CN111729350A - Equipment for extracting lithium from brine by adsorption method - Google Patents
Equipment for extracting lithium from brine by adsorption method Download PDFInfo
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- CN111729350A CN111729350A CN202010645609.XA CN202010645609A CN111729350A CN 111729350 A CN111729350 A CN 111729350A CN 202010645609 A CN202010645609 A CN 202010645609A CN 111729350 A CN111729350 A CN 111729350A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
- B01D15/02—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor with moving adsorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D33/00—Filters with filtering elements which move during the filtering operation
- B01D33/04—Filters with filtering elements which move during the filtering operation with filtering bands or the like supported on cylinders which are impervious for filtering
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D33/00—Filters with filtering elements which move during the filtering operation
- B01D33/58—Handling the filter cake in the filter for purposes other than for regenerating the filter cake remaining on the filtering element
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D33/00—Filters with filtering elements which move during the filtering operation
- B01D33/58—Handling the filter cake in the filter for purposes other than for regenerating the filter cake remaining on the filtering element
- B01D33/60—Handling the filter cake in the filter for purposes other than for regenerating the filter cake remaining on the filtering element for washing
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D15/00—Lithium compounds
- C01D15/02—Oxides; Hydroxides
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D15/00—Lithium compounds
- C01D15/08—Carbonates; Bicarbonates
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Abstract
The invention provides equipment for extracting lithium from brine by an adsorption method, and belongs to the technical field of adsorption lithium extraction equipment. It includes belt vacuum filter, belt vacuum filter be connected with and be used for the solid-liquid mixing mechanism with brine and adsorbent mixture, belt vacuum filter is last and be equipped with interconnect's raw materials brine district, salt washing district and desorption district along belt vacuum filter's transmission direction in proper order, raw materials brine district is connected to solid-liquid mixing mechanism, salt washing liquid's first liquid conveying mechanism and the second liquid conveying mechanism who carries desorption liquid are connected respectively and are washed salt district and desorption district. Compared with the existing adsorption tower, the invention has low investment cost, greatly reduces the investment and production cost of the subsequent desalting and purifying process, and can stably obtain the battery-grade lithium carbonate or lithium hydroxide finally.
Description
Technical Field
The invention belongs to the technical field of lithium extraction equipment by adsorption, and relates to equipment for extracting lithium from brine by an adsorption method.
Background
The adsorbent and the use form of the adsorbent are the key of the water treatment technology by the adsorption method. Because of the defects of difficult solid-liquid separation, difficult recovery and the like of the powder adsorbent, the water treatment adsorption method after 90 years in the 20 th century generally adopts a process of combining the particle adsorbent with an adsorption tower.
The water treatment adsorbent is mainly divided into an organic adsorbent and an inorganic adsorbent, the organic adsorbent with the diameter of about 1-2mm forms a mature market, and the water treatment adsorbent is filled in an adsorption tower and is widely applied to various fields of water treatment. The granulation process of inorganic adsorbents represented by iron-based adsorbents, aluminum-based adsorbents and manganese-based adsorbents, particularly hydroxyl iron adsorbents, aluminum adsorbents and manganese adsorbents which cannot be formed by calcination, is still lack of a mature and complete solution at present, the granulated inorganic adsorbents are easy to break, and the activity of the granulated adsorbents is far lower than that of powder.
The adsorption method brine lithium extraction technology has wide adaptability to different salt lakes, and can treat brine with low lithium content. The adsorption method brine lithium extraction technology is industrialized on a large scale in Argentina salt lakes and Qinghai salt lakes in China at present. Meanwhile, the adsorption method brine lithium extraction technology has a great deal of research attention, and relates to a plurality of fields of adsorbent synthesis, lithium extraction efficiency of different brines, adsorption reaction mechanisms and the like.
A great deal of research and practice shows that the most efficient adsorbent for extracting lithium from brine is oxide or hydroxide of aluminum series, manganese series, titanium series and the like. The above mentioned metal oxide or hydroxide adsorbent granulation technology is consistently a difficult problem in the water treatment industry. However, the current industrial production line for extracting lithium from brine still follows the technical route of the traditional water treatment adsorption method and adopts a process of combining a granular adsorbent with an adsorption tower.
Because of the properties of lithium adsorbents extracted from brine, studies and patents have proposed extracting lithium from brine using powder adsorbents. In order to realize the recovery of the powder adsorbent, the solid-liquid separation of the adsorbent and water is realized by utilizing a plate-and-frame filter press, a centrifugal machine and a ceramic membrane; there are also studies and patents that carry the magnetic particles on the adsorbent, and then use a magnetic separator to achieve solid-liquid separation.
The technical route of particle adsorbent combined with adsorption tower for lithium extraction from brine has some problems: 1) in the production stage, a large number of adsorption towers filled with the adsorbent are required to be constructed, so that the investment cost is high; 2) magnesium to lithium ratio of greater than 3:1, salt to lithium ratio TDS: a desorption solution with Li larger than 30: 1; 3) the lithium recovery rate of the adsorption section is generally less than 60%, and if high lithium recovery rate is to be realized, multi-tower series connection and function conversion are required, so that the difficulty of industrial continuous production is greatly improved.
