WO2022007811A1 - Device for extracting lithium from brine by using adsorption method - Google Patents

Device for extracting lithium from brine by using adsorption method Download PDF

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Publication number
WO2022007811A1
WO2022007811A1 PCT/CN2021/104835 CN2021104835W WO2022007811A1 WO 2022007811 A1 WO2022007811 A1 WO 2022007811A1 CN 2021104835 W CN2021104835 W CN 2021104835W WO 2022007811 A1 WO2022007811 A1 WO 2022007811A1
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Prior art keywords
washing
salt
liquid
brine
desorption
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PCT/CN2021/104835
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French (fr)
Chinese (zh)
Inventor
李亦然
沈芳明
马君耀
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浙江衢州明德新材料有限公司
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Publication of WO2022007811A1 publication Critical patent/WO2022007811A1/en

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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
    • 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
    • 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
    • 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
    • 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
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • the invention belongs to the technical field of lithium extraction equipment by adsorption, and relates to a device for extracting lithium from brine by an adsorption method.
  • Adsorbent and the form of use of adsorbent are the key to adsorption water treatment technology. Due to the difficulties of solid-liquid separation and difficult recovery of powder adsorbents, the process of combining granular adsorbents with adsorption towers has been widely used in water treatment adsorption methods since the 1990s.
  • Water treatment adsorbents are mainly divided into two categories: organic and inorganic.
  • Organic adsorbents with a diameter of about 1-2mm have formed a mature market, and their filling in adsorption towers has been widely used in various fields of water treatment.
  • Lithium extraction from brine by adsorption has wide adaptability to different salt lakes and can handle brine with low lithium content.
  • the technology of lithium extraction from brine by adsorption has achieved large-scale industrialization in Argentina Salt Lake and Qinghai Salt Lake in my country.
  • there has been a lot of research attention on the extraction of lithium from brine by adsorption involving the synthesis of adsorbents, the efficiency of lithium extraction from different brines, and the mechanism of adsorption reaction.
  • the total salinity of brine can reach hundreds of grams per liter, while the lithium content in it is only tens to hundreds of mg per liter.
  • the applicant of this patent has found through a lot of research and experiments that in the process of extracting lithium from brine by adsorption, how to minimize the salt-to-lithium ratio in the desorption solution is the key to extracting lithium from brine by adsorption.
  • the purpose of the present invention is to address the above-mentioned problems, and to provide a device for extracting lithium from brine by adsorption.
  • a device for extracting lithium from brine by adsorption method including a belt vacuum filter, the belt vacuum filter is connected with a solid-liquid mixing mechanism for mixing brine and adsorbent, and the belt vacuum filter is connected along the belt vacuum filter.
  • the transmission direction of the belt vacuum filter is sequentially provided with a raw brine area, a salt washing area and a desorption area that are connected to each other.
  • the solid-liquid mixing mechanism is connected to the raw brine area.
  • Two liquid conveying mechanisms are respectively connected to the salt washing zone and the desorption zone.
  • the first liquid conveying mechanism includes at least two washing salt liquid circulation components that are independent of each other and connected in sequence, and different washing salt liquid circulation components Connect side to side one by one.
  • the discharge port of the brine circulation component closest to the raw brine area is connected to the tail of the belt vacuum filter, and the brine circulation component closest to the desorption area is provided with a Washing salt liquid conveyor, the discharge port of the washing salt liquid circulation assembly on the side near the desorption zone in each adjacent two washing salt liquid circulation assemblies is located above the belt vacuum filter and is connected with the other washing salt liquid circulation assembly. corresponding to the feeding port.
  • the salt-washing liquid circulation assembly includes a salt-washing liquid vacuum box connected to a belt vacuum filter, and a washing-salt-liquid conveying assembly connected to the washing salt liquid vacuum box,
  • the discharge port of the washing salt liquid conveying assembly on the washing salt liquid circulation assembly on the side of the desorption zone in each of the two adjacent washing salt liquid circulation assemblies is located above the belt vacuum filter and is connected with the other washing salt liquid circulation assembly.
  • the second liquid conveying mechanism includes at least two desorption liquid circulation components that are independent of each other and are connected in sequence, and different desorption liquid circulation components are composed of a remote from the salt washing area. Connect side to side one by one.
  • the discharge port of the desorption liquid circulation component closest to the salt washing area is connected to the subsequent finishing section, and the feed port of the desorption liquid circulation component farthest from the salt washing area is connected to the
  • the desorption liquid conveyor above the belt vacuum filter, the discharge port of the desorption liquid circulation component on the side away from the salt washing area in each adjacent two desorption liquid circulation components is located above the belt vacuum filter and is connected with the other desorption liquid.
  • the feed port of the liquid circulation component corresponds.
  • the desorption liquid circulation assembly includes a desorption liquid vacuum box connected to a belt vacuum filter, and a desorption liquid conveying assembly connected to the desorption liquid vacuum box.
  • the desorbing fluid conveying component on the side far from the salt washing area is located above the belt vacuum filter and corresponds to the desorbing fluid vacuum box on the other desorbing fluid circulating component.
  • the equipment for extracting lithium from brine by adsorption method also includes a salt-washing backwater area connected to the desorption zone, and the discharge port of the first liquid conveying mechanism is connected to the salt-washing backwater area.
  • the equipment for extracting lithium from brine by adsorption method also includes a washing salt return water area connected to the desorption area, and the discharge port of the washing salt liquid circulation component closest to the raw brine area is connected to the washing salt return water area.
  • the backwater area is connected to the solid-liquid mixing mechanism through a conveyor belt.
  • the salt water return area includes a salt water return vacuum box connected to a belt vacuum filter, and the salt water return vacuum box passes through the salt water return conveying assembly Connect the washing salt recovery solid-liquid separator, and the raw material brine area is connected to the raw material brine solid-liquid separator through the raw material brine conveying component.
  • the investment cost of the present invention is low, and the investment cost can be reduced by about 80%.
  • a desorption solution with a magnesium-lithium ratio of less than 1:1 and a salt-to-lithium ratio (TDS/Li) of less than 10:1 can be obtained, which greatly reduces the investment and production cost of the subsequent desalination and purification process, and can finally obtain a battery stably grade lithium carbonate or lithium hydroxide.
  • the loss of adsorbent is small, and the leakage rate of adsorbent in a single adsorption and desorption cycle is less than 0.01%.
  • Fig. 1 is the structural representation of the present invention
  • Fig. 2 is the partial structure schematic diagram of the present invention
  • FIG. 3 is a schematic diagram of a partial structure of the present invention.
  • solid-liquid mixing mechanism 1 mixing tank 1a, raw brine area 2, salt washing area 3, desorption area 4, first liquid conveying mechanism 5, second liquid conveying mechanism 6, washing salt liquid circulation component 7, washing salt Liquid collection tank 7a, washing salt liquid vacuum box 8, washing salt liquid conveying assembly 9, desorbing liquid circulation assembly 10, desorbing liquid vacuum box 11, desorbing liquid conveying assembly 11a, washing salt water return area 12, conveyor belt 13, washing salt Return water vacuum box 14, washing salt return water conveying assembly 15, washing salt recovery solid-liquid separator 16, raw brine conveying assembly 17, raw brine solid-liquid separator 18, belt vacuum filter 100, rack 101, filter cloth 102.
  • Scraper 103 scraper 103.
  • a device for extracting lithium from brine by adsorption method includes a belt vacuum filter 100, and the belt vacuum filter 100 is connected with a solid-liquid mixing device for mixing brine and adsorbent Mechanism 1, on the belt vacuum filter 100 and along the transmission direction of the belt vacuum filter 100, there are sequentially connected raw brine area 2, salt washing area 3 and desorption area 4, and the solid-liquid mixing mechanism 1 is connected to the raw brine.
  • the first liquid transport mechanism 5 for transporting the washing salt solution and the second liquid transport mechanism 6 for transporting the desorption liquid are connected to the salt washing zone 3 and the desorption zone 4, respectively.
  • the raw brine area 2, the salt washing area 3 and the desorption area 4 are connected to each other in the belt vacuum filter 100, and the settings of these areas are based on the solid-liquid mixing mechanism 1, the first liquid conveying mechanism 5
  • the area where the material or liquid of the second liquid conveying mechanism 6 is in contact with the belt vacuum filter 100 is divided.
  • the belt vacuum filter 100 is in the prior art, and commercially available products can be used.
