Process for continuous moving adsorption of lithium from lithium-containing brine

Abstract

The application provides a continuous moving adsorption lithium extraction process and system. The continuous moving adsorption lithium extraction process provided by the application introduces first compressed air to perform bed loosening treatment on the ion exchange column in full column state, uses the first compressed air to disturb the adsorption bed in the ion exchange column in full column state, keeps the adsorption bed loose, improves the mass transfer efficiency of the lithium-containing brine, introduces second compressed air as the liquid discharge medium of the saturated state exchange column, reduces the lithium loss caused by the traditional water washing, avoids the decrease of the enrichment degree of potassium ions in the tail brine caused by the water washing, shortens the potassium ion concentration time, and improves the production efficiency of the potassium fertilizer, introduces industrial water as the lithium washing medium to save water resources and improve the lithium recovery rate, and introduces third compressed air as the liquid discharge medium of the ion exchange column to be recovered to save water resources, improve the enrichment degree and recovery rate of lithium ions in the elution liquid.

Description

Technical Field

[0001] This application relates to the field of lithium extraction technology from lithium-containing brine, and more specifically, to a continuous moving adsorption process for lithium extraction from lithium-containing brine. Background Technology

[0002] Lithium is a core raw material for the new energy industry, and brine extraction has become the mainstream route due to its large resource reserves and low cost. Traditional intermittent adsorption processes suffer from problems such as discontinuous operation, low efficiency, and significant lithium loss. While existing continuous moving bed processes can achieve continuous operation, they have drawbacks such as unreasonable series connection of adsorption zones and non-optimal switching of lithium washing media, which restrict their engineering applications.

[0003] In view of the above, this application is hereby submitted. Summary of the Invention

[0004] The main objective of this application is to provide a continuous moving bed lithium extraction process using lithium-containing brine, in order to solve the problems of unreasonable series connection of adsorption zones and non-optimal switching of lithium washing media in existing continuous moving bed processes, which restrict their engineering applications.

[0005] To achieve the above objectives, according to one aspect of this application, a continuous mobile lithium extraction process from lithium-containing brine is provided, comprising: step S1, passing lithium-containing brine into an empty ion exchange column for adsorption treatment, and passing a first compressed air into the column under full conditions for bed loosening treatment, to obtain a saturated ion exchange column and tail brine; wherein, the empty ion exchange column is provided with an adsorption bed; step S2, passing a second compressed air into the brine adsorption exchange column for drainage treatment, to obtain a deion exchange column to be washed and brine buffer; step S3, passing industrial water into the deion exchange column to be washed for lithium washing treatment, to obtain an ion exchange column to be desorbed and lithium washing solution; step S4, passing demineralized water into the ion exchange column to be desorbed for desorption treatment, to obtain a first desorbed solution and an ion exchange column to be recovered; wherein, the temperature of the demineralized water is 24~28℃; step S5, passing a third compressed air into the ion exchange column to be recovered for desorbed solution recovery treatment, to obtain an empty ion exchange column and a second desorbed solution, and mixing the second desorbed solution and the first desorbed solution to obtain a desorbed solution.

[0006] Furthermore, in step S1, the adsorption bed is filled with an aluminum-based adsorbent, and the single-column packing amount of the aluminum-based adsorbent is 5~6m. 3 Lithium-containing brine includes: Li + 0.04~0.30 g / L, Mg 2+ 48~85g / L, Ca 2+ 0.25~0.5g / L, Na + 6~45g / L, K + :7.5~13.5g / L, B: 0.1~0.2g / L, SO4 2-9.5~13g / L, Cl - : 171~270g / L.

[0007] Furthermore, the tailings are used to produce potash fertilizer.

[0008] Further, in step S1, the pressure of the first compressed air is 0.3~0.5MPa.

[0009] Furthermore, the flow rate of the first compressed air is 100~200m³. 3 / h.

[0010] Furthermore, the first compressed air intake method is bottom inlet and top outlet.

[0011] Further, in step S2, the pressure of the second compressed air is 0.3~0.5MPa, and the pressure inside the saturated ion exchange column is 0.2~0.4MPa during the drainage process. The brine buffer solution is returned to step S1 and mixed with the lithium-containing brine to continue the adsorption process.

[0012] Further, in step S3, the industrial water includes: Li + 0.003~0.02 mg / L, Mg 2+ 30~45mg / L, Ca 2+ 25~36mg / L, Na + 75~85mg / L, K + : 4~6mg / L, B: 0.2~0.45mg / L, SO4 2- 90~120mg / L, Cl - : 100~120mg / L.

[0013] Furthermore, the lithium washing solution is returned to step S1 and mixed with lithium-containing brine for continued adsorption treatment.

[0014] Further, in step S4, the demineralized water includes: Li + 0.7~1.0 mg / L, Mg 2+ 0.05~0.2 mg / L, Ca 2+ 0~0.1 mg / L, Na + 15~35mg / L, K + :0.1~0.5mg / L, B: 13~30mg / L, SO4 2- 0.1~0.5 mg / L, Cl - : 15~40mg / L.

[0015] Furthermore, in step S5, the pressure of the third compressed air is 0.3~0.5MPa.

[0016] Furthermore, in step S5, when performing the eluent recovery process, the pressure inside the ion exchange column to be recovered is 0.2~0.4 MPa.

[0017] Furthermore, in the eluent, Li + The concentration is 0.45~1.8g / L, and the magnesium-lithium ratio is ≤4:1, preferably ≤3:1.

[0018] Furthermore, in the eluent, the potassium-lithium ratio is ≤0.45:1, preferably ≤0.25:1.

[0019] Furthermore, in the eluent, the sodium-lithium ratio is ≤0.45:1, preferably ≤0.25:1.

[0020] Furthermore, the continuous moving lithium extraction process from lithium-containing brine is carried out in a continuous moving adsorption system. This system includes a support plate, an adsorption zone, a loose bed zone, a recovery zone, a desorption zone, a lithium washing zone, and a drainage zone. The adsorption zone includes a first adsorption zone and a second adsorption zone. The loose bed zone is located between the first and second adsorption zones. The first adsorption zone, loose bed zone, second adsorption zone, recovery zone, desorption zone, lithium washing zone, and drainage zone are arranged sequentially around the axis of the support plate. Multiple ion exchange columns are mounted on the support plate and are sequentially distributed around the axis of the support plate in the first adsorption zone, loose bed zone, second adsorption zone, recovery zone, desorption zone, lithium washing zone, and drainage zone. The axis of the support plate is rotatable around its own axis, allowing any one of the multiple ion exchange columns to enter the adsorption zone, loose bed zone, recovery zone, desorption zone, lithium washing zone, and drainage zone.

[0021] Furthermore, the first adsorption zone and the second adsorption zone are connected in series, and each of the first and second adsorption zones is equipped with 9 ion exchange columns. The liquid inlet of the first adsorption zone is top-in, bottom-out, and the liquid inlet of the second adsorption zone is bottom-in, top-out. The sparse bed zone is equipped with 1 ion exchange column, and the gas inlet of the sparse bed zone is bottom-in, top-out. The recovery zone is equipped with 1 ion exchange column, and the gas inlet of the recovery zone is top-in, bottom-out. The desorption zone includes a first desorption zone, a second desorption zone, and a third desorption zone connected in series, each equipped with 2 ion exchange columns, and the liquid inlet of the first desorption zone, the second desorption zone, and the third desorption zone are each independently top-in, bottom-out. The lithium washing zone is equipped with 3 ion exchange columns connected in series, and the liquid inlet of the lithium washing zone is top-in, bottom-out. The draining zone is equipped with 1 ion exchange column, and the gas inlet of the draining zone is top-in, bottom-out.

[0022] Applying the technical solution of this application, the continuous moving adsorption lithium extraction process for lithium-containing brine provided by this application introduces a first compressed air to loosen the adsorption bed of a full-capacity ion exchange column, thereby improving the mass transfer efficiency of the lithium-containing brine. By introducing a second compressed air as the draining medium for the saturated exchange column, lithium loss caused by traditional water washing is reduced, and the reduction in potassium ion enrichment in the tail brine caused by water washing is avoided, thus shortening the potassium ion concentration time and improving the production efficiency of potassium fertilizer. Introducing industrial water as the lithium washing medium saves water resources while increasing the lithium recovery rate. Introducing a third compressed air as the draining medium for the ion exchange column to be recovered saves water resources while increasing the lithium ion enrichment and recovery rate in the eluent. Attached Figure Description

[0023] The accompanying drawings, which form part of this application, are used to provide a further understanding of this application. The illustrative embodiments and descriptions of this application are used to explain this application and do not constitute an undue limitation of this application. In the drawings:

[0024] Figure 1 A schematic flow diagram of a continuous moving lithium extraction process from lithium-containing brine according to some embodiments of this application is shown. Detailed Implementation

[0025] It should be noted that, unless otherwise specified, the embodiments and features described in this application can be combined with each other. The present application will now be described in detail with reference to the embodiments.

[0026] As analyzed in the background section of this application, traditional intermittent adsorption lithium extraction processes suffer from problems such as discontinuous operation, low efficiency, and significant lithium loss. While existing continuous moving bed processes achieve continuous operation, they suffer from drawbacks such as an unreasonable series connection of adsorption zones and suboptimal switching of lithium washing media, hindering their engineering applications. To address these issues, this application provides a continuous moving bed adsorption lithium extraction process using lithium-containing brine.

[0027] In a first typical embodiment of this application, a continuous moving adsorption lithium extraction process for lithium-containing brine is provided, comprising the following steps: Step S1, lithium-containing brine is passed into an empty ion exchange column for adsorption treatment, and a first compressed air is introduced into the column under full condition for bed loosening treatment to obtain a saturated ion exchange column and tail brine, wherein an adsorption bed is provided in the empty ion exchange column; Step S2, a second compressed air is introduced into the saturated ion exchange column for liquid drainage treatment to obtain a deion exchange column to be washed and brine buffer solution; Step S3, industrial water is introduced into the deion exchange column to be washed for lithium washing treatment to obtain a lithium washing column to be desorbed and lithium washing solution; Step S4, demineralized water is introduced into the deion exchange column to be desorbed for desorption treatment to obtain a first desorbed solution and a ion exchange column to be recovered; wherein the temperature of the demineralized water is 22~30℃; Step S5, a third compressed air is introduced into the ion exchange column to be recovered for desorbed solution recovery treatment to obtain an empty ion exchange column and a second desorbed solution, and the second desorbed solution and the first desorbed solution are mixed to obtain a desorbed solution.

[0028] The lithium extraction process for lithium-containing brine using continuous moving adsorption provided in this application involves introducing a first compressed air to loosen the adsorption bed in a fully loaded ion exchange column, thereby improving the mass transfer efficiency of the lithium-containing brine. A second compressed air is introduced as the draining medium for the saturated ion exchange column, reducing lithium loss caused by traditional water washing and preventing a decrease in potassium ion enrichment in the tail brine, thus shortening the potassium ion concentration time and improving the production efficiency of potassium fertilizer. Industrial water is used as the lithium washing medium, saving water resources while increasing lithium recovery. Finally, a third compressed air is introduced as the draining medium for the ion exchange column to be recycled, saving water resources while increasing the enrichment and recovery rate of lithium ions in the eluent.

[0029] In step S4 above, using demineralized water at a temperature of 24~28℃ for the desorption process is more conducive to improving the lithium ion desorption efficiency and lithium ion recovery rate. If the temperature of the demineralized water is too low, the desorption efficiency is low and the lithium recovery rate is reduced; if the temperature of the demineralized water is too high, energy consumption increases. Specifically, the temperature of the demineralized water is 24℃, 25℃, 26℃, 27℃, 28℃, or any combination of two values.

[0030] In some embodiments of this application, in step S1 above, the adsorption bed of the ion exchange column is filled with an aluminum-based adsorbent, which is a commonly used adsorbent in the art, preferably with a capacity ≥2.5 g / L, to further improve the adsorption efficiency.

[0031] In some embodiments of this application, the single-column packing density of the aluminum-based adsorbent is 5-6 m³. 3To further improve the adsorption efficiency of lithium ions, the aluminum-based adsorbent is used to fill a single column with a density of 5m³. 3 5.2m 3 5.5m 3 5.8m 3 6m 3 Or a range of values ​​consisting of any two numerical values.

[0032] In some embodiments of this application, the lithium-containing brine includes, but is not limited to, salt lake brine, underground brine, etc. In some specific embodiments, the lithium-containing brine includes: Li + 0.04~0.30 g / L, Mg 2+ 48~85g / L, Ca 2+ 0.25~0.5g / L, Na + 6~45g / L, K + :7.5~13.5g / L, B: 0.1~0.2g / L, SO4 2- 9.5~13g / L, Cl - : 171~270 g / L. Specifically, in lithium-containing brines, Li + The concentration is 0.04 g / L, 0.05 g / L, 0.06 g / L, 0.08 g / L, 0.10 g / L, 0.15 g / L, 0.20 g / L, 0.25 g / L, 0.30 g / L, or any range of two values; Mg 2+ The concentration is 48 g / L, 50 g / L, 52 g / L, 55 g / L, 58 g / L, 60 g / L, 62 g / L, 65 g / L, or any range of two values; Ca 2+ The concentration is 0.3 g / L, 0.32 g / L, 0.35 g / L, 0.38 g / L, 0.4 g / L, 0.42 g / L, 0.45 g / L, 0.48 g / L, 0.5 g / L, or any range of two values; Na + The concentration is 6 g / L, 6.5 g / L, 8 g / L, 10 g / L, 12 g / L, 15 g / L, 18 g / L, 20 g / L, 25 g / L, 30 g / L, 35 g / L, 40 g / L, 45 g / L, or any range of two values; K + The concentration of [a] is 7.5 g / L, 8 g / L, 8.5 g / L, 9 g / L, 9.5 g / L, 10 g / L, 10.5 g / L, or any two of these values; the concentration of [b] is 0.1 g / L, 0.12 g / L, 0.15 g / L, 0.18 g / L, 0.2 g / L, or any two of these values; SO4 2-The concentration is 9.5 g / L, 10 g / L, 10.5 g / L, 11 g / L, 11.5 g / L, 12 g / L, 12.5 g / L, 13 g / L, or any range of two values; Cl - The concentration is 171 g / L, 175 g / L, 180 g / L, 185 g / L, 190 g / L, 195 g / L, 200 g / L, 210 g / L, 220 g / L, 230 g / L, 233 g / L, or any range of two values.

[0033] In some embodiments of this application, in step S1, the pressure of the first compressed air is 0.3~0.5 MPa, which is beneficial to fully agitate the adsorption bed in the ion exchange column under full column conditions, and to keep the adsorption bed loose, so as to further promote the full contact between the adsorption bed and the lithium-containing brine, improve the adsorption efficiency, and thus further improve the mass transfer efficiency of the lithium-containing brine. Specifically, the pressure of the first compressed air is 0.3 MPa, 0.35 MPa, 0.4 MPa, 0.45 MPa, 0.5 MPa, or any two of these values.

[0034] In some embodiments of this application, the flow rate of the first compressed air is 100~200m³. 3 / h, to further improve the efficiency of the sparse bed treatment. Specifically, the flow rate of the first compressed air is 100m³ / h. 3 / h, 120m 3 / h, 150m 3 / h, 180m 3 / h、200m 3 / h or a range of values ​​consisting of any two numbers.

[0035] In some embodiments of this application, the first compressed air is introduced into the ion exchange column when the column is full of lithium brine, which is more conducive to improving the efficiency of the sparse bed treatment and the mass transfer efficiency between the adsorption bed and the lithium brine.

[0036] In some embodiments of this application, the first compressed air is introduced from the bottom and exited from the top to further agitate the adsorption bed and further improve the mass transfer efficiency of the brine.

[0037] In some embodiments of this application, the tail brine is used to produce potash fertilizer. Because a second compressed air is used for drainage instead of water, dilution of the tail brine is avoided, which is more conducive to increasing the concentration of potassium ions in the tail brine. This, in turn, increases the supersaturation of carnallite during potash fertilizer production, further shortens the evaporation time, and improves the production efficiency of potash fertilizer.

[0038] In some embodiments of this application, in step S2, the brine in the saturated ion exchange column is discharged by introducing a second compressed air into the column to remove the brine, thus obtaining the ion exchange column to be washed and the brine buffer solution. This not only reduces the brine entrainment in the adsorbent bed, but also helps to reduce magnesium impurities in the lithium washing solution and the magnesium ion content in the eluent. In this way, the waste of water resources caused by the traditional method of using water for drainage is avoided, while also reducing lithium loss and improving the lithium recovery rate.

[0039] In some embodiments of this application, the pressure of the second compressed air is 0.3~0.5 MPa to further improve the efficiency of the drainage treatment. Specifically, the pressure of the second compressed air is 0.3 MPa, 0.35 MPa, 0.4 MPa, 0.45 MPa, 0.5 MPa, or any range of two values.

[0040] In some embodiments of this application, during the drainage process, the flow rate of the second compressed air is controlled to maintain the pressure inside the saturated ion exchange column at 0.2~0.4 MPa, thereby ensuring more thorough drainage and a higher enrichment of lithium in the eluent. Specifically, during the drainage process, the pressure inside the saturated ion exchange column is within a range of 0.2 MPa, 0.25 MPa, 0.3 MPa, 0.35 MPa, 0.4 MPa, or any two of these values.

[0041] In some embodiments of this application, the brine buffer solution is returned to step S1 and mixed with lithium-containing brine for further adsorption treatment to further improve the lithium recovery rate.

[0042] In some embodiments of this application, in step S3, calcium and magnesium ions adsorbed on the surface of the adsorbent bed are washed with industrial water to increase the enrichment of lithium in the eluent and reduce the magnesium-lithium ratio while saving water resources.

[0043] In some embodiments of this application, the industrial water is commonly used industrial water. In some specific embodiments, the industrial water includes: Li + 0.003~0.02 mg / L, Mg 2+ 30~45mg / L, Ca 2+ 25~36mg / L, Na + 75~85mg / L, K + : 4~6mg / L, B: 0.2~0.45mg / L, SO4 2- 90~120mg / L, Cl - : 100~120mg / L.

[0044] Specifically, in industrial water, Li +The concentration is 0.003 mg / L, 0.005 mg / L, 0.008 mg / L, 0.01 mg / L, 0.012 mg / L, 0.015 mg / L, 0.018 mg / L, 0.02 mg / L, or any range of two values; Mg 2+ The concentration is 30 mg / L, 32 mg / L, 35 mg / L, 38 mg / L, 40 mg / L, 42 mg / L, 45 mg / L, or any range of two values; Ca 2+ The concentration is 25 mg / L, 28 mg / L, 30 mg / L, 32 mg / L, 35 mg / L, 36 mg / L, or any range of two values; Na + The concentration is 7 mg / L, 78 mg / L, 80 mg / L, 82 mg / L, 85 mg / L, or any range of two values; K + The concentration of α is 4 mg / L, 4.5 mg / L, 5 mg / L, 5.5 mg / L, 6 mg / L, or any two of these values; the concentration of β is 0.2 mg / L, 0.25 mg / L, 0.3 mg / L, 0.35 mg / L, 0.4 mg / L, 0.45 mg / L, or any two of these values; SO4 2- The concentration is 90 mg / L, 95 mg / L, 100 mg / L, 105 mg / L, 110 mg / L, 115 mg / L, 120 mg / L, or any range of two values; Cl - The concentration is 100 mg / L, 105 mg / L, 110 mg / L, 115 mg / L, 120 mg / L, or any range of two values.

[0045] In some embodiments of this application, the lithium washing solution is returned to step S1 and mixed with lithium-containing brine before being passed into an ion exchange column for further adsorption treatment, so as to recover lithium ions from the lithium washing solution and further improve the lithium ion recovery rate.

[0046] In some embodiments of this application, step S4, which uses demineralized water to desorb the empty ion exchange column, is more conducive to improving the efficiency of lithium ion desorption and treatment and increasing the lithium ion recovery rate.

[0047] In some embodiments of this application, the demineralized water includes, but is not limited to, deionized water, pure water, or purified water, to avoid introducing impurities that could affect lithium ion desorption. In some specific embodiments, the demineralized water includes: Li + 0.7~1.0 mg / L, Mg 2 + 0.05~0.2 mg / L, Ca 2+ 0~0.1 mg / L, Na+ 15~35mg / L, K + :0.1~0.5mg / L, B: 13~30mg / L, SO4 2- 0.1~0.5 mg / L, Cl - : 15~40mg / L.

[0048] Specifically, in the desalinated water, Li + The concentration is 0.7 g / mL, 0.8 g / mL, 0.9 g / mL, 1.0 g / mL, or any range of two values; Mg 2+ The concentration is 0.05 g / mL, 0.08 g / mL, 0.1 g / mL, 0.12 g / mL, 0.15 g / mL, 0.18 g / mL, 0.2 g / mL, or any range of two values; Ca 2+ The concentration is 0, 0.01 g / mL, 0.02 g / mL, 0.05 g / mL, 0.08 g / mL, 0.1 g / mL, or any range of two values; K + The concentration of is 0.1 g / mL, 0.15 g / mL, 0.2 g / mL, 0.3 g / mL, 0.4 g / mL, 0.5 mg / L, or any range of two values; the concentration of B is 13 g / mL, 14 g / mL, 15 g / mL, 18 g / mL, 20 g / mL, 22 g / mL, 25 g / mL, 28 g / mL, 30 g / mL, or any range of two values; SO4 2- The concentration is 0.1 g / mL, 0.15 g / mL, 0.2 g / mL, 0.25 g / mL, 0.3 g / mL, 0.4 g / mL, 0.5 g / mL, or any range of two values; Cl - The concentration is 15 g / mL, 18 g / mL, 20 g / mL, 25 g / mL, 30 g / mL, 35 g / mL, 40 g / mL or any two values ​​within a range.

[0049] In some embodiments, in order to further improve the lithium recovery rate, in step S5, a third compressed air is introduced into the ion exchange column to be recovered for desorption liquid recovery treatment, so as to more completely desorb the lithium ions adsorbed in the adsorption bed, thereby further improving the lithium recovery rate.

[0050] In some specific embodiments, the pressure of the third compressed air is 0.3~0.5MPa to further improve the efficiency of the bed treatment. Specifically, the pressure of the second compressed air is 0.3MPa, 0.35MPa, 0.4MPa, 0.45MPa, 0.5MPa, or any combination of two values.

[0051] In some embodiments of this application, during the recovery of the eluent, the flow rate of the third compressed air is controlled to maintain the pressure inside the ion exchange column to be recovered at 0.2~0.4 MPa, thereby ensuring more thorough recovery of the eluent and improving the lithium recovery rate while avoiding dilution of the eluent by washing with water. Specifically, during the recovery of the eluent, the pressure inside the ion exchange column to be recovered is within a range of 0.2 MPa, 0.25 MPa, 0.3 MPa, 0.35 MPa, 0.4 MPa, or any two of these values.

[0052] In some embodiments of this application, the tail brine includes: K + 10~13.5g / L, Na + 10~14g / L, Li + 0~10mg / L, Mg 2+ The concentration of sodium and potassium ions in the tail brine is 68~80 g / L, which results in a high concentration of sodium and potassium ions while the lithium ion content is very low, leading to a higher lithium ion recovery rate.

[0053] Specifically, in the tail brine, K + The concentration is 10 g / L, 10.5 g / L, 11 g / L, 11.5 g / L, 12 g / L, 12.5 g / L, 13 g / L, 13.5 g / L, or any range of two values; Na + The concentration is 10 g / L, 10.5 g / L, 11 g / L, 12 g / L, 13 g / L, 14 g / L, or any range of two values; Li + The concentration is 0, 1 g / L, 2 g / L, 5 g / L, 8 g / L, 10 g / L, or any range of two values.

[0054] In some embodiments of this application, in the eluent, Li + The concentration of Li is 0.45~1.8 g / L, and the magnesium-to-lithium ratio is ≤4:1, preferably ≤3:1, for example, a magnesium-to-lithium ratio of 0.1~4:1, 0.1~3:1, or 0.1~1.5:1, to improve the lithium ion enrichment and adsorption rate in the eluent. Specifically, in the eluent, Li + The concentration is 0.45 g / L, 0.5 g / L, 0.6 g / L, 0.8 g / L, 1.0 g / L, 1.2 g / L, 1.5 g / L, 1.8 g / L or any two of these values; the magnesium-lithium ratio is 0.1:1, 0.2:1, 0.5:1, 0.8:1, 1.0:1, 1.1:1, 1.2:1, 1.3:1, 1.4:1, 1.5:1, 2:1, 2.5:1, 3:1, 3.5:1, 4:1 or any two of these values.

[0055] In some embodiments of this application, the potassium-to-lithium ratio in the eluent is 0.02 to 0.45:1, preferably 0.02 to 0.25:1, to further reduce the potassium content in the eluent and facilitate lithium recovery. Specifically, the potassium-to-lithium ratio in the eluent is 0.02:1, 0.05:1, 0.08:1, 0.1:1, 0.12:1, 0.15:1, 0.18:1, 0.2:1, 0.22:1, 0.25:1, 0.28:1, 0.3:1, 0.35:1, 0.4:1, 0.45:1, or any range of two values.

[0056] In some embodiments of this application, the sodium-to-lithium ratio in the eluent is 0.01 to 0.45:1, preferably 0.01 to 0.25:1, further reducing the potassium content in the eluent and facilitating lithium recovery. Specifically, the sodium-to-lithium ratio in the eluent is 0.01:1, 0.02:1, 0.05:1, 0.08:1, 0.1:1, 0.15:1, 0.2:1, 0.25:1, 0.3:1, 0.35:1, 0.4:1, 0.45:1, or any range of two values.

[0057] In some embodiments of this application, the above-described continuous moving adsorption lithium extraction process using lithium-containing brine is carried out in a continuous moving lithium extraction system, such as... Figure 1 As shown, the continuous mobile lithium extraction system includes a support plate, an adsorption zone, a recovery zone, a desorption zone, a lithium washing zone, and a drainage zone. The adsorption zone includes a first adsorption zone and a second adsorption zone, with a loose bed zone between the first and second adsorption zones. The first adsorption zone, loose bed zone, second adsorption zone, recovery zone, desorption zone, lithium washing zone, and drainage zone are arranged sequentially around the axis of the support plate. The support plate is equipped with multiple ion exchange columns, which are sequentially distributed around the axis of the support plate in the first adsorption zone, loose bed zone, second adsorption zone, recovery zone, desorption zone, lithium washing zone, and drainage zone. The axis of the support plate is rotatable around its own axis so that any one of the multiple ion exchange columns can enter the adsorption zone, loose bed zone, recovery zone, desorption zone, lithium washing zone, and drainage zone.

[0058] In some embodiments of this application, the first adsorption zone and the second adsorption zone are connected in series, and each of the first adsorption zone and the second adsorption zone is provided with 9 ion exchange columns. The liquid inlet method of the first adsorption zone is top inlet and bottom outlet, and the liquid inlet method of the second adsorption zone is bottom inlet and top outlet, so as to further improve the adsorption efficiency of the ion exchange column.

[0059] In some embodiments of this application, the sparse bed region is provided with one ion exchange column, and the air inlet of the sparse bed region is bottom inlet and top outlet, so as to further improve the disturbance of the adsorption bed in the ion exchange column by the first compressed air and improve the mass transfer efficiency of the adsorption bed to the lithium brine.

[0060] In some embodiments of this application, the recovery zone is provided with one ion exchange column, and the gas inlet of the recovery zone is top-inlet and bottom-outlet, so as to further improve the efficiency of the eluent recovery treatment and promote the complete removal of the eluent in the saturated ion exchange column.

[0061] In some embodiments of this application, the analysis zone includes a first analysis zone, a second analysis zone, and a third analysis zone arranged in series. Each of the first analysis zone, the second analysis zone, and the third analysis zone is provided with two ion exchange columns. The liquid inlet method of the first analysis zone, the second analysis zone, and the third analysis zone is top-in and bottom-out, so as to further improve the analysis efficiency and increase the enrichment of lithium ions in the analysis solution.

[0062] In some embodiments of this application, the lithium washing zone includes three ion exchange columns arranged in series to further reduce the energy consumption of industrial water and the content of impurity ions in the eluent. The lithium washing zone has a top-in, bottom-out liquid inlet configuration.

[0063] In some embodiments of this application, the drainage zone is provided with an ion exchange column, and the air inlet of the drainage zone is top-inlet and bottom-outlet to further improve the efficiency of drainage treatment and promote the complete discharge of brine in the brine adsorption ion exchange column, thereby further reducing the content of impurity ions in the cleaning solution.

[0064] In some embodiments of this application, the continuous mobile adsorption system further includes a brine tank, a compressed air storage tank, a tail brine tank, a hot water tank, a desorption water tank, and a wash water tank. The brine tank stores lithium-containing brine and is connected to the adsorption zone to allow the lithium-containing brine to be introduced into the adsorption zone for adsorption treatment. The compressed air storage tank stores compressed air and is connected to the bed thinning zone, the recovery zone, and the discharge zone, respectively, to allow the compressed air to be introduced into these zones for bed thinning, desorption liquid recovery, and discharge treatment, respectively. The tail brine tank is connected to the absorption zone to store the tail brine discharged from the adsorption zone. The wash water tank stores industrial water and is connected to the lithium washing zone to allow the industrial water to be introduced into the lithium washing zone for lithium washing treatment. The hot water tank stores demineralized water and is connected to the desorption zone to allow the demineralized water to be introduced into the desorption zone for desorption treatment. The desorption water tank stores the desorption liquid and is connected to both the recovery zone and the desorption zone to allow the first and second desorption liquids to be discharged into the desorption water tank for mixing.

[0065] In addition, the brine tank is connected to the drainage area so that the brine buffer solution discharged from the drainage area can be discharged into the brine tank and mixed with the lithium-containing brine before being passed through the ion exchange column for adsorption treatment.

[0066] The brine tank is also connected to the lithium washing zone so that the lithium washing solution discharged from the lithium washing zone can be discharged into the brine tank and mixed with the lithium-containing brine before being passed through the ion exchange column for adsorption treatment.

[0067] The beneficial effects of this application will be further illustrated below with reference to embodiments and comparative examples.

[0068] Example 1

[0069] This embodiment provides a continuous moving lithium extraction process using lithium-containing brine, the composition of which is shown in Table 1 below.

[0070] Table 1

[0071]

[0072] The continuous moving lithium extraction process using lithium-containing brine is carried out entirely within a continuous moving lithium extraction system, such as... Figure 1 As shown, the continuous mobile lithium extraction system includes a support plate, an adsorption zone, a recovery zone, a desorption zone, a lithium washing zone, and a drainage zone. The adsorption zone includes a first adsorption zone and a second adsorption zone, with a loose bed zone between the first and second adsorption zones. The first adsorption zone, loose bed zone, second adsorption zone, recovery zone, desorption zone, lithium washing zone, and drainage zone are arranged sequentially around the axis of the support plate. The support plate is equipped with multiple ion exchange columns, which are sequentially distributed around the axis of the support plate in the first adsorption zone, loose bed zone, second adsorption zone, recovery zone, desorption zone, lithium washing zone, and drainage zone. The axis of the support plate is rotatable around its own axis so that any one of the multiple ion exchange columns can enter the adsorption zone, loose bed zone, recovery zone, desorption zone, lithium washing zone, and drainage zone.

[0073] The first adsorption zone and the second adsorption zone are connected in series, and each of the first adsorption zone and the second adsorption zone is equipped with 9 parallel ion exchangers. The liquid inlet method of the first adsorption zone (columns 1 to 9) is top inlet and bottom outlet, and the liquid inlet method of the second adsorption zone (columns 11 to 19) is bottom inlet and top outlet.

[0074] The sparse bed zone is equipped with one ion exchange column (column No. 10), and the air intake method of the sparse bed zone is bottom inlet and top outlet.

[0075] The recovery zone is equipped with one ion exchange column (column No. 20), and the gas inlet of the recovery zone is top-inlet and bottom-outlet.

[0076] The analysis zone includes a first analysis zone, a second analysis zone, and a third analysis zone arranged in series. Each of the first analysis zone, the second analysis zone, and the third analysis zone has two parallel ion exchange columns. The liquid inlet method of the first analysis zone (columns 21-22), the second analysis zone (columns 23-24), and the third analysis zone (columns 25-26) is top inlet and bottom outlet.

[0077] The lithium washing zone consists of three ion exchange columns connected in series, with the liquid entering from the top and exiting from the bottom.

[0078] The drainage area is equipped with one ion exchange column, and the air inlet of the drainage area is top-inlet and bottom-outlet.

[0079] In addition, such as Figure 1 As shown, the continuous mobile adsorption system also includes a brine tank, a compressed air storage tank, a tail brine tank, a hot water tank, a desorption water tank, and a wash water tank. The brine tank is used to store lithium-containing brine and is connected to the adsorption zone to allow the lithium-containing brine to be introduced into the adsorption zone for adsorption treatment.

[0080] The compressed air storage tank is used to store compressed air, which is connected to the bed-clearing zone, the recovery zone, and the drainage zone, respectively, so that the compressed air can be introduced into the bed-clearing zone, the recovery zone, and the drainage zone for bed-clearing treatment, desorption liquid recovery treatment, and drainage treatment, respectively. The tail brine tank is connected to the absorption zone to store the tail brine discharged from the adsorption zone.

[0081] The wash water tank is used to store industrial water. The wash water tank is connected to the lithium washing area so that the industrial water can be introduced into the lithium washing area for lithium washing treatment.

[0082] The hot water tank is used to store demineralized water. The hot water tank is connected to the analysis zone so that the demineralized water can be introduced into the analysis zone for analysis processing.

[0083] The elution water tank is used to store the elution liquid. The elution water tank is connected to both the recovery area and the elution area to discharge the first and second elution liquids into the elution water tank for mixing.

[0084] The brine tank is also connected to the drainage area so that the brine buffer solution discharged from the drainage area can be discharged into the brine tank and mixed with the lithium-containing brine before being passed through the ion exchange column for adsorption treatment.

[0085] The brine tank is also connected to the lithium washing zone so that the lithium washing solution discharged from the lithium washing zone can be discharged into the brine tank and mixed with the lithium-containing brine before being passed through the ion exchange column for adsorption treatment.

[0086] The continuous moving lithium extraction process using lithium-containing brine includes the following steps:

[0087] (1) Adsorption treatment and bed loosening treatment: Lithium-containing brine is pumped into the adsorption zone for adsorption treatment. Each empty ion exchange column in the adsorption zone is equipped with an adsorption bed, which is filled with an aluminum-based adsorbent with an adsorption capacity of 2.5 g / L and a single column packing density of 5.5 m. 3 The lithium-containing brine is pumped into the adsorption zone for adsorption treatment, with a total influent flow rate of 115 m³ / h. 3 / / h, after adsorption treatment, a saturated ion exchange column and tail brine are obtained. The tail brine is discharged to a tail brine tank for storage. Furthermore, during the adsorption process, the ion exchange column in the adsorption zone is transferred to the loosening bed zone, where first compressed air is introduced for loosening treatment. The pressure of the first compressed air is 0.3 MPa, and the flow rate is 100 m³ / h. 3 / h.

[0088] (2) Drainage treatment: The above saturated ion exchange columns are sequentially transferred to the drainage zone. The second compressed air is introduced into the drainage zone for drainage treatment to obtain the ion exchange column to be washed and the brine buffer solution. The brine buffer solution is returned to the brine tank. The pressure of the second compressed air is 0.3 MPa, and the pressure inside the saturated ion exchange column in the drainage zone is 0.2 MPa.

[0089] (3) Lithium washing treatment: The above-mentioned deionization exchange column to be washed is transferred to the lithium washing area, and industrial water is introduced at a flow rate of 42m³. 3 A flow rate of / h is fed into the lithium washing zone for lithium washing treatment, yielding the ion exchange column to be analyzed and the lithium washing solution. The lithium washing solution is returned to the brine tank. The industrial water consists of: Li + 0.01 mg / L, Mg 2+ 38 mg / L, Ca 2+ 20 mg / L, Na + 80 mg / L, K + B: 5 mg / L, SO4: 0.3 mg / L 2- 100 mg / L, Cl - 110mg / .

[0090] (4) Desorption treatment: The ion exchange columns to be desorbed are sequentially transferred to the desorption zone for desorption treatment. The 24℃ deionized water is then introduced at a flow rate of 40m. 3 A flow rate of / h is sequentially pumped into the desorption zone to obtain the ion exchange column to be recovered and the first desorption solution. The first desorption solution is then passed into the desorption water tank for storage. The composition of the deionized water is: Li + 0.8 mg / L, Mg 2+ 0.1 mg / L, Ca 2+ 0.08 mg / L, Na + 20 mg / L, K + B: 0.3 mg / L, SO4: 16 mg / L 2- 0.3 mg / L, Cl - 30 mg / L.

[0091] (5) Eluent Recovery Process: The ion exchange columns to be recovered are sequentially transferred to the recovery zone for eluent recovery. Third compressed air is introduced into the ion exchange columns to recover the adsorbed eluent, resulting in an empty ion exchange column and a second eluent. The second eluent is then introduced into an eluent water tank and mixed with the first eluent to form an eluent for storage. The pressure of the third compressed air is 0.3 MPa, and the internal pressure of the ion exchange columns to be recovered is 0.2 MPa.

[0092] Example 2

[0093] The difference between this embodiment and Embodiment 1 is that the composition of the lithium-containing brine is shown in Table 2 below.

[0094] Table 2

[0095]

[0096] The continuous moving lithium extraction process from lithium-containing brine provided in this embodiment includes the following steps:

[0097] (1) Adsorption treatment and bed loosening treatment: Lithium-containing brine is pumped into the adsorption zone for adsorption treatment. Each empty ion exchange column in the adsorption zone is equipped with an adsorption bed, which is filled with aluminum-based adsorbent. The adsorption capacity of the aluminum-based adsorbent is 2.5 g / L, and the single column packing is 5 m³. 3 The lithium-containing brine is pumped into the adsorption zone for adsorption treatment, with a total influent flow rate of 250 m³ / h. 3 / / h, after adsorption treatment, a saturated ion exchange column and tail brine are obtained. The tail brine is discharged to a tail brine tank for storage. Furthermore, during the adsorption process, the ion exchange column in the adsorption zone is switched to the loosening bed zone, where first compressed air is introduced for loosening treatment. The pressure of the first compressed air is 0.4 MPa, and the flow rate is 150 m³ / h. 3 / h.

[0098] (2) Drainage treatment: The above saturated ion exchange columns are sequentially transferred to the drainage zone. The second compressed air is introduced into the drainage zone for drainage treatment to obtain the ion exchange column to be washed and the brine buffer solution. The brine buffer solution is returned to the brine tank. The pressure of the second compressed air is 0.4 MPa, and the pressure inside the saturated ion exchange column in the drainage zone is 0.3 MPa.

[0099] (3) Lithium washing treatment: The above-mentioned deionization exchange column to be washed is transferred to the lithium washing area, and industrial water is introduced at a flow rate of 45m. 3 A flow rate of / h is fed into the lithium washing zone for lithium washing treatment, yielding the ion exchange column to be analyzed and the lithium washing solution. The lithium washing solution is returned to the brine tank. The industrial water consists of: Li + 0.003 mg / L, Mg 2+ 45 mg / L, Ca 2+ 25 mg / L, Na + 85mg / L, K + B: 4 mg / L, SO4: 0.45 mg / L 2- 90 mg / L, Cl - 120 mg / L.

[0100] (4) Desorption treatment: The ion exchange columns to be desorbed are sequentially transferred to the desorption zone for desorption treatment. The 26℃ deionized water is then desorbed at 65m. 3A flow rate of / h is sequentially pumped into the desorption zone to obtain the ion exchange column to be recovered and the first desorption solution. The first desorption solution is then passed into the desorption water tank for storage. The composition of the deionized water is: Li + 0.7 mg / L, Mg 2+ 0.2 mg / L, Ca 2+ 0 mg / L, Na + 35mg / L, K + B: 0.1 mg / L, SO4: 30 mg / L 2- 0.1 mg / L, Cl - : 40mg / L.

[0101] (5) Eluent Recovery Process: The ion exchange columns to be recovered are sequentially transferred to the recovery zone for eluent recovery. Third compressed air is introduced into the ion exchange columns to recover the adsorbed eluent, resulting in an empty ion exchange column and a second eluent. The second eluent is then introduced into an eluent water tank and mixed with the first eluent to form an eluent for storage. The pressure of the third compressed air is 0.4 MPa, and the internal pressure of the ion exchange columns to be recovered is 0.3 MPa.

[0102] Example 3

[0103] The difference between this embodiment and Embodiment 1 is that the composition of the lithium-containing brine is shown in Table 3 below.

[0104] Table 3

[0105]

[0106] The continuous moving lithium extraction process from lithium-containing brine provided in this embodiment includes the following steps:

[0107] (1) Adsorption treatment and bed loosening treatment: Lithium-containing brine is pumped into the adsorption zone for adsorption treatment. Each ion exchange column in the adsorption zone is equipped with an adsorption bed, which is filled with aluminum-based adsorbent. The adsorption capacity of the aluminum-based adsorbent is 2.5 g / L, and the single column packing is 6 m³. 3 The lithium-containing brine is pumped into the adsorption zone for adsorption treatment, with a total influent flow rate of 400 m³ / s. 3 / / h, after adsorption treatment, a halide-absorbing ion exchange column and tail halide are obtained. The tail halide is discharged to a tail halide tank for storage. Furthermore, during the adsorption process, the ion exchange column in the adsorption zone is switched to the loosening bed zone where first compressed air is introduced for loosening treatment. The pressure of the first compressed air is 0.5 MPa, and the flow rate is 200 m³ / s. 3 / h.

[0108] (2) Drainage treatment: The above-mentioned halide ion exchange columns are sequentially transferred to the drainage zone. The second compressed air is introduced into the drainage zone for drainage treatment to obtain the ion exchange column to be washed and the brine buffer solution. The brine buffer solution is returned to the brine tank. The pressure of the second compressed air is 0.5 MPa, and the pressure inside the halide ion exchange column in the drainage zone is 0.4 MPa.

[0109] (3) Lithium washing treatment: The above-mentioned deionization exchange column to be washed is transferred to the lithium washing area, and industrial water is introduced at a flow rate of 47m³. 3 A flow rate of / h is fed into the lithium washing zone for lithium washing treatment, resulting in an empty ion exchange column and lithium washing solution. The lithium washing solution is returned to the brine tank. The industrial water consists of: Li + 0.02 mg / L, Mg 2+ 30 mg / L, Ca 2+ 36 mg / L, Na + 75mg / L, K + B: 6 mg / L, SO4: 0.2 mg / L 2- 120 mg / L, Cl - 100mg / L.

[0110] (4) Desorption treatment: The above-mentioned empty ion exchange columns were sequentially transferred to the desorption zone for desorption treatment. The 28℃ demineralized water was then desorbed at 90m. 3 A flow rate of / h is sequentially pumped into the desorption zone to obtain a saturated ion exchange column and a first desorption solution. The first desorption solution is then passed into a desorption water tank for storage. The composition of the deionized water is: Li + 1.0 mg / L, Mg 2+ 0.05 mg / L, Ca 2+ 0.1 mg / L, Na + 15mg / L, K + B: 0.5 mg / L, SO4: 13 mg / L 2- 0.5 mg / L, Cl - 15 mg / L.

[0111] (5) Eluent Recovery Process: The saturated ion exchange columns are sequentially transferred to the recovery zone for eluent recovery. Third compressed air is introduced into the saturated ion exchange columns to recover the adsorbed eluent, resulting in an ion exchange column and a second eluent. The second eluent is then introduced into an eluent water tank and mixed with the first eluent for storage. The pressure of the third compressed air is 0.5 MPa, and the internal pressure of the saturated ion exchange column is 0.4 MPa.

[0112] Example 4

[0113] The difference between this embodiment and embodiment 2 is that, in step (4), the temperature of the deionized water used for desorption treatment is 25°C.

[0114] Example 5

[0115] The difference between this embodiment and Embodiment 2 is that the pressures of the first compressed air, the second compressed air, and the third compressed air are all 0.1 MPa.

[0116] Example 6

[0117] The difference between this embodiment and Embodiment 2 is that the pressures of the first compressed air, the second compressed air, and the third compressed air are all 0.8 MPa.

[0118] Comparative Example 1

[0119] The difference between this comparative example and Example 2 is that, in step (4), the temperature of the deionized water used for desorption treatment is 20°C.

[0120] Comparative Example 2

[0121] The difference between this comparative example and Example 2 is that, in step (4), the temperature of the deionized water used for desorption treatment is 35°C.

[0122] Test case

[0123] The eluent obtained in step (4) of each embodiment was measured and the lithium recovery rate was calculated. The content of major ions in the eluent and the lithium recovery rate are shown in Table 4 below.

[0124] The lithium recovery rate is calculated as follows: (lithium concentration in the eluent) (Total volume of eluent) / (Volume of lithium-containing brine feed) (Lithium concentration in lithium-containing brine).

[0125] Table 4

[0126]

[0127] Note: (1) In Table 4, the concentration units of Li, Na, K, Mg, Ca and B are all mg / L.

[0128] (2) In Table 4, Mg / Li refers to the mass ratio of Mg to Li in the solution; K / Li refers to the mass ratio of potassium to lithium; and Na / Li refers to the mass ratio of sodium to lithium.

[0129] The comparison between Examples 1-4 and Comparative Examples 1-2 shows that the temperature of the demineralized water has a significant impact on the recovery rate. A demineralized water temperature of 24-28°C is more conducive to improving the lithium recovery rate and reducing the magnesium-lithium ratio, potassium-lithium ratio, and sodium-lithium ratio.

[0130] A comparison of Examples 1-4 and Examples 5-6 shows that controlling the pressure of the first compressed air, the second compressed air, and the third compressed air to 0.3~0.5MPa is more conducive to improving the recovery of lithium and reducing the magnesium-lithium ratio, potassium-lithium ratio, and sodium-lithium ratio in the solution.

[0131] The above-described embodiments of this application achieve the following technical effects: The continuous moving adsorption lithium extraction process for lithium-containing brine provided in this application introduces a first compressed air to loosen the adsorption bed in a full-column state of the ion exchange column, thereby improving the mass transfer efficiency of the lithium-containing brine; by introducing a second compressed air as the draining medium for the saturated ion exchange column, lithium loss caused by traditional water washing is reduced, and the reduction in potassium ion enrichment in the tail brine caused by water washing is avoided, thus shortening the potassium ion concentration time and improving the production efficiency of potassium fertilizer; by introducing industrial water as the lithium washing medium, the lithium recovery rate is improved while saving water resources; by introducing a third compressed air as the draining medium for the saturated ion exchange column, the enrichment and recovery rate of lithium ions in the eluent are improved while saving water resources.

[0132] The above description is merely a preferred embodiment of this application and is not intended to limit this application. Various modifications and variations can be made to this application by those skilled in the art. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of this application should be included within the protection scope of this application.

Claims

1. A continuous moving lithium extraction process from lithium-containing brine, characterized in that, include: Step S1: Lithium-containing brine is passed into an empty ion exchange column for adsorption treatment, and compressed air is introduced into the column at full capacity for bed loosening treatment to obtain a saturated ion exchange column and tail brine; wherein, the empty ion exchange column is provided with an adsorption bed. Step S2: Pass the second compressed air into the saturated ion exchange column for drainage treatment to obtain the ion exchange column to be washed and the brine buffer solution. Step S3: Industrial water is passed into the ion exchange column to be washed for lithium washing treatment to obtain the ion exchange column to be analyzed and the lithium washing solution. Step S4: The demineralized water is passed into the ion exchange column to be analyzed for analysis, resulting in a first analysis solution and the ion exchange column to be recovered; wherein, the temperature of the demineralized water is 24~28℃; Step S5: Pass the third compressed air into the ion exchange column to be recycled for the recovery of the eluent, and obtain the empty ion exchange column and the second eluent. Mix the second eluent and the first eluent to obtain the eluent.

2. The continuous moving lithium extraction process from lithium-containing brine according to claim 1, characterized in that, In step S1, the adsorption bed is filled with an aluminum-based adsorbent, and the single-column packing amount of the aluminum-based adsorbent is 5~6m. 3 ; And / or, in step S1, the lithium-containing brine includes: Li + 0.04~0.30 g / L, Mg 2+ 48~85g / L, Ca 2+ 0.25~0.5g / L, Na + 6~45g / L, K + :7.5~13.5g / L, B: 0.1~0.2g / L, SO4 2- 9.5~13g / L, Cl - : 171~270g / L; And / or, the tail brine is used to produce potash fertilizer.

3. The continuous moving lithium extraction process from lithium-containing brine according to claim 1, characterized in that, In step S1, the pressure of the first compressed air is 0.3~0.5MPa; And / or, the flow rate of the first compressed air is 100~200m³. 3 / h; And / or, the first compressed air intake method is bottom inlet and top outlet.

4. The continuous moving lithium extraction process from lithium-containing brine according to claim 1, characterized in that, In step S2, the pressure of the second compressed air is 0.3~0.5MPa; And / or, during the drainage process, the pressure inside the saturated exchange column is 0.2~0.4 MPa; And / or, the brine buffer solution is returned to step S1 and mixed with the lithium-containing brine to continue the adsorption treatment.

5. The continuous moving lithium extraction process from lithium-containing brine according to claim 1, characterized in that, In step S3, the industrial water includes: Li + 0.003~0.02 mg / L, Mg 2+ 30~45mg / L, Ca 2+ 25~36mg / L, Na + 75~85mg / L, K + : 4~6mg / L, B: 0.2~0.45mg / L, SO4 2- 90~120mg / L, Cl - 100~120mg / L; And / or, the lithium washing solution is returned to step S1 and mixed with the lithium-containing brine to continue the adsorption treatment.

6. The continuous moving lithium extraction process from lithium-containing brine according to claim 1, characterized in that, In step S4, the demineralized water includes: Li + 0.7~1.0 mg / L, Mg 2+ 0.05~0.2 mg / L, Ca 2+ 0~0.1 mg / L, Na + 15~35mg / L, K + :0.1~0.5mg / L, B: 13~30mg / L, SO4 2- 0.1~0.5 mg / L, Cl - : 15~40mg / L.

7. The continuous moving lithium extraction process from lithium-containing brine according to claim 1, characterized in that, In step S5, the pressure of the third compressed air is 0.3~0.5MPa; And / or, when performing the recovery treatment of the eluent, the pressure inside the ion exchange column to be recovered is 0.2~0.4MPa.

8. The continuous moving lithium extraction process from lithium-containing brine according to claim 1, characterized in that, In the eluent, Li + The concentration is 0.45~1.8g / L, and the magnesium-lithium ratio is ≤4:1, preferably ≤3:1; And / or, in the eluent, the potassium-to-lithium ratio is ≤0.45:1, preferably ≤0.25:1; And / or, in the eluent, the sodium-lithium ratio is ≤0.45:1, preferably ≤0.25:

1.

9. The continuous moving lithium extraction process from lithium-containing brine according to any one of claims 1 to 8, characterized in that, The continuous moving lithium extraction process from lithium-containing brine is carried out in a continuous moving adsorption system. This system includes a support plate, an adsorption zone, a bed thinning zone, a recovery zone, a desorption zone, a lithium washing zone, and a drainage zone. The adsorption zone includes a first adsorption zone and a second adsorption zone. The bed thinning zone is located between the first and second adsorption zones. The first adsorption zone, the bed thinning zone, the second adsorption zone, the recovery zone, the desorption zone, the lithium washing zone, and the drainage zone are arranged sequentially around the axis of the support plate. The support plate is equipped with multiple ion exchange columns, which are sequentially distributed around the axis of the support plate in the first adsorption zone, the bed thinning zone, the second adsorption zone, the recovery zone, the desorption zone, the lithium washing zone, and the drainage zone. The axis of the support plate is rotatable around its own axis, allowing any one of the multiple ion exchange columns to enter the adsorption zone, the bed thinning zone, the recovery zone, the desorption zone, the lithium washing zone, and the drainage zone.

10. The continuous moving lithium extraction process from lithium-containing brine according to claim 9, characterized in that, The first adsorption zone and the second adsorption zone are connected in series, and each of the first adsorption zone and the second adsorption zone is provided with 9 ion exchange columns. The liquid inlet method of the first adsorption zone is top inlet and bottom outlet, and the liquid inlet method of the second adsorption zone is bottom inlet and top outlet. And / or, the sparse bed zone is provided with one ion exchange column, and the gas inlet method of the sparse bed zone is bottom inlet and top outlet; And / or, the recovery zone is equipped with one ion exchange column, and the gas inlet of the recovery zone is top inlet and bottom outlet; And / or, the analysis zone includes a first analysis zone, a second analysis zone, and a third analysis zone arranged in series, each of the first analysis zone, the second analysis zone, and the third analysis zone being provided with two ion exchange columns, and the liquid inlet method of the first analysis zone, the second analysis zone, and the third analysis zone being independently top-in and bottom-out; And / or, the lithium washing zone is provided with three ion exchange columns arranged in series, and the liquid inlet method of the lithium washing zone is top inlet and bottom outlet; And / or, the drainage zone is equipped with one ion exchange column, and the air intake method of the drainage zone is top inlet and bottom outlet.

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