The brine lithium extraction process of combining a powder adsorbent with a plate-and-frame filter press, a centrifuge, a precise filter or a ceramic membrane is still in a laboratory or a pilot-scale stage at present, relevant documents and patents only pay attention to solid-liquid separation of the powder adsorbent and brine, and the understanding and the attention to the washing process of the adsorbent in the brine lithium extraction process are lacked, so that desorption liquid with low salt-lithium ratio cannot be obtained by the processes.
The total salinity of the brine can reach hundreds of grams per liter, and the lithium content is only dozens to hundreds of milligrams per liter. Through a large number of research experiments, the applicant finds that how to reduce the ratio of the lithium salt in the desorption solution to the maximum extent in the process of extracting the lithium in the brine by using the adsorption method is the key point of extracting the lithium from the brine by using the adsorption method.
Disclosure of Invention
The invention aims to solve the problems and provides equipment for extracting lithium from brine by an adsorption method.
In order to achieve the purpose, the invention adopts the following technical scheme:
the utility model provides an equipment for lithium is carried to adsorption process brine, includes belt vacuum filter, belt vacuum filter be connected with and be used for the solid-liquid mixing mechanism who mixes brine and adsorbent, belt vacuum filter is last and be equipped with interconnect's raw materials brine district, salt washing district and desorption district along belt vacuum filter's transmission direction in proper order, raw materials brine district is connected to solid-liquid mixing mechanism, salt washing liquid's first liquid conveying mechanism and the second liquid conveying mechanism who carries desorption liquid are connected respectively and are washed salt district and desorption district.
In foretell equipment for adsorption process brine carries lithium, first liquid conveying mechanism include at least two mutually independent and wash salt solution circulation subassembly that connects gradually, different wash salt solution circulation subassemblies are connected one by a side to the opposite side that is close to desorption district.
In the above-mentioned equipment for adsorption process brine lithium extraction, the discharge gate of the salt washing liquid circulation component closest to the raw material brine area is connected with the tail of the belt vacuum filter, the salt washing liquid conveyor is arranged above the salt washing liquid circulation component closest to the desorption area, and the discharge gate of the salt washing liquid circulation component on one side close to the desorption area in every two adjacent salt washing liquid circulation components is positioned above the belt vacuum filter and corresponds to the feed inlet of the other salt washing liquid circulation component.
In foretell equipment for adsorption process brine carries lithium, the salt solution circulation subassembly wash salt solution vacuum box including connecting belt vacuum filter to and connect the salt solution conveying assembly who washes the salt solution vacuum box, every two adjacent salt solution circulation subassemblies wash salt solution conveying assembly's that is close to on the salt solution circulation subassembly of desorption district one side discharge gate is located belt vacuum filter top and corresponds with the salt solution vacuum box that washes on another salt solution circulation subassembly.
In the above-mentioned equipment for adsorption process brine lithium extraction, second liquid conveying mechanism include at least two desorption liquid circulation subassemblies that are independent each other and connect gradually, different desorption liquid circulation subassemblies are connected one by one to the opposite side by keeping away from one side in salt washing district.
In the above-mentioned equipment for adsorption method brine lithium extraction, the discharge port of the desorption liquid circulation component closest to the salt washing zone is connected with the subsequent finishing process, the feed port of the desorption liquid circulation component farthest from the salt washing zone is connected with the desorption liquid conveyor located above the belt vacuum filter, and the discharge port of the desorption liquid circulation component on one side of each two adjacent desorption liquid circulation components far from the salt washing zone is located above the belt vacuum filter and corresponds to the feed port of the other desorption liquid circulation component.
In the above-mentioned equipment for adsorption method brine lithium extraction, the desorption liquid circulation component includes the desorption liquid vacuum box of connecting the belt vacuum filter to and the desorption liquid conveying component of connecting the desorption liquid vacuum box, and the desorption liquid conveying component on the desorption liquid circulation component that keeps away from salt-washing area one side in every two adjacent desorption liquid circulation components is located the belt vacuum filter top and corresponds with the desorption liquid vacuum box on another desorption liquid circulation component.
In foretell equipment for adsorption process brine carries lithium, still include the salt washing return water district of connecting the desorption district, first liquid conveying mechanism's discharge gate connect the salt washing return water district.
In foretell an equipment for lithium is carried to adsorption process brine, still including the salt washing return water district of connecting the desorption district, the salt washing return water district is connected to the discharge gate that is closest to the salt washing liquid circulation subassembly in raw materials brine district, and the salt washing return water district passes through the conveyer belt and connects solid-liquid mixing mechanism.
In foretell be arranged in adsorption process brine to carry lithium equipment, the salt washing return water district including the salt washing return water vacuum box who connects belt vacuum filter, the salt washing return water vacuum box is connected through salt washing return water conveying component and is washed salt recovery solid-liquid separation ware, raw materials brine district passes through raw materials brine conveying component and connects raw materials brine solid-liquid separation ware.
Compared with the prior art, the invention has the advantages that:
1. compared with the existing adsorption tower, the invention has low investment cost, and can reduce the investment cost by about 80 percent.
2. The desorption solution with the magnesium-lithium ratio of less than 1:1 and the salt-lithium ratio (TDS/Li) of less than 10:1 can be obtained by the method, so that the investment and production cost of the subsequent desalting and purifying process are greatly reduced, and finally, the battery-grade lithium carbonate or lithium hydroxide can be stably obtained.
3. The loss of the adsorbent is small, and the leakage rate of the adsorbent in a single adsorption and desorption cycle is less than 0.01 percent.
Additional advantages, objects, and features of the invention will be set forth in part in the description which follows and in part will become apparent to those having ordinary skill in the art upon examination of the following or may be learned from practice of the invention.
Drawings
FIG. 1 is a schematic structural view of the present invention;
FIG. 2 is a schematic view of a portion of the present invention;
fig. 3 is a partial structural schematic diagram of the present invention.
In the figure: the system comprises a solid-liquid mixing mechanism 1, a mixing tank 1a, a raw material brine area 2, a salt washing area 3, a desorption area 4, a first liquid conveying mechanism 5, a second liquid conveying mechanism 6, a salt washing liquid circulating component 7, a salt washing liquid collecting tank 7a, a salt washing liquid vacuum box 8, a salt washing liquid conveying component 9, a desorption liquid circulating component 10, a desorption liquid vacuum box 11, a desorption liquid conveying component 11a, a salt washing water return area 12, a conveying belt 13, a salt washing water return vacuum box 14, a salt washing water return conveying component 15, a salt washing recovery solid-liquid separator 16, a raw material brine conveying component 17, a raw material brine solid-liquid separator 18, a belt type vacuum filter 100, a rack 101, a filter cloth 102 and a scraper 103.
Detailed Description
The invention is further described below with reference to the accompanying drawings.
As shown in fig. 1-3, an apparatus for extracting lithium from adsorption-process brine comprises a belt vacuum filter 100, wherein the belt vacuum filter 100 is connected with a solid-liquid mixing mechanism 1 for mixing brine with an adsorbent, a raw material brine area 2, a salt washing area 3 and a desorption area 4 which are connected with each other are sequentially arranged on the belt vacuum filter 100 along the transmission direction of the belt vacuum filter 100, the solid-liquid mixing mechanism 1 is connected with the raw material brine area 2, and a first liquid conveying mechanism 5 for conveying the salt washing liquid and a second liquid conveying mechanism 6 for conveying the desorption liquid are respectively connected with the salt washing area 3 and the desorption area 4.
In this embodiment, the raw material brine zone 2, the salt-washing zone 3 and the desorption zone 4 are connected to each other in the belt vacuum filter 100, and these zones are set by dividing the zones in which the materials or liquids of the solid-liquid mixing means 1, the first liquid conveying means 5 and the second liquid conveying means 6 are in contact with the belt vacuum filter 100. The belt vacuum filter 100 is a conventional filter 100, which can be a commercially available product, and specifically, the belt vacuum filter 100 includes a frame 101 and a filter cloth 102 on the frame 101, the filter cloth 102 is connected end to end in an annular shape, and a motor on the frame 101 is driven by a tensioning wheel and other components to rotate in a circumferential circulating manner.
The filter cloth 102 is used for solid-liquid separation, i.e. the adsorbent is separated from the liquid, preferably, the filter cloth 102 is selected from a filter cloth with large ventilation volume, and the ventilation volume of the filter cloth is more than 500L/m2S to ensure the processing capacity of separating the brine from the adsorbent, and the retention rate of the adsorbent is more than 90 percent.
The solid-liquid mixing mechanism 1 mixes the adsorbent with brine, lithium-containing salt and other salts in the brine are adsorbed by the adsorbent, the solid-liquid mixing mechanism 1 conveys the mixture to the raw material brine area 2, the adsorbent and the brine in the raw material brine area 2 realize solid-liquid separation, the brine penetrates through the filter cloth 102, and the adsorbent is positioned on the filter cloth 102.
The solid-liquid mixing mechanism 1 comprises a mixing tank 1a, wherein a stirring paddle is arranged in the mixing tank 1a and used for stirring the adsorbent and brine, the mixing tank 1a can be directly arranged above the raw material brine area 2, so that the adsorbent and the brine mixture can be directly sprinkled on the filter cloth 102 of the raw material brine area 2, or the mixing tank 1a is connected through a delivery pump, so that the adsorbent and the brine mixture are input on the filter cloth 102 of the raw material brine area 2. The brine is pumped into the mixing tank 1a, and the adsorbent can be directly added into the mixing tank 1a or added into the mixing tank 1a through a conveying belt.
The salt washing liquid is fresh water and is pumped above the salt washing area 3 by a delivery pump, i.e. the first liquid delivery mechanism 5 can be a delivery pump for delivering fresh water.
As a preferred solution, as shown in fig. 3, the first liquid conveying mechanism 5 includes at least two mutually independent and sequentially connected wash salt circulation assemblies 7, and different wash salt circulation assemblies 7 are connected one by one from one side close to the desorption region 4 to the other side. That is, the brine circulating assemblies 7 are implemented in series with each other.
The discharge hole of the salt washing liquid circulation component 7 closest to the raw material brine area 2 is connected with the tail part of the belt type vacuum filter 100, wherein the tail part refers to the tail end of the filter cloth 102, and the effluent water of the salt washing liquid circulation component 7 closest to the raw material brine area 2 returns to the tail end of the filter cloth 102, so that the salt content in the adsorbent on the filter cloth 102 is increased.
A salt washing liquid conveyor is arranged above the salt washing liquid circulating assembly 7 closest to the desorption area 4, is a spray head connected with a conveying pump or a pipeline and the like, and is used for spraying fresh water on the adsorbent of the filter cloth 102 directly so as to separate salt in the adsorbent.
In this embodiment, the manner of connecting the multiple brine-washing circulation modules 7 in series actually forms the effect of gradient elution, and also conforms to the principle of a small amount of multiple times in chemistry, so as to elute the miscellaneous salts in the adsorbent in advance.
The discharge hole of the salt washing liquid circulation assembly 7 close to one side of the desorption area 4 in every two adjacent salt washing liquid circulation assemblies 7 is positioned above the belt type vacuum filter 100 and corresponds to the feed hole of the other salt washing liquid circulation assembly 7. With the structure, the salt concentration in the salt washing liquid from the salt washing liquid circulation component 7 close to the desorption region 4 to the salt washing liquid circulation component 7 far away from the desorption region 4 is sequentially increased, so that the incremental gradient elution is realized, and the elution efficiency is improved.
The applicants have found that the lithium salt adsorbed by the adsorbent is less readily desorbed as the salt concentration in the brine is higher, and that the lithium is less readily eluted as the salt-to-lithium ratio (ratio of normal salt to lithium-containing salt) in the adsorbent is higher. The invention provides a gradient elution structure in consideration of satisfying the requirements of desalting by washing and reducing the elution of lithium salt. The principle of the gradient elution structure is: the salt content of the brine discharged from the discharge port of the brine circulation module 7 gradually increases from the direction close to the desorption zone 4 to the direction close to the raw material brine zone 2, that is, the brine closest to the desorption zone 4 is pure water, and the brine closest to the raw material brine zone 2 contains partially desorbed lithium salts and other eluted miscellaneous salts. The advantage is that the salt content of the salt washing solution along the transmission direction of the filter cloth 102 is gradually decreased, the salt is gradually eluted, and the probability of synchronous elution of the lithium salt in the elution process is greatly reduced, so that the lithium salt is prevented from being eluted in advance, and other miscellaneous salts are better eluted.
In this embodiment, a structure for re-adsorbing and recovering lithium salt from the discharge port of the brine circulating module 7 closest to the raw material brine zone 2 is also provided. Namely, the device also comprises a washed salt water return area 12 connected with the desorption area 4, and the discharge hole of the first liquid conveying mechanism 5 is connected with the washed salt water return area 12. Specifically, the discharge port of the salt washing liquid circulating component 7 closest to the raw material brine area 2 is connected with the salt washing water return area 12. Because the washing salt return water area 12 is connected behind the desorption area 4, the lithium salt in the absorbent reaching the washing salt return water area 12 is desorbed, or the content of the lithium salt in the absorbent is extremely low, the lithium salt contained in the return water at the discharge port of the washing salt solution circulation component 7 can be absorbed by the absorbent again, thereby avoiding the waste of the lithium salt.
The specific structure of the gradient salt wash is as follows: the salt washing liquid circulating assembly 7 comprises a salt washing liquid vacuum box 8 connected with the belt type vacuum filter 100 and a salt washing liquid conveying assembly 9 connected with the salt washing liquid vacuum box 8, and a discharge hole of the salt washing liquid conveying assembly 9 on the salt washing liquid circulating assembly 7 on one side, close to the desorption area 4, of every two adjacent salt washing liquid circulating assemblies 7 is positioned above the belt type vacuum filter 100 and corresponds to the salt washing liquid vacuum box 8 on the other salt washing liquid circulating assembly 7.
The salt washing liquid circulation component 7 comprises a salt washing liquid collecting tank 7a connected with a salt washing liquid vacuum box 8, the salt washing liquid collecting tank 7a is connected with a vacuum pump and a conveying pump, the salt washing liquid is transferred through the conveying pump, the salt washing liquid reaches the upper portion of the filter cloth 102, an adsorbent on the filter cloth is leached, vacuum is generated through the vacuum pump, and liquid on the filter cloth 102 is sucked into the salt washing liquid collecting tank 7 a. The salt washing water of the salt washing liquid circulation component 7 closest to the raw material brine area 2 is pumped to the upper part of the salt washing water return area 12 by a delivery pump to carry out leaching on the adsorbent.
The water distribution structure is arranged above the salt washing liquid vacuum box 8, the water distribution structure can be a pipe or a plurality of pipes are arranged at intervals along the axial direction of the belt type vacuum filter 100, the water distribution structure is connected with a salt washing liquid water inlet, the water distribution structure closest to the desorption area 4 is directly connected with a salt washing liquid conveyor, the salt washing liquid circulation component 7 closest to the raw material brine area 2 is not connected with the water distribution structure, and the outlets of the other salt washing liquid circulation components 7 are connected with the water distribution structure.
The second liquid conveying mechanism 6 comprises at least two mutually independent desorption liquid circulating assemblies 10 which are connected in sequence, and different desorption liquid circulating assemblies 10 are connected one by one from one side far away from the salt washing area 3 to the other side.
It will be appreciated that the desorption liquid circulation module 10 may be constructed identically to the wash salt circulation module 7, and functions to transport liquid to elute the lithium salts from the adsorbent by washing the adsorbent on the filter cloth 102 with liquid.
In this embodiment, the desorption liquid circulation module 10 is also connected in series to achieve the effect of gradient elution. The discharge port of the desorption liquid circulation assembly 10 closest to the salt washing zone 3 is connected with a subsequent finishing working section, which is a subsequent working section, such as filtration, concentration and the like, but the finishing working section is the prior art, and does not belong to the structure of the invention or the technical problem to be solved by the invention.
The feed inlet of the desorption liquid circulation component 10 farthest from the salt washing area 3 is connected with a desorption liquid conveyor positioned above the belt vacuum filter 100, the desorption liquid conveyor can be a conveying pump for directly conveying pure water, and the discharge outlet of the desorption liquid circulation component 10 on one side, far from the salt washing area 3, of every two adjacent desorption liquid circulation components 10 is positioned above the belt vacuum filter 100 and corresponds to the feed inlet of the other desorption liquid circulation component 10.
Along the conveying direction of the filter cloth 102 of the vacuum filter 100, the lithium content in the desorption liquid is gradually reduced, and finally the pure water is used for desorbing the adsorbent, so that the lithium in the adsorbent can be sufficiently eluted.
The desorption liquid circulation component 10 comprises a desorption liquid vacuum box 11 connected with the belt vacuum filter 100 and a desorption liquid conveying component 11a connected with the desorption liquid vacuum box 11, wherein the desorption liquid conveying component on the desorption liquid circulation component 10 on one side, far away from the salt washing area 3, of every two adjacent desorption liquid circulation components 10 is positioned above the belt vacuum filter 100 and corresponds to the desorption liquid vacuum box 11 on the other desorption liquid circulation component 10. The desorption liquid conveying assembly 11a comprises a collecting tank and a conveying pump which are connected with the desorption liquid vacuum box 11, wherein an outlet of the conveying pump and a pipeline of one desorption liquid circulation assembly 10 corresponds to the desorption liquid vacuum box 11 on the other adjacent desorption liquid circulation assembly 10.
Similarly, a water distribution structure is also arranged above each desorption liquid vacuum box 11, the water distribution structure can be directly provided with a plurality of openings on a pipeline or a spray head, and the water distribution structure sprays the desorption liquid to spray the adsorbent on the filter cloth 102, so that the lithium salt is washed out of the adsorbent. This elution mode has a great advantage: because the lithium content in the adsorbent on the filter cloth 102 of the belt vacuum filter 100 is transported backwards, the lithium content is less and is less likely to be desorbed, and after the desorption liquid circulation assembly 10 of the embodiment is in a serial structure, the lithium content in the desorption liquid is also smaller backwards along with the transport direction of the filter cloth 102, that is, along with the transport direction of the filter cloth 102, the lithium content in the desorption liquid from different desorption liquid circulation assemblies 10 and the lithium content in the adsorbent on the filter cloth 102 show a positive correlation, and finally, pure water is used as the desorption liquid to directly desorb and elute the adsorbent with the least lithium content, thereby achieving the effect of complete elution.
It should be noted that the brine from the brine recycle module 7 closest to the raw brine zone 2 can be directed to the brine pan. However, the treatment can reduce the salt content of brine in the salt pan, and the brine washing also contains certain lithium, which is directly discharged into the salt pan to cause incomplete lithium adsorption, thereby affecting the extraction rate of lithium. Therefore, as a preferable scheme, the present embodiment is provided with a salt washing water returning area 12 after the desorption area 4, the discharge port of the salt washing liquid circulation component 7 closest to the raw material brine area 2 is connected with the salt washing water returning area 12, and the water discharged from the salt washing liquid circulation component 7 rinses the adsorbent on the salt washing water returning area 12.
The salt washing water return area 12 is connected with the solid-liquid mixing mechanism 1 through a conveying belt 13. Specifically, a scraper 103 is arranged at a position, corresponding to the tail of the filter cloth 102, on the frame 101, the scraper 103 scrapes off the adsorbent on the filter cloth 102, and then the adsorbent falls onto the conveyer belt 13, the conveyer belt 13 is connected with the mixing tank 1a, the adsorbent returns to the mixing tank 1a again and is mixed with brine to adsorb lithium salt in the brine, and the adsorbent completes adsorption-desorption-reabsorption cycle.
The salt washing water return area 12 comprises a salt washing water return vacuum box 14 connected with the belt type vacuum filter 100, the salt washing water return vacuum box 14 is connected with a salt washing recovery solid-liquid separator 16 through a salt washing water return conveying component 15, and the raw material brine area 2 is connected with a raw material brine solid-liquid separator 18 through a raw material brine conveying component 17.
In this embodiment, the solid-liquid separator 16 is one or more of a bag filter, a compact filter, a magnetic separator, a three-leg centrifuge, and a disc separator. When the adsorbent is a magnetic adsorbent, a magnetic separator can be selected, and when the adsorbent is a non-magnetic adsorbent, other solid-liquid separation equipment except the magnetic separator is selected.
The working process of the invention is as follows:
the adsorbent is put into the mixing tank 1a, brine in the salt pan is pumped into the mixing tank, the solid-liquid ratio is 1:10-200, specifically, according to the type selection of the vacuum filter 100 and the salt content of the brine, and the salt in the brine is adsorbed by the adsorbent under the stirring state.
The mixture of the adsorbent and the brine is put into a raw material brine area 2 from a mixing tank, the brine penetrates through the filter cloth 102 under the vacuum action of the belt type vacuum filter 100, the adsorbent is isolated on the filter cloth 102, the adsorbent reaches a salt washing area 3 along with the transmission of the filter cloth 102, the salt washing liquid leaches the adsorbent on the filter cloth above the salt washing area 3, the miscellaneous salts in the adsorbent are eluted, the salt washing liquid after elution returns to a salt washing water return area 12, and the adsorbent in the salt washing water return area 12 is leached, so that the adsorbent adsorbs the adsorbent and lithium salt which are permeated and filtered in the salt washing liquid.
After the adsorbent in the salt washing area 3 enters the desorption area 4, the lithium salt in the adsorbent is sucked out after the desorption liquid is washed, and the lithium salt-containing liquid is obtained after the lithium salt-containing liquid is collected by the desorption liquid circulation component 10 and can enter the next procedure for treatment.
The applicant finds through a large number of experiments that the minimum ventilation amount of the filter cloth for different brine separation is not less than 500L/m2 & s, so that the ideal processing capacity of the belt type vacuum filter can be met, and the leakage amount of the adsorbent under different use conditions is different but is generally less than 10%. The content of the adsorbent in the brine, the salt washing liquid and the desorption liquid passing through the filter cloth of the belt type vacuum filter is generally lower than 1 percent.
And performing solid-liquid separation on the brine, the salt washing liquid and the desorption liquid with the solid content of less than 1% by a magnetic separator, a precise filtering device or a ceramic membrane for secondary treatment, and then discharging the brine, the salt washing liquid and the desorption liquid to a salt field or treating the brine, the salt washing liquid and the desorption liquid in a post-system. If the adsorbent contains magnetic substances, the adsorbent can be recovered by a magnetic separator, and if the adsorbent does not contain magnetic substances, the adsorbent can be recovered by a precise filtration device or a ceramic membrane.
The adsorbent filtered by the belt vacuum filter is subjected to secondary capture by a magnetic separator, a precise filtering device and a ceramic membrane, and then backflushed to the corresponding water supply port of the belt vacuum filter, and further returned to the main adsorption and desorption circulation. The trapping rate of the belt filter to the adsorbent is more than 90%, and the trapping rate of the rear-section solid-liquid separation equipment to the adsorbent is more than 99.9%, so that the leakage rate of the adsorbent in a single adsorption and desorption cycle is less than 0.01%.
The belt type vacuum filter provided by the invention can realize the small water volume quick washing of the adsorbent, the desorption regeneration of the adsorbent and the recovery of the lithium lost from salt washing. The desorption solution with the magnesium-lithium ratio of less than 1:1 and the salt-lithium ratio (TDS/Li) of less than 10:1 can be obtained by the method, so that the investment and production cost of the subsequent desalting and purifying process are greatly reduced, and finally, the battery-grade lithium carbonate or lithium hydroxide can be stably obtained. The new equipment provided by the invention can recover lithium ions lost in the salt washing process, so that the lithium ion recovery rate in the brine adsorption and desorption process can reach more than 80%.
The specific embodiments described herein are merely illustrative of the spirit of the invention. Various modifications or additions may be made to the described embodiments or alternatives may be employed by those skilled in the art without departing from the spirit of the invention.
Claims (10)
1. The utility model provides an equipment for adsorption process brine carries lithium, includes belt vacuum filter (100), its characterized in that, belt vacuum filter (100) be connected with and be used for solid-liquid mixing mechanism (1) with brine and adsorbent mixture, belt vacuum filter (100) go up and be equipped with interconnect's raw materials brine district (2) in proper order along the transmission direction of belt vacuum filter (100), wash salt district (3) and desorption district (4), raw materials brine district (2) is connected in solid-liquid mixing mechanism (1), carry first liquid conveying mechanism (5) of washing salt liquid and carry second liquid conveying mechanism (6) of desorption liquid and connect respectively and wash salt district (3) and desorption district (4).
2. The apparatus for extraction of lithium from adsorption brine according to claim 1, wherein the first liquid delivery mechanism (5) comprises at least two mutually independent and sequentially connected brine-scrubbing circulation assemblies (7), and the different brine-scrubbing circulation assemblies (7) are connected one by one from one side close to the desorption zone (4) to the other side.
3. The equipment for extracting lithium from brine by adsorption method according to claim 2, characterized in that the discharge port of the salt washing liquid circulating component (7) closest to the raw material brine area (2) is connected with the tail part of the belt type vacuum filter (100), a salt washing liquid conveyer is arranged above the salt washing liquid circulating component (7) closest to the desorption area (4), and the discharge port of the salt washing liquid circulating component (7) on one side close to the desorption area (4) in every two adjacent salt washing liquid circulating components (7) is positioned above the belt type vacuum filter (100) and corresponds to the feed port of the other salt washing liquid circulating component (7).
4. The equipment for extracting lithium from brine by adsorption method according to claim 3, wherein the salt washing liquid circulation component (7) comprises a salt washing liquid vacuum box (8) connected with the belt type vacuum filter (100) and a salt washing liquid conveying component (9) connected with the salt washing liquid vacuum box (8), and the discharge port of the salt washing liquid conveying component (9) on the salt washing liquid circulation component (7) close to one side of the desorption area (4) in every two adjacent salt washing liquid circulation components (7) is positioned above the belt type vacuum filter (100) and corresponds to the salt washing liquid vacuum box (8) on the other salt washing liquid circulation component (7).
5. The apparatus for extraction of lithium from adsorptive brine according to claim 1, wherein said second liquid transport mechanism (6) comprises at least two desorption liquid circulation modules (10) independent from each other and connected in sequence, wherein different desorption liquid circulation modules (10) are connected one by one from one side far away from the salt-washing zone (3) to the other.
6. The equipment for extracting lithium from adsorption brine according to claim 5, wherein the discharge port of the desorption liquid circulation assembly (10) closest to the salt washing area (3) is connected with the subsequent finishing section, the feed port of the desorption liquid circulation assembly (10) farthest from the salt washing area (3) is connected with a desorption liquid conveyer positioned above the belt vacuum filter (100), and the discharge port of the desorption liquid circulation assembly (10) on the side far from the salt washing area (3) in each two adjacent desorption liquid circulation assemblies (10) is positioned above the belt vacuum filter (100) and corresponds to the feed port of the other desorption liquid circulation assembly (10).
7. The equipment for extracting lithium from adsorption brine according to claim 6, wherein the desorption liquid circulation assemblies (10) comprise a desorption liquid vacuum box (11) connected with the belt vacuum filter (100) and a desorption liquid conveying assembly (11a) connected with the desorption liquid vacuum box (11), and the desorption liquid conveying assembly (11a) on the desorption liquid circulation assembly (10) on the side far away from the salt washing area (3) in each two adjacent desorption liquid circulation assemblies (10) is positioned above the belt vacuum filter (100) and corresponds to the desorption liquid vacuum box (11) on the other desorption liquid circulation assembly (10).
8. The equipment for extracting lithium from brine by an adsorption method according to claim 1, further comprising a salt washing water return area (12) connected with the desorption area (4), wherein the discharge port of the first liquid conveying mechanism (5) is connected with the salt washing water return area (12).
9. The equipment for extracting lithium from brine by an adsorption method according to claim 2, further comprising a salt washing water return area (12) connected with the desorption area (4), wherein a discharge port of the salt washing liquid circulation component (7) closest to the raw material brine area (2) is connected with the salt washing water return area (12), and the salt washing water return area (12) is connected with the solid-liquid mixing mechanism (1) through a conveying belt (13).
10. The equipment for extracting lithium from adsorption brine according to claim 8 or 9, wherein the salt washing water return area (12) comprises a salt washing water return vacuum box (14) connected with the belt type vacuum filter (100), the salt washing water return vacuum box (14) is connected with a salt washing water return solid-liquid separator (16) through a salt washing water return conveying component (15), and the raw brine area (2) is connected with a raw brine solid-liquid separator (18) through a raw brine conveying component (17).
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| CN202010645609.XA CN111729350B (en) | 2020-07-07 | 2020-07-07 | Equipment for extracting lithium from brine by adsorption method |
| PCT/CN2021/104835 WO2022007811A1 (en) | 2020-07-07 | 2021-07-06 | Device for extracting lithium from brine by using adsorption method |
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| CN202010645609.XA CN111729350B (en) | 2020-07-07 | 2020-07-07 | Equipment for extracting lithium from brine by adsorption method |
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| CN111729350B CN111729350B (en) | 2023-09-08 |
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| WO2022007662A1 (en) * | 2020-07-07 | 2022-01-13 | 浙江衢州明德新材料有限公司 | Band filter and application thereof in extraction of lithium from brine using adsorption method |
| WO2022007660A1 (en) * | 2020-07-07 | 2022-01-13 | 浙江衢州明德新材料有限公司 | Method for extracting lithium from brine by using powdered adsorbent |
| WO2022007811A1 (en) * | 2020-07-07 | 2022-01-13 | 浙江衢州明德新材料有限公司 | Device for extracting lithium from brine by using adsorption method |
| CN115261639A (en) * | 2022-07-18 | 2022-11-01 | 西宁永正锂业有限公司 | Nondestructive recovery process, nondestructive recovery device and nondestructive circulation system of powdery adsorbent for lithium extraction from brine |
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| CN114906966A (en) * | 2022-05-11 | 2022-08-16 | 顶峰油脂化工(泰兴)有限公司 | Vacuum belt type salt washing filter and treatment method of salt-containing wastewater |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101012072A (en) * | 2006-12-31 | 2007-08-08 | 于向真 | Adsorption treatment process for sewage |
| CN209123481U (en) * | 2018-08-30 | 2019-07-19 | 成都泰利创富锂业科技有限公司 | A kind of continuous adsorption-desorption system mentioning lithium for industry |
| CN210583956U (en) * | 2019-08-20 | 2020-05-22 | 白银扎布耶锂业有限公司 | A vacuum belt filter washes edulcoration device for lithium ore pulp |
| CN212700660U (en) * | 2020-07-07 | 2021-03-16 | 浙江衢州明德新材料有限公司 | Equipment for extracting lithium from brine by adsorption method |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201404729Y (en) * | 2009-05-20 | 2010-02-17 | 湖州核华机械有限公司 | Horizontal band type vacuum filter |
| CN109650413B (en) * | 2018-12-07 | 2021-05-25 | 三门峡联利新材料有限公司 | Method and system for enriching lithium from sodium aluminate solution in alumina plant |
| CN209773034U (en) * | 2019-01-21 | 2019-12-13 | 潍坊鑫山环保重工科技有限公司 | dewatering and chlorine reducing device for alkali residue produced in alkali production by ammonia-soda process |
| CN111729350B (en) * | 2020-07-07 | 2023-09-08 | 衢州永正锂业科技有限公司 | Equipment for extracting lithium from brine by adsorption method |
| CN213221206U (en) * | 2020-07-07 | 2021-05-18 | 浙江衢州明德新材料有限公司 | Salt-washing backwater structure for lithium extraction device |
| CN213221252U (en) * | 2020-07-07 | 2021-05-18 | 浙江衢州明德新材料有限公司 | Salt lithium separation device applied to brine lithium extraction process |
| CN111826531A (en) * | 2020-07-07 | 2020-10-27 | 浙江衢州明德新材料有限公司 | Method for extracting lithium from brine by using powdery adsorbent |
| CN111825152B (en) * | 2020-07-07 | 2022-11-01 | 西宁永正锂业有限公司 | Belt filter and application thereof in adsorption method brine lithium extraction |
-
2020
- 2020-07-07 CN CN202010645609.XA patent/CN111729350B/en active Active
-
2021
- 2021-07-06 WO PCT/CN2021/104835 patent/WO2022007811A1/en active Application Filing
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101012072A (en) * | 2006-12-31 | 2007-08-08 | 于向真 | Adsorption treatment process for sewage |
| CN209123481U (en) * | 2018-08-30 | 2019-07-19 | 成都泰利创富锂业科技有限公司 | A kind of continuous adsorption-desorption system mentioning lithium for industry |
| CN210583956U (en) * | 2019-08-20 | 2020-05-22 | 白银扎布耶锂业有限公司 | A vacuum belt filter washes edulcoration device for lithium ore pulp |
| CN212700660U (en) * | 2020-07-07 | 2021-03-16 | 浙江衢州明德新材料有限公司 | Equipment for extracting lithium from brine by adsorption method |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2022007662A1 (en) * | 2020-07-07 | 2022-01-13 | 浙江衢州明德新材料有限公司 | Band filter and application thereof in extraction of lithium from brine using adsorption method |
| WO2022007660A1 (en) * | 2020-07-07 | 2022-01-13 | 浙江衢州明德新材料有限公司 | Method for extracting lithium from brine by using powdered adsorbent |
| WO2022007811A1 (en) * | 2020-07-07 | 2022-01-13 | 浙江衢州明德新材料有限公司 | Device for extracting lithium from brine by using adsorption method |
| CN115261639A (en) * | 2022-07-18 | 2022-11-01 | 西宁永正锂业有限公司 | Nondestructive recovery process, nondestructive recovery device and nondestructive circulation system of powdery adsorbent for lithium extraction from brine |
| CN115261639B (en) * | 2022-07-18 | 2024-07-26 | 衢州永正锂业科技有限公司 | Nondestructive recovery process, nondestructive recovery device and nondestructive circulation system of powdery adsorbent for extracting lithium from brine |
| CN115992315A (en) * | 2023-03-23 | 2023-04-21 | 河北云瑞化工设备有限公司 | Device and method for extracting lithium from salt lake brine with high magnesium-lithium ratio |
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| WO2022007811A1 (en) | 2022-01-13 |
| CN111729350B (en) | 2023-09-08 |
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