation tank, pure water, and tap water.

9. The method for desorption of the novel high-sulfate brine aluminum-based lithium extraction adsorbent according to claim 4, characterized in that, The top feed water is one or more of the following: adsorbed tail brine, pure water, and tap water.

10. The method for desorption of the novel high-sulfate brine aluminum-based lithium extraction adsorbent according to claim 1, characterized in that, The continuous ion exchange equipment includes 15-30 ion exchange columns arranged in a rotating manner. Each ion exchange column has an upper outlet and a lower outlet, and both the inlet and outlet are connected to a central rotary valve.

Images