  • 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. Ring, the motor on the frame 101 drives the lower circumferential circular rotation through components such as tensioning pulleys.
  • the filter cloth 102 is used for solid-liquid separation, that is, the adsorbent and the liquid are separated.
  • the filter cloth 102 is preferably a filter cloth with a large ventilation volume, and the ventilation volume of the filter cloth is greater than 500 L/m 2 ⁇ s, so as to ensure the processing capacity of the separation of brine and adsorbent. , the retention rate of the adsorbent is greater than 90%.
  • the solid-liquid mixing mechanism 1 mixes the adsorbent with the brine, the lithium-containing salts and other salts in the brine are adsorbed by the adsorbent, and the solid-liquid mixing mechanism 1 transports the mixture to the raw brine zone 2, where the adsorbent and the raw material brine zone 2.
  • the brine realizes solid-liquid separation, the brine penetrates the filter cloth 102 , and the adsorbent is located on the filter cloth 102 .
  • the solid-liquid mixing mechanism 1 includes a mixing tank 1a with a stirring paddle in the mixing tank 1a for stirring the adsorbent and brine.
  • the mixing tank 1a can be directly placed above the raw brine area 2, so that the adsorbent and brine mixture can be directly sprinkled on the surface.
  • the brine is pumped into the mixing tank 1a, and the adsorbent can be directly added to the mixing tank 1a, or added to the mixing tank 1a through a conveyor belt.
  • the salt-washing liquid adopts fresh water, and is sent to the top of the salt-washing area 3 by a conveying pump, that is, the first liquid conveying mechanism 5 may be a conveying pump for conveying fresh water.
  • the first liquid conveying mechanism 5 includes at least two washing salt liquid circulation assemblies 7 which are independent of each other and are connected in sequence. Connect side to side one by one. That is to say, the washing salt solution circulation components 7 are connected in series with each other.
  • the discharge port of the salt washing liquid circulation assembly 7 closest to the raw brine zone 2 is connected to the tail of the belt vacuum filter 100, where the tail refers to the end of the filter cloth 102, and the discharge port of the washing salt liquid circulation assembly 7 closest to the raw brine zone 2.
  • the effluent returns to the end of the filter cloth 102 to increase the salt content in the adsorbent on the filter cloth 102 .
  • a salt washing liquid conveyor is provided above the washing salt liquid circulation component 7 closest to the desorption zone 4, and the washing salt liquid conveyor is a nozzle or a pipeline connected to a conveying pump, and is used to directly spray fresh water on the adsorbent of the filter cloth 102 to remove the salts from the adsorbent.
  • the way of connecting a plurality of washing salt solution circulation components 7 in series actually forms the effect of gradient elution, and also conforms to the principle of small amount and many times in chemistry, and pre-eluting the miscellaneous salts in the adsorbent.
  • the discharge port of the washing salt liquid circulation assembly 7 on the side close to the desorption zone 4 is located above the belt vacuum filter 100 and is connected with the inlet of the other washing salt liquid circulation assembly 7. corresponding to the mouth.
  • the present invention creatively proposes a structure of gradient elution.
  • the principle of the gradient elution structure is: the salt content of the washing salt solution from the discharge port of the washing salt solution circulation component 7 gradually increases from the direction close to the desorption zone 4 to the direction close to the raw brine zone 2, that is, the most The washing salt solution near the desorption zone 4 is pure water, and the washing salt solution closest to the raw brine zone 2 contains partially desorbed lithium salts and other eluted miscellaneous salts.
  • This advantage is that the salt content of the washing salt solution along the transmission direction of the filter cloth 102 decreases gradually, the salt is gradually eluted, and the probability that the lithium salt is synchronously eluted during the elution process is greatly reduced, thereby preventing the lithium salt from being washed in advance. It also makes other miscellaneous salts get better elution.
  • This embodiment also provides a structure for re-adsorbing and recovering the lithium salt coming out of the discharge port of the salt washing liquid circulation component 7 closest to the raw brine zone 2 . That is, it also includes a salt water return area 12 connected to the desorption area 4 , and the discharge port of the first liquid conveying mechanism 5 is connected to the wash salt water return area 12 . Specifically, the discharge port of the washing salt liquid circulation component 7 closest to the raw brine zone 2 is connected to the washing salt return water zone 12 .
  • the salt-washing backwater zone 12 Since the salt-washing backwater zone 12 is connected behind the desorption zone 4, the lithium salt in the adsorbent that reaches the salt-washing backwater zone 12 has been desorbed, or the lithium salt content in the adsorbent is extremely low, and the salt-washing liquid circulates The lithium salt contained in the return water of the outlet of the component 7 can be adsorbed by the adsorbent again, thereby avoiding the waste of lithium salt.
  • the washing salt solution circulation assembly 7 includes a washing salt solution vacuum box 8 connected to the belt vacuum filter 100, and a washing salt solution conveying component 9 connected to the washing salt solution vacuum box 8.
  • Each phase The discharge port of the washing salt liquid conveying assembly 9 on the washing salt liquid circulation assembly 7 on the side close to the desorption zone 4 of the two adjacent washing salt liquid circulation assemblies 7 is located above the belt vacuum filter 100 and is connected with the other washing salt liquid.
  • the washing salt liquid vacuum box 8 on the liquid circulation assembly 7 corresponds.
  • the washing salt liquid circulation assembly 7 includes a washing salt liquid collecting tank 7a connected to the washing salt liquid vacuum box 8, and the washing salt liquid collecting tank 7a is connected to a vacuum pump and a transfer pump, and the washing salt liquid is transferred through the transfer pump, so that the washing salt liquid reaches the filter cloth 102 Above, the adsorbent on the filter cloth is rinsed, a vacuum is generated by a vacuum pump, and the liquid on the filter cloth 102 is sucked into the washing salt liquid collection tank 7a.
  • the washing salt water of the washing salt liquid circulation component 7 closest to the raw brine zone 2 is pumped to the top of the washing salt return water zone 12 by a transfer pump to rinse the adsorbent.
  • a water distribution structure is provided above the washing salt solution vacuum box 8, and the water distribution structure can be a tube, or a plurality of tubes are arranged at intervals along the axial direction of the belt vacuum filter 100, and the water distribution structure is connected to the washing salt solution water inlet,
  • the water distribution structure closest to the desorption zone 4 is directly connected to the washing salt liquid conveyor, the washing salt liquid circulation component 7 closest to the raw brine zone 2 is not connected to the water distribution structure, and the outlets of the other washing salt liquid circulation components 7 are connected to a cloth water structure.
  • the second liquid conveying mechanism 6 includes at least two desorption liquid circulation assemblies 10 which are independent of each other and are connected in sequence. Different desorption liquid circulation assemblies 10 are connected one by one from one side away from the salt washing area 3 to the other side.
  • the structure of the desorbing liquid circulation assembly 10 can be the same as that of the washing salt liquid circulation assembly 7, and its function is to transport liquid, wash the adsorbent on the filter cloth 102 through the liquid, and remove the adsorbent in the adsorbent. Lithium salt eluted.
  • the desorption liquid circulation assemblies 10 are also connected in series with each other, so as to achieve the effect of gradient elution.
  • the discharge port of the desorbing liquid circulation assembly 10 closest to the salt washing zone 3 is connected to the subsequent finishing section, which is the subsequent section, such as filtration, concentration, etc., but the finishing section is the prior art and does not belong to the present invention.
  • the structure is not the technical problem to be solved by the present invention.
  • the feed port of the desorption liquid circulation assembly 10 farthest from the salt washing zone 3 is connected to the desorption liquid conveyor located above the belt vacuum filter 100.
  • the desorption liquid conveyor can be a transfer pump, which directly transports pure water.
  • the discharge port of the desorption liquid circulation assembly 10 on the side away from the salt washing zone 3 of the desorption liquid circulation assembly 10 is located above the belt vacuum filter 100 and corresponds to the feed port of the other desorption liquid circulation assembly 10 .
  • the lithium content in the desorption solution gradually decreases, and finally the adsorbent is desorbed by pure water, so that the lithium in the adsorbent can be fully eluted.
  • the desorption liquid circulation assembly 10 includes a desorption liquid vacuum box 11 connected to the belt vacuum filter 100, and a desorption liquid conveying assembly 11a connected to the desorption liquid vacuum box 11. Each adjacent two desorption liquid circulation assemblies 10 are far away from the salt washing area. 3.
  • the desorption liquid conveying assembly on the desorption liquid circulation assembly 10 on one side is located above the belt vacuum filter 100 and corresponds to the desorption liquid vacuum box 11 on the other desorption liquid circulation assembly 10.
  • the desorption liquid conveying assembly 11a includes a collection tank and a conveying pump connected to the desorption liquid vacuum box 11, wherein the outlet of the conveying pump of one desorption liquid circulation assembly 10 is connected to the pipeline and the desorption liquid vacuum on the adjacent other desorption liquid circulation assembly 10. Box 11 corresponds.
  • each desorption liquid vacuum box 11 a water distribution structure is also provided above each desorption liquid vacuum box 11.
  • the water distribution structure can be directly provided with a number of openings on the pipeline, or a spray head, etc.
  • the adsorbent on the cloth 102 is sprayed to wash out the lithium salt from the adsorbent.
  • This elution method has a great advantage: since the lithium content in the adsorbent on the filter cloth 102 of the belt vacuum filter 100 is transported further back, the less the content is, the less likely it is to be desorbed.
  • the lithium content in the desorption liquid decreases with the transmission direction of the filter cloth 102 going backward, that is, with the transmission direction of the filter cloth 102, different desorption liquid circulation assemblies 10
  • the lithium content in the desorbed liquid and the lithium content in the adsorbent on the filter cloth 102 have a positive correlation.
  • pure water is used as the desorption liquid to directly desorb and elute the adsorbent with the least lithium content to achieve Elute complete effect.
  • washing salt water of the washing salt liquid circulation component 7 closest to the raw brine area 2 can be directly sent to the salt field.
  • this treatment will reduce the salt content of the brine in the salt field, and the washing brine also contains a certain amount of lithium. Direct discharge into the salt field results in incomplete lithium adsorption and affects the extraction rate of lithium. Therefore, as a preferred solution, in this embodiment, a washing salt return water zone 12 is set behind the desorption zone 4, and the discharge port of the washing salt liquid circulation component 7 closest to the raw brine zone 2 is connected to the washing salt return water zone. 12. The effluent from the washing salt liquid circulation component 7 rinses the adsorbent on the washing salt return water area 12.
  • the brine backwater area 12 is connected to the solid-liquid mixing mechanism 1 through a conveyor belt 13 .
  • a scraper 103 is provided on the frame 101 at a position corresponding to the tail of the filter cloth 102.
  • the scraper 103 scrapes off the adsorbent on the filter cloth 102 and then drops it onto the conveyor belt 13.
  • the mixing tank 1a is connected, the adsorbent is returned to the mixing tank 1a, mixed with the brine, and the lithium salt in the brine is adsorbed, and the adsorbent completes the cycle of adsorption-desorption-re-adsorption.
  • the washing salt return water area 12 includes a washing salt return water vacuum box 14 connected to the belt vacuum filter 100, and the washing salt return water vacuum box 14 is connected to the washing salt recovery solid-liquid separator 16 through the washing salt return water conveying assembly 15, and the raw material brine Zone 2 is connected to the raw material brine solid-liquid separator 18 through the raw material brine conveying assembly 17 .
  • the solid-liquid separator 16 is one or more of a bag filter, a compact filter, a magnetic separator, a three-legged centrifuge, and a disc separator.
  • a magnetic separator can be selected, and when the adsorbent is a non-magnetic adsorbent, other solid-liquid separation equipment other than the magnetic separator is selected.
  • the working process of the present invention is:
  • the adsorbent is put into the mixing tank 1a, the brine in the salt field is pumped into the mixing tank, and the solid-liquid ratio is 1:10-200. In the state, the salt in the brine is adsorbed by the adsorbent.
  • the mixture of adsorbent and brine is put into the raw brine area 2 from the mixing tank. Under the vacuum action of the belt vacuum filter 100, the brine penetrates the filter cloth 102, and the adsorbent is isolated on the filter cloth 102. 102 drive, the adsorbent reaches the salt washing zone 3, and the washing salt solution washes the adsorbent on the filter cloth above the salt washing zone 3, eluting the miscellaneous salts in the adsorbent, and the washing salt after the elution treatment
  • the liquid is returned to the salt-washing backwater area 12, and the adsorbent in the salt-washing backwater area 12 is rinsed, so that the adsorbent adsorbs the adsorbent and the lithium salt that have been diafiltered in the salt-washing liquid.
  • the lithium salt in the adsorbent is sucked out after being rinsed by the desorption liquid, and is collected by the desorption liquid circulation component 10 to obtain a liquid containing lithium salt, which can enter to the next process for processing.
  • the minimum ventilation volume of the filter cloth should not be less than 500 L/m2 ⁇ s to meet the ideal processing capacity of the belt vacuum filter. A certain difference, but generally less than 10%. At this time, the content of the adsorbent in the brine, washing salt solution and desorption solution passing through the filter cloth of the belt vacuum filter is generally less than 1%.
  • the above-mentioned brine, washing salt solution and desorption solution with a solid content of less than 1% are subjected to solid-liquid separation after secondary treatment by magnetic separator, precision filtration equipment or ceramic membrane, and then discharged to the salt field or entered into the post-system for treatment. If the adsorbent contains magnetic substances, it can be recovered by a magnetic separator. If the adsorbent does not contain magnetic substances, it can be recovered by precision filtration equipment or ceramic membranes.
  • the adsorbent filtered from the belt vacuum filter is collected by the magnetic separator, precision filtration equipment and ceramic membrane for the second time, and then recoiled back to the corresponding water supply port of the belt vacuum filter, and then returned to the main circulation of adsorption and desorption.
  • the capture rate of the adsorbent by the belt filter is greater than 90%, and the capture rate of the adsorbent by the back-end solid-liquid separation equipment is greater than 99.9%, so the leakage rate of the adsorbent in a single adsorption and desorption cycle is less than 0.01%.
  • the belt vacuum filter proposed by the invention can realize the rapid washing of the adsorbent with a small amount of water, the desorption and regeneration of the adsorbent and the recovery of lithium lost by washing salt.
  • the invention can obtain a desorption solution with a magnesium-lithium ratio of less than 1:1 and a salt-to-lithium ratio (TDS/Li) of less than 10:1, which greatly reduces the investment and production cost of the subsequent desalination and purification process, and finally can stably obtain battery-grade carbonic acid.
  • Lithium or Lithium Hydroxide The new equipment proposed by the invention can recover the lithium ions lost in the salt washing process, and then make the brine adsorption and desorption process reach a lithium ion recovery rate of more than 80%.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)
  • Water Treatment By Sorption (AREA)
  • Treatment Of Liquids With Adsorbents In General (AREA)

Abstract

The present invention relates to the technical field of adsorption-based lithium extraction devices, and provides a device extracting lithium from brine by using an adsorption method. The device comprises a belt-type vacuum filter; the belt-type vacuum filter is connected to a solid-liquid mixing mechanism used for mixing brine and an adsorbent; a raw brine area, a salt leaching area, and a desorption area which are connected to each other are successively provided on the belt-type vacuum filter in a transmission direction thereof; the solid-liquid mixing mechanism is connected to the raw brine area; a first liquid delivery mechanism for delivering a salt leaching liquid and a second liquid delivery mechanism for delivering a desorbing liquid are respectively connected to the salt leaching area and the desorption area. Compared with adsorption by the existing adsorption towers, the present invention is low in investment cost, greatly reduces the investment and production costs in subsequent desalting and purification processes, and finally can stably obtain battery-grade lithium carbonate or lithium hydroxide.

Description

用于吸附法卤水提锂的设备Equipment for Lithium Extraction from Brine by Adsorption 技术领域technical field
本发明属于吸附提锂设备技术领域，涉及一种用于吸附法卤水提锂的设备。The invention belongs to the technical field of lithium extraction equipment by adsorption, and relates to a device for extracting lithium from brine by an adsorption method.
背景技术Background technique
吸附剂及吸附剂的使用形式是吸附法水处理技术的关键。由于粉体吸附剂固液分离困难、难回收等缺陷，20世纪90年代以后水处理吸附法已普遍采用颗粒吸附剂结合吸附塔的工艺。Adsorbent and the form of use of adsorbent are the key to adsorption water treatment technology. Due to the difficulties of solid-liquid separation and difficult recovery of powder adsorbents, the process of combining granular adsorbents with adsorption towers has been widely used in water treatment adsorption methods since the 1990s.
水处理吸附剂主要分为有机和无机两大类，直径1-2mm左右的有机吸附剂已形成成熟市场，其填装在吸附塔中已广泛应用于水处理各个领域。以铁系、铝系、锰系等为代表的无机吸附剂，尤其是不能通过煅烧成型的羟基铁、铝、锰等吸附剂，其造粒过程目前尚缺乏成熟、完善的解决方案，造粒后的无机吸附剂往往易破碎，且颗粒吸附剂活性远低于粉体。Water treatment adsorbents are mainly divided into two categories: organic and inorganic. Organic adsorbents with a diameter of about 1-2mm have formed a mature market, and their filling in adsorption towers has been widely used in various fields of water treatment. Inorganic adsorbents represented by iron series, aluminum series, manganese series, etc., especially hydroxyl iron, aluminum, manganese and other adsorbents that cannot be formed by calcination, the granulation process still lacks mature and perfect solutions. The latter inorganic adsorbent is often easily broken, and the activity of the granular adsorbent is much lower than that of the powder.
吸附法卤水提锂技术对不同盐湖有广泛的适应性，可处理低锂含量卤水。吸附法卤水提锂技术目前已在阿根廷盐湖和我国青海盐湖实现规模工业化。同时，吸附法卤水提锂技术已有大量的研究关注，涉及吸附剂合成、不同卤水提锂效率、吸附反应机制等多个领域。Lithium extraction from brine by adsorption has wide adaptability to different salt lakes and can handle brine with low lithium content. At present, the technology of lithium extraction from brine by adsorption has achieved large-scale industrialization in Argentina Salt Lake and Qinghai Salt Lake in my country. At the same time, there has been a lot of research attention on the extraction of lithium from brine by adsorption, involving the synthesis of adsorbents, the efficiency of lithium extraction from different brines, and the mechanism of adsorption reaction.
大量研究和实践表明，卤水提锂最高效的吸附剂是铝系、锰系、钛系等的氧化物或氢氧化物。上述金属氧化物或氢氧化物的吸附剂造粒技术一贯是水处理行业难题。然而，目前卤水提锂工业化产线仍沿袭传统水处理吸附法的技术路线，采用颗粒吸附剂结合吸附塔的工艺。A large number of studies and practices have shown that the most efficient adsorbents for lithium extraction from brine are oxides or hydroxides of aluminum, manganese, and titanium. The above-mentioned metal oxide or hydroxide adsorbent granulation technology has always been a difficult problem in the water treatment industry. However, at present, the industrial production line of lithium extraction from brine still follows the technical route of traditional water treatment adsorption method, and adopts the process of particle adsorbent combined with adsorption tower.
由于卤水提锂吸附剂的特性，已有研究和专利提出了利用粉体吸附剂进行卤水提锂。为了实现粉体吸附剂的回收，有研究利用板框压滤机、离心机和陶瓷膜实现吸附剂与水的固液分离；也有研究和专利将吸附剂载磁，其后利用磁选机实现固液分离。Due to the characteristics of the brine extracting lithium sorbent, the use of powder sorbents to extract lithium from brine has been proposed by research and patents. In order to realize the recovery of powder adsorbent, there are studies using plate and frame filter press, centrifuge and ceramic membrane to realize the solid-liquid separation of adsorbent and water; there are also studies and patents to magnetize adsorbent, and then use magnetic separator to realize Solid-liquid separation.
技术问题technical problem
颗粒吸附剂结合吸附塔的技术路线用于卤水提锂存在一些问题：1）投产阶段需大量构建填满吸附剂的吸附塔，投资成本高昂；2）一般得到镁锂比大于3:1，盐锂比TDS：Li大于30:1的解吸液；3）吸附段锂回收率一般小于60%，若要实现高锂回收率，需设置多塔串联和功能转换，大幅提高工业连续生产的难度。There are some problems in the technical route of using granular adsorbent combined with adsorption tower to extract lithium from brine: 1) In the production stage, a large number of adsorption towers filled with adsorbent need to be constructed, and the investment cost is high; Lithium ratio TDS: Desorption liquid with Li greater than 30:1; 3) The lithium recovery rate in the adsorption section is generally less than 60%. To achieve a high lithium recovery rate, multiple towers in series and function conversion need to be set up, which greatly increases the difficulty of industrial continuous production.
粉体吸附剂结合板框压滤机、离心机、精密过滤或陶瓷膜的卤水提锂工艺目前尚处于实验室或中试阶段，相关文献、专利均仅关注粉体吸附剂与卤水的固液分离，对卤水提锂过程中吸附剂的洗涤过程缺乏认识和关注，因此上述工艺均无法得到低盐锂比解吸液。The process of extracting lithium from brine using powder adsorbents combined with plate and frame filter presses, centrifuges, precision filtration or ceramic membranes is still in the laboratory or pilot stage. Separation, lack of understanding and attention to the washing process of the adsorbent in the process of extracting lithium from brine, so the above processes cannot obtain a low-salt lithium ratio desorbent.
卤水总盐度可达数百克/升，而其中锂含量仅为数十至数百毫克/升。本专利申请者经大量研究试验发现，在利用吸附法提取卤水中锂的过程中，如何最大限度地降低解吸液中的盐锂比是吸附法卤水提锂的关键。The total salinity of brine can reach hundreds of grams per liter, while the lithium content in it is only tens to hundreds of mg per liter. The applicant of this patent has found through a lot of research and experiments that in the process of extracting lithium from brine by adsorption, how to minimize the salt-to-lithium ratio in the desorption solution is the key to extracting lithium from brine by adsorption.
技术解决方案technical solutions
本发明的目的是针对上述问题，提供一种用于吸附法卤水提锂的设备。 The purpose of the present invention is to address the above-mentioned problems, and to provide a device for extracting lithium from brine by adsorption.
为达到上述目的，本发明采用了下列技术方案：To achieve the above object, the present invention has adopted the following technical solutions:
一种用于吸附法卤水提锂的设备，包括带式真空过滤机，所述的带式真空过滤机连接有用于将卤水和吸附剂混合的固液混合机构，带式真空过滤机上并沿着带式真空过滤机的传动方向依次设有相互连接的原料卤水区、洗盐区和解吸区，固液混合机构连接原料卤水区，输送洗盐液的第一液体输送机构和输送解吸液的第二液体输送机构分别连接洗盐区和解吸区。 A device for extracting lithium from brine by adsorption method, including a belt vacuum filter, the belt vacuum filter is connected with a solid-liquid mixing mechanism for mixing brine and adsorbent, and the belt vacuum filter is connected along the belt vacuum filter. The transmission direction of the belt vacuum filter is sequentially provided with a raw brine area, a salt washing area and a desorption area that are connected to each other. The solid-liquid mixing mechanism is connected to the raw brine area. Two liquid conveying mechanisms are respectively connected to the salt washing zone and the desorption zone.
在上述的用于吸附法卤水提锂的设备中，所述的第一液体输送机构包括至少两个相互独立且依次连接的洗盐液循环组件，不同的洗盐液循环组件由靠近解吸区的一侧向另一侧逐个连接。In the above-mentioned equipment for extracting lithium from brine by adsorption, the first liquid conveying mechanism includes at least two washing salt liquid circulation components that are independent of each other and connected in sequence, and different washing salt liquid circulation components Connect side to side one by one.
在上述的用于吸附法卤水提锂的设备中，最靠近原料卤水区的洗盐液循环组件的出料口连接带式真空过滤机尾部，最靠近解吸区的洗盐液循环组件上方设有洗盐液输送器，每相邻的两个洗盐液循环组件中靠近解吸区一侧的洗盐液循环组件的出料口位于带式真空过滤机上方并与另一个洗盐液循环组件的进料口对应。In the above-mentioned equipment for extracting lithium from brine by adsorption method, the discharge port of the brine circulation component closest to the raw brine area is connected to the tail of the belt vacuum filter, and the brine circulation component closest to the desorption area is provided with a Washing salt liquid conveyor, the discharge port of the washing salt liquid circulation assembly on the side near the desorption zone in each adjacent two washing salt liquid circulation assemblies is located above the belt vacuum filter and is connected with the other washing salt liquid circulation assembly. corresponding to the feeding port.
在上述的用于吸附法卤水提锂的设备中，所述的洗盐液循环组件包括连接带式真空过滤机的洗盐液真空盒，以及连接洗盐液真空盒的洗盐液输送组件，每相邻的两个洗盐液循环组件中靠近解吸区一侧的洗盐液循环组件上的洗盐液输送组件的出料口位于带式真空过滤机上方并与另一个洗盐液循环组件上的洗盐液真空盒对应。In the above-mentioned equipment for extracting lithium from brine by adsorption, the salt-washing liquid circulation assembly includes a salt-washing liquid vacuum box connected to a belt vacuum filter, and a washing-salt-liquid conveying assembly connected to the washing salt liquid vacuum box, The discharge port of the washing salt liquid conveying assembly on the washing salt liquid circulation assembly on the side of the desorption zone in each of the two adjacent washing salt liquid circulation assemblies is located above the belt vacuum filter and is connected with the other washing salt liquid circulation assembly. Corresponding to the washing salt solution vacuum box on the.
在上述的用于吸附法卤水提锂的设备中，所述的第二液体输送机构包括至少两个相互独立且依次连接的解吸液循环组件，不同的解吸液循环组件由远离洗盐区的一侧向另一侧逐个连接。In the above-mentioned equipment for extracting lithium from brine by adsorption, the second liquid conveying mechanism includes at least two desorption liquid circulation components that are independent of each other and are connected in sequence, and different desorption liquid circulation components are composed of a remote from the salt washing area. Connect side to side one by one.
在上述的用于吸附法卤水提锂的设备中，最靠近洗盐区的解吸液循环组件的出料口连接后续精加工工段，最远离洗盐区的解吸液循环组件的进料口连接位于带式真空过滤机上方的解吸液输送器，每相邻的两个解吸液循环组件中远离洗盐区一侧的解吸液循环组件的出料口位于带式真空过滤机上方并与另一个解吸液循环组件的进料口对应。In the above-mentioned equipment for extracting lithium from brine by adsorption, the discharge port of the desorption liquid circulation component closest to the salt washing area is connected to the subsequent finishing section, and the feed port of the desorption liquid circulation component farthest from the salt washing area is connected to the The desorption liquid conveyor above the belt vacuum filter, the discharge port of the desorption liquid circulation component on the side away from the salt washing area in each adjacent two desorption liquid circulation components is located above the belt vacuum filter and is connected with the other desorption liquid. The feed port of the liquid circulation component corresponds.
在上述的用于吸附法卤水提锂的设备中，所述的解吸液循环组件包括连接带式真空过滤机的解吸液真空盒，以及连接解吸液真空盒的解吸液输送组件，每相邻的两个解吸液循环组件中远离洗盐区一侧的解吸液循环组件上的解吸液输送组件位于带式真空过滤机上方并与另一个解吸液循环组件上的解吸液真空盒对应。In the above-mentioned equipment for extracting lithium from brine by adsorption, the desorption liquid circulation assembly includes a desorption liquid vacuum box connected to a belt vacuum filter, and a desorption liquid conveying assembly connected to the desorption liquid vacuum box. Among the two desorbing fluid circulation assemblies, the desorbing fluid conveying component on the side far from the salt washing area is located above the belt vacuum filter and corresponds to the desorbing fluid vacuum box on the other desorbing fluid circulating component.
在上述的用于吸附法卤水提锂的设备中，还包括连接解吸区的洗盐回水区，所述的第一液体输送机构的出料口连接洗盐回水区。In the above-mentioned equipment for extracting lithium from brine by adsorption method, it also includes a salt-washing backwater area connected to the desorption zone, and the discharge port of the first liquid conveying mechanism is connected to the salt-washing backwater area.
在上述的用于吸附法卤水提锂的设备中，还包括连接解吸区的洗盐回水区，最靠近原料卤水区的洗盐液循环组件的出料口连接洗盐回水区，洗盐回水区通过输送带连接固液混合机构。In the above-mentioned equipment for extracting lithium from brine by adsorption method, it also includes a washing salt return water area connected to the desorption area, and the discharge port of the washing salt liquid circulation component closest to the raw brine area is connected to the washing salt return water area. The backwater area is connected to the solid-liquid mixing mechanism through a conveyor belt.
在上述的用于吸附法卤水提锂的设备中，所述的洗盐回水区包括连接带式真空过滤机的洗盐回水真空盒，洗盐回水真空盒通过洗盐回水输送组件连接洗盐回收固液分离器，原料卤水区通过原料卤水输送组件连接原料卤水固液分离器。In the above-mentioned equipment for extracting lithium from brine by adsorption, the salt water return area includes a salt water return vacuum box connected to a belt vacuum filter, and the salt water return vacuum box passes through the salt water return conveying assembly Connect the washing salt recovery solid-liquid separator, and the raw material brine area is connected to the raw material brine solid-liquid separator through the raw material brine conveying component.
有益效果beneficial effect
与现有的技术相比，本发明的优点在于：Compared with the prior art, the advantages of the present invention are:
1、相比现有的吸附塔吸附，本发明投资成本低，可降低约80%的投资成本。1. Compared with the adsorption of the existing adsorption tower, the investment cost of the present invention is low, and the investment cost can be reduced by about 80%.
2、利用本发明可以得到镁锂比小于1:1，盐锂比（TDS/Li）小于10:1的解吸液，大幅降低了后续除盐提纯工艺的投资和生产成本，最终可以稳定得到电池级碳酸锂或氢氧化锂。2. Using the present invention, a desorption solution with a magnesium-lithium ratio of less than 1:1 and a salt-to-lithium ratio (TDS/Li) of less than 10:1 can be obtained, which greatly reduces the investment and production cost of the subsequent desalination and purification process, and can finally obtain a battery stably grade lithium carbonate or lithium hydroxide.
3、吸附剂损失小，吸附剂在单次吸附解吸循环中的泄漏率小于0.01%。3. The loss of adsorbent is small, and the leakage rate of adsorbent in a single adsorption and desorption cycle is less than 0.01%.
本发明的其它优点、目标和特征将部分通过下面的说明体现，部分还将通过对本发明的研究和实践而为本领域的技术人员所理解。Other advantages, objects, and features of the present invention will appear in part from the description that follows, and in part will be appreciated by those skilled in the art from the study and practice of the invention.
附图说明Description of drawings
图1是本发明的结构示意图；Fig. 1 is the structural representation of the present invention;
图2是本发明的局部结构示意图；Fig. 2 is the partial structure schematic diagram of the present invention;
图3是本发明的局部结构示意图。FIG. 3 is a schematic diagram of a partial structure of the present invention.
图中：固液混合机构1、混合罐1a、原料卤水区2、洗盐区3、解吸区4、第一液体输送机构5、第二液体输送机构6、洗盐液循环组件7、洗盐液收集罐7a、洗盐液真空盒8、洗盐液输送组件9、解吸液循环组件10、解吸液真空盒11、解吸液输送组件11a、洗盐回水区12、输送带13、洗盐回水真空盒14、洗盐回水输送组件15、洗盐回收固液分离器16、原料卤水输送组件17、原料卤水固液分离器18、带式真空过滤机100、机架101、滤布102、刮板103。In the figure: solid-liquid mixing mechanism 1, mixing tank 1a, raw brine area 2, salt washing area 3, desorption area 4, first liquid conveying mechanism 5, second liquid conveying mechanism 6, washing salt liquid circulation component 7, washing salt Liquid collection tank 7a, washing salt liquid vacuum box 8, washing salt liquid conveying assembly 9, desorbing liquid circulation assembly 10, desorbing liquid vacuum box 11, desorbing liquid conveying assembly 11a, washing salt water return area 12, conveyor belt 13, washing salt Return water vacuum box 14, washing salt return water conveying assembly 15, washing salt recovery solid-liquid separator 16, raw brine conveying assembly 17, raw brine solid-liquid separator 18, belt vacuum filter 100, rack 101, filter cloth 102. Scraper 103.
本发明的最佳实施方式BEST MODE FOR CARRYING OUT THE INVENTION
下面结合附图对本发明进行进一步说明。The present invention will be further described below with reference to the accompanying drawings.
如图1-3所示，一种用于吸附法卤水提锂的设备，包括带式真空过滤机100，所述的带式真空过滤机100连接有用于将卤水和吸附剂混合的固液混合机构1，带式真空过滤机100上并沿着带式真空过滤机100的传动方向依次设有相互连接的原料卤水区2、洗盐区3和解吸区4，固液混合机构1连接原料卤水区2，输送洗盐液的第一液体输送机构5和输送解吸液的第二液体输送机构6分别连接洗盐区3和解吸区4。 As shown in Figures 1-3, a device for extracting lithium from brine by adsorption method includes a belt vacuum filter 100, and the belt vacuum filter 100 is connected with a solid-liquid mixing device for mixing brine and adsorbent Mechanism 1, on the belt vacuum filter 100 and along the transmission direction of the belt vacuum filter 100, there are sequentially connected raw brine area 2, salt washing area 3 and desorption area 4, and the solid-liquid mixing mechanism 1 is connected to the raw brine. In zone 2, the first liquid transport mechanism 5 for transporting the washing salt solution and the second liquid transport mechanism 6 for transporting the desorption liquid are connected to the salt washing zone 3 and the desorption zone 4, respectively.
在本实施例中，原料卤水区2、洗盐区3和解吸区4在带式真空过滤机100为相互连接的，这些区域的设定是根据固液混合机构1、第一液体输送机构5和第二液体输送机构6的物料或液体与带式真空过滤机100接触的区域进行划分的。带式真空过滤机100为现有技术，可采用市售产品，具体的说，带式真空过滤机100包括机架101，以及在机架101上的滤布102，该滤布102首尾连接呈环形，再机架101上的电机通过张紧轮等组件驱动下周向循环转动。In this embodiment, the raw brine area 2, the salt washing area 3 and the desorption area 4 are connected to each other in the belt vacuum filter 100, and the settings of these areas are based on the solid-liquid mixing mechanism 1, the first liquid conveying mechanism 5 The area where the material or liquid of the second liquid conveying mechanism 6 is in contact with the belt vacuum filter 100 is divided. The belt vacuum filter 100 is in the prior art, and commercially available products can be used. 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. Ring, the motor on the frame 101 drives the lower circumferential circular rotation through components such as tensioning pulleys.
滤布102用以固液分离，即将吸附剂和液体进行分离，滤布102优选选用大通气量滤布，滤布通气量大于500 L/m 2·s，以保证卤水与吸附剂分离的处理能力，对吸附剂的截留率大于90%。 The filter cloth 102 is used for solid-liquid separation, that is, the adsorbent and the liquid are separated. The filter cloth 102 is preferably a filter cloth with a large ventilation volume, and the ventilation volume of the filter cloth is greater than 500 L/m 2 ·s, so as to ensure the processing capacity of the separation of brine and adsorbent. , the retention rate of the adsorbent is greater than 90%.
固液混合机构1将吸附剂与卤水混合，卤水中的含锂盐及其他盐被吸附剂吸附，固液混合机构1将混合物输送到原料卤水区2，在该原料卤水区2中吸附剂与卤水实现固液分离，卤水透过滤布102，吸附剂位于滤布102上。The solid-liquid mixing mechanism 1 mixes the adsorbent with the brine, the lithium-containing salts and other salts in the brine are adsorbed by the adsorbent, and the solid-liquid mixing mechanism 1 transports the mixture to the raw brine zone 2, where the adsorbent and the raw material brine zone 2. The brine realizes solid-liquid separation, the brine penetrates the filter cloth 102 , and the adsorbent is located on the filter cloth 102 .
固液混合机构1包括一个混合罐1a，混合罐1a里面具有搅拌桨，用于搅拌吸附剂和卤水，混合罐1a可直接置于原料卤水区2上方，使吸附剂与卤水混合物能直接洒落在原料卤水区2的滤布102上，或者通过输送泵连接混合罐1a，使吸附剂与卤水混合物输入到原料卤水区2的滤布102上。卤水采用泵送到混合罐1a中，吸附剂可直接加入混合罐1a，或者通过输送带加入到混合罐1a中。The solid-liquid mixing mechanism 1 includes a mixing tank 1a with a stirring paddle in the mixing tank 1a for stirring the adsorbent and brine. The mixing tank 1a can be directly placed above the raw brine area 2, so that the adsorbent and brine mixture can be directly sprinkled on the surface. On the filter cloth 102 of the raw brine zone 2, or connected to the mixing tank 1a through a transfer pump, the mixture of adsorbent and brine is input to the filter cloth 102 of the raw brine zone 2. The brine is pumped into the mixing tank 1a, and the adsorbent can be directly added to the mixing tank 1a, or added to the mixing tank 1a through a conveyor belt.
洗盐液采用淡水，通过输送泵送到洗盐区3上方，也即第一液体输送机构5可以为输送淡水的输送泵。The salt-washing liquid adopts fresh water, and is sent to the top of the salt-washing area 3 by a conveying pump, that is, the first liquid conveying mechanism 5 may be a conveying pump for conveying fresh water.
作为一种优选的方案，结合图3所示，第一液体输送机构5包括至少两个相互独立且依次连接的洗盐液循环组件7，不同的洗盐液循环组件7由靠近解吸区4的一侧向另一侧逐个连接。也就是说，洗盐液循环组件7实现相互串联。As a preferred solution, as shown in FIG. 3 , the first liquid conveying mechanism 5 includes at least two washing salt liquid circulation assemblies 7 which are independent of each other and are connected in sequence. Connect side to side one by one. That is to say, the washing salt solution circulation components 7 are connected in series with each other.
最靠近原料卤水区2的洗盐液循环组件7的出料口连接带式真空过滤机100尾部，这里的尾部是指滤布102末端，最靠近原料卤水区2的洗盐液循环组件7的出水回到滤布102末端上，增加滤布102上的吸附剂中的含盐量。The discharge port of the salt washing liquid circulation assembly 7 closest to the raw brine zone 2 is connected to the tail of the belt vacuum filter 100, where the tail refers to the end of the filter cloth 102, and the discharge port of the washing salt liquid circulation assembly 7 closest to the raw brine zone 2. The effluent returns to the end of the filter cloth 102 to increase the salt content in the adsorbent on the filter cloth 102 .
最靠近解吸区4的洗盐液循环组件7上方设有洗盐液输送器，洗盐液输送器为连接输送泵的喷头或者是管道等，用于将淡水直接喷洒在滤布102的吸附剂上，从而将吸附剂中的盐脱离。A salt washing liquid conveyor is provided above the washing salt liquid circulation component 7 closest to the desorption zone 4, and the washing salt liquid conveyor is a nozzle or a pipeline connected to a conveying pump, and is used to directly spray fresh water on the adsorbent of the filter cloth 102 to remove the salts from the adsorbent.
在本实施例中，多个洗盐液循环组件7串联连接的方式，实际上是形成梯度洗脱的效果，也符合化学中少量多次的原则，将吸附剂中的杂盐预先洗脱。In this embodiment, the way of connecting a plurality of washing salt solution circulation components 7 in series actually forms the effect of gradient elution, and also conforms to the principle of small amount and many times in chemistry, and pre-eluting the miscellaneous salts in the adsorbent.
每相邻的两个洗盐液循环组件7中靠近解吸区4一侧的洗盐液循环组件7的出料口位于带式真空过滤机100上方并与另一个洗盐液循环组件7的进料口对应。这种结构，靠近近解吸区4的洗盐液循环组件7到远离解吸区4的洗盐液循环组件7的洗盐液中的盐浓度依次递增，实现递增式的梯度洗脱提高洗脱的效率。In each of the two adjacent washing salt liquid circulation assemblies 7, the discharge port of the washing salt liquid circulation assembly 7 on the side close to the desorption zone 4 is located above the belt vacuum filter 100 and is connected with the inlet of the other washing salt liquid circulation assembly 7. corresponding to the mouth. With this structure, the salt concentration in the washing salt solution from the washing salt solution circulation assembly 7 close to the desorption zone 4 to the washing salt solution circulation assembly 7 far from the desorption zone 4 increases sequentially, so that incremental gradient elution is realized to improve the elution efficiency. efficient.
申请人发现，当洗盐液中的盐浓度越高时，被吸附剂吸附的锂盐越不容易解吸，当吸附剂中的盐锂比（普通盐与含锂盐的比）越高时，锂越不容易被洗脱。考虑到要同时满足洗脱盐及降低锂盐的洗脱，本发明创造性的提出梯度洗脱的结构。该梯度洗脱结构的原理是：洗盐液循环组件7的出料口出来的洗盐液的含盐量，由靠近解吸区4的方向向靠近原料卤水区2的方向逐渐增高，也即最靠近解吸区4的洗盐液为纯水，而最靠近原料卤水区2的洗盐液中包含有部分解吸的锂盐和其他洗脱下来的杂盐。这个优点在于，沿滤布102传动方向的洗盐液的含盐量呈梯度递减，盐分被逐步洗脱，洗脱过程中锂盐被同步洗脱的概率大大降低，从而防止锂盐被提前洗脱，也使其他杂盐得到更好的洗脱。The applicant found that when the salt concentration in the washing salt solution is higher, the lithium salt adsorbed by the adsorbent is less easily desorbed, and when the salt-lithium ratio (ratio of ordinary salt to lithium-containing salt) in the adsorbent is higher, Lithium is less easily eluted. Considering that the elution of the salt and the reduction of the elution of the lithium salt should be satisfied at the same time, the present invention creatively proposes a structure of gradient elution. The principle of the gradient elution structure is: the salt content of the washing salt solution from the discharge port of the washing salt solution circulation component 7 gradually increases from the direction close to the desorption zone 4 to the direction close to the raw brine zone 2, that is, the most The washing salt solution near the desorption zone 4 is pure water, and the washing salt solution closest to the raw brine zone 2 contains partially desorbed lithium salts and other eluted miscellaneous salts. This advantage is that the salt content of the washing salt solution along the transmission direction of the filter cloth 102 decreases gradually, the salt is gradually eluted, and the probability that the lithium salt is synchronously eluted during the elution process is greatly reduced, thereby preventing the lithium salt from being washed in advance. It also makes other miscellaneous salts get better elution.
本实施例，还提供了一种将最靠近原料卤水区2的洗盐液循环组件7的出料口出来的锂盐重新吸附回收的结构。也即，还包括连接解吸区4的洗盐回水区12，所述的第一液体输送机构5的出料口连接洗盐回水区12。具体的说，是最靠近原料卤水区2的洗盐液循环组件7的出料口连接洗盐回水区12。由于洗盐回水区12连接在在解吸区4后面，到达洗盐回水区12内的吸附剂内的锂盐已经被解吸，或者或吸附剂内的锂盐含量极低，洗盐液循环组件7的出料口的回水中含有的锂盐又可以再次被吸附剂吸附，从而避免锂盐浪费。This embodiment also provides a structure for re-adsorbing and recovering the lithium salt coming out of the discharge port of the salt washing liquid circulation component 7 closest to the raw brine zone 2 . That is, it also includes a salt water return area 12 connected to the desorption area 4 , and the discharge port of the first liquid conveying mechanism 5 is connected to the wash salt water return area 12 . Specifically, the discharge port of the washing salt liquid circulation component 7 closest to the raw brine zone 2 is connected to the washing salt return water zone 12 . Since the salt-washing backwater zone 12 is connected behind the desorption zone 4, the lithium salt in the adsorbent that reaches the salt-washing backwater zone 12 has been desorbed, or the lithium salt content in the adsorbent is extremely low, and the salt-washing liquid circulates The lithium salt contained in the return water of the outlet of the component 7 can be adsorbed by the adsorbent again, thereby avoiding the waste of lithium salt.
梯度洗盐的具体结构是这样的：洗盐液循环组件7包括连接带式真空过滤机100的洗盐液真空盒8，以及连接洗盐液真空盒8的洗盐液输送组件9，每相邻的两个洗盐液循环组件7中靠近解吸区4一侧的洗盐液循环组件7上的洗盐液输送组件9的出料口位于带式真空过滤机100上方并与另一个洗盐液循环组件7上的洗盐液真空盒8对应。The specific structure of the gradient washing salt is as follows: the washing salt solution circulation assembly 7 includes a washing salt solution vacuum box 8 connected to the belt vacuum filter 100, and a washing salt solution conveying component 9 connected to the washing salt solution vacuum box 8. Each phase The discharge port of the washing salt liquid conveying assembly 9 on the washing salt liquid circulation assembly 7 on the side close to the desorption zone 4 of the two adjacent washing salt liquid circulation assemblies 7 is located above the belt vacuum filter 100 and is connected with the other washing salt liquid. The washing salt liquid vacuum box 8 on the liquid circulation assembly 7 corresponds.
洗盐液循环组件7包括连接洗盐液真空盒8洗盐液收集罐7a，洗盐液收集罐7a连接真空泵和输送泵，通过输送泵来转移洗盐液，使洗盐液到达滤布102上方，对滤布上的吸附剂进行淋洗，通过真空泵产生真空，滤布102上的液体吸入到洗盐液收集罐7a中。最靠近原料卤水区2的洗盐液循环组件7的洗盐水用输送泵打到洗盐回水区12上方，对吸附剂进行淋洗。The washing salt liquid circulation assembly 7 includes a washing salt liquid collecting tank 7a connected to the washing salt liquid vacuum box 8, and the washing salt liquid collecting tank 7a is connected to a vacuum pump and a transfer pump, and the washing salt liquid is transferred through the transfer pump, so that the washing salt liquid reaches the filter cloth 102 Above, the adsorbent on the filter cloth is rinsed, a vacuum is generated by a vacuum pump, and the liquid on the filter cloth 102 is sucked into the washing salt liquid collection tank 7a. The washing salt water of the washing salt liquid circulation component 7 closest to the raw brine zone 2 is pumped to the top of the washing salt return water zone 12 by a transfer pump to rinse the adsorbent.
洗盐液真空盒8上方设有布水结构，布水结构可以是一根管，或者是多根管沿带式真空过滤机100轴向间隔排列，该布水结构连接洗盐液进水口，其中最靠近解吸区4的布水结构直接连接洗盐液输送器，最靠近原料卤水区2的洗盐液循环组件7不连接布水结构，其余的洗盐液循环组件7出口均连接一个布水结构。A water distribution structure is provided above the washing salt solution vacuum box 8, and the water distribution structure can be a tube, or a plurality of tubes are arranged at intervals along the axial direction of the belt vacuum filter 100, and the water distribution structure is connected to the washing salt solution water inlet, The water distribution structure closest to the desorption zone 4 is directly connected to the washing salt liquid conveyor, the washing salt liquid circulation component 7 closest to the raw brine zone 2 is not connected to the water distribution structure, and the outlets of the other washing salt liquid circulation components 7 are connected to a cloth water structure.
第二液体输送机构6包括至少两个相互独立且依次连接的解吸液循环组件10，不同的解吸液循环组件10由远离洗盐区3的一侧向另一侧逐个连接。The second liquid conveying mechanism 6 includes at least two desorption liquid circulation assemblies 10 which are independent of each other and are connected in sequence. Different desorption liquid circulation assemblies 10 are connected one by one from one side away from the salt washing area 3 to the other side.
可以理解为，解吸液循环组件10的结构可以与洗盐液循环组件7的结构是一样的，其功能就是输送液体，通过液体对滤布102上的吸附剂进行淋洗，将吸附剂中的锂盐洗脱。It can be understood that the structure of the desorbing liquid circulation assembly 10 can be the same as that of the washing salt liquid circulation assembly 7, and its function is to transport liquid, wash the adsorbent on the filter cloth 102 through the liquid, and remove the adsorbent in the adsorbent. Lithium salt eluted.
在本实施例中，解吸液循环组件10也是相互串联的结构，起到梯度洗脱的效果。最靠近洗盐区3的解吸液循环组件10的出料口连接后续精加工工段，该精加工工段为后续工段，如过滤、浓缩等，但精加工工段为现有技术，不属于本发明的结构，也不是本发明所要解决的技术问题。In this embodiment, the desorption liquid circulation assemblies 10 are also connected in series with each other, so as to achieve the effect of gradient elution. The discharge port of the desorbing liquid circulation assembly 10 closest to the salt washing zone 3 is connected to the subsequent finishing section, which is the subsequent section, such as filtration, concentration, etc., but the finishing section is the prior art and does not belong to the present invention. The structure is not the technical problem to be solved by the present invention.
最远离洗盐区3的解吸液循环组件10的进料口连接位于带式真空过滤机100上方的解吸液输送器，解吸液输送器可以为输送泵，直接输送纯水，每相邻的两个解吸液循环组件10中远离洗盐区3一侧的解吸液循环组件10的出料口位于带式真空过滤机100上方并与另一个解吸液循环组件10的进料口对应。The feed port of the desorption liquid circulation assembly 10 farthest from the salt washing zone 3 is connected to the desorption liquid conveyor located above the belt vacuum filter 100. The desorption liquid conveyor can be a transfer pump, which directly transports pure water. The discharge port of the desorption liquid circulation assembly 10 on the side away from the salt washing zone 3 of the desorption liquid circulation assembly 10 is located above the belt vacuum filter 100 and corresponds to the feed port of the other desorption liquid circulation assembly 10 .
沿着真空过滤机100的滤布102的传输方向，解吸液中的锂含量逐渐降低，最后为纯水对吸附剂进行解吸，使吸附剂中的锂能够被充分洗脱。Along the transmission direction of the filter cloth 102 of the vacuum filter 100, the lithium content in the desorption solution gradually decreases, and finally the adsorbent is desorbed by pure water, so that the lithium in the adsorbent can be fully eluted.
解吸液循环组件10包括连接带式真空过滤机100的解吸液真空盒11，以及连接解吸液真空盒11的解吸液输送组件11a，每相邻的两个解吸液循环组件10中远离洗盐区3一侧的解吸液循环组件10上的解吸液输送组件位于带式真空过滤机100上方并与另一个解吸液循环组件10上的解吸液真空盒11对应。解吸液输送组件11a包括连接解吸液真空盒11的收集罐和输送泵，其中一个解吸液循环组件10的输送泵与管道连接的出口与相邻的另一个解吸液循环组件10上的解吸液真空盒11对应。The desorption liquid circulation assembly 10 includes a desorption liquid vacuum box 11 connected to the belt vacuum filter 100, and a desorption liquid conveying assembly 11a connected to the desorption liquid vacuum box 11. Each adjacent two desorption liquid circulation assemblies 10 are far away from the salt washing area. 3. The desorption liquid conveying assembly on the desorption liquid circulation assembly 10 on one side is located above the belt vacuum filter 100 and corresponds to the desorption liquid vacuum box 11 on the other desorption liquid circulation assembly 10. The desorption liquid conveying assembly 11a includes a collection tank and a conveying pump connected to the desorption liquid vacuum box 11, wherein the outlet of the conveying pump of one desorption liquid circulation assembly 10 is connected to the pipeline and the desorption liquid vacuum on the adjacent other desorption liquid circulation assembly 10. Box 11 corresponds.
同样的，每个解吸液真空盒11上方也设有一个布水结构，布水结构可以直接是管道上设置若干开口，或者是喷洒头等，该布水结构将解吸液形成喷淋状，对滤布102上的吸附剂进行喷淋，从而将锂盐从吸附剂中洗出。这种洗脱方式，存在一个极大的优点：由于带式真空过滤机100滤布102上的吸附剂中的锂含量是越往后传输，含量越少，越不容易被解吸，而本实施例的解吸液循环组件10呈串联结构后，解吸液中的锂含量随滤布102的传输方向也是越往后越小，也即随着滤布102的传输方向，不同的解吸液循环组件10出来的解吸液中的锂含量与滤布102上的吸附剂中的锂含量呈现一个正相关的关系，到最后就是用纯水作为解吸液直接对锂含量最少的吸附剂进行解吸洗脱，达到洗脱完全的效果。Similarly, a water distribution structure is also provided above each desorption liquid vacuum box 11. The water distribution structure can be directly provided with a number of openings on the pipeline, or a spray head, etc. The adsorbent on the cloth 102 is sprayed to wash out the lithium salt from the adsorbent. This elution method has a great advantage: since the lithium content in the adsorbent on the filter cloth 102 of the belt vacuum filter 100 is transported further back, the less the content is, the less likely it is to be desorbed. After the desorption liquid circulation assembly 10 of the example is in a series structure, the lithium content in the desorption liquid decreases with the transmission direction of the filter cloth 102 going backward, that is, with the transmission direction of the filter cloth 102, different desorption liquid circulation assemblies 10 The lithium content in the desorbed liquid and the lithium content in the adsorbent on the filter cloth 102 have a positive correlation. In the end, pure water is used as the desorption liquid to directly desorb and elute the adsorbent with the least lithium content to achieve Elute complete effect.
需要说明的是，最靠近原料卤水区2的洗盐液循环组件7的洗盐水可以直接打到盐田。但这样处理会降低盐田中的卤水的含盐率，且洗盐水中也含有一定的锂，直接排入盐田造成锂吸附不完全，影响锂的提取率。因此，作为一种优选的方案，本实施例在解吸区4后面设置了一个洗盐回水区12，最靠近原料卤水区2的洗盐液循环组件7的出料口连接洗盐回水区12，洗盐液循环组件7出水对洗盐回水区12上的吸附剂进行淋洗。It should be noted that the washing salt water of the washing salt liquid circulation component 7 closest to the raw brine area 2 can be directly sent to the salt field. However, this treatment will reduce the salt content of the brine in the salt field, and the washing brine also contains a certain amount of lithium. Direct discharge into the salt field results in incomplete lithium adsorption and affects the extraction rate of lithium. Therefore, as a preferred solution, in this embodiment, a washing salt return water zone 12 is set behind the desorption zone 4, and the discharge port of the washing salt liquid circulation component 7 closest to the raw brine zone 2 is connected to the washing salt return water zone. 12. The effluent from the washing salt liquid circulation component 7 rinses the adsorbent on the washing salt return water area 12.
洗盐回水区12通过输送带13连接固液混合机构1。具体的说，在机架101上与滤布102尾部对应的位置设有一块刮板103，刮板103将滤布102上的吸附剂刮下后，掉落到输送带13上，输送带13连接混合罐1a，吸附剂重新回到混合罐1a中，与卤水混合，将卤水中的锂盐吸附，吸附剂完成吸附-解吸-重新吸附的循环。The brine backwater area 12 is connected to the solid-liquid mixing mechanism 1 through a conveyor belt 13 . Specifically, a scraper 103 is provided on the frame 101 at a position corresponding to the tail of the filter cloth 102. The scraper 103 scrapes off the adsorbent on the filter cloth 102 and then drops it onto the conveyor belt 13. The mixing tank 1a is connected, the adsorbent is returned to the mixing tank 1a, mixed with the brine, and the lithium salt in the brine is adsorbed, and the adsorbent completes the cycle of adsorption-desorption-re-adsorption.
洗盐回水区12包括连接带式真空过滤机100的洗盐回水真空盒14，洗盐回水真空盒14通过洗盐回水输送组件15连接洗盐回收固液分离器16，原料卤水区2通过原料卤水输送组件17连接原料卤水固液分离器18。The washing salt return water area 12 includes a washing salt return water vacuum box 14 connected to the belt vacuum filter 100, and the washing salt return water vacuum box 14 is connected to the washing salt recovery solid-liquid separator 16 through the washing salt return water conveying assembly 15, and the raw material brine Zone 2 is connected to the raw material brine solid-liquid separator 18 through the raw material brine conveying assembly 17 .
在本实施例中，固液分离器16为布袋式过滤器、紧密过滤器、磁选机、三足离心机、碟片式分离机中的一种或几种。当吸附剂为磁性吸附剂时，可选用磁选机，当吸附剂为非磁性吸附剂时，则选用除磁选机以外的其他固液分离设备。In this embodiment, the solid-liquid separator 16 is one or more of a bag filter, a compact filter, a magnetic separator, a three-legged 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 other than the magnetic separator is selected.
工业实用性Industrial Applicability
本发明的工作过程是：The working process of the present invention is:
吸附剂投入到混合罐1a中，盐田的卤水用泵送到混合罐中，固液比为1:10-200，具体根据式真空过滤机100的选型及卤水的含盐量设定，搅拌状态下，卤水中的盐被吸附剂吸附。The adsorbent is put into the mixing tank 1a, the brine in the salt field is pumped into the mixing tank, and the solid-liquid ratio is 1:10-200. In the state, the salt in the brine is adsorbed by the adsorbent.
吸附剂和卤水的混合物，从混合罐中，投入到原料卤水区2，在带式真空过滤机100的真空作用下，卤水透过滤布102，吸附剂隔离在滤布102上，随着滤布102的传动，吸附剂到达洗盐区3，洗盐液在洗盐区3上方对滤布上的吸附剂进行淋洗，将吸附剂中的杂盐洗脱，经过洗脱处理后的洗盐液回到洗盐回水区12，对洗盐回水区12内的吸附剂进行淋洗，使吸附剂吸附洗盐液中透滤的吸附剂以及锂盐。The mixture of adsorbent and brine is put into the raw brine area 2 from the mixing tank. Under the vacuum action of the belt vacuum filter 100, the brine penetrates the filter cloth 102, and the adsorbent is isolated on the filter cloth 102. 102 drive, the adsorbent reaches the salt washing zone 3, and the washing salt solution washes the adsorbent on the filter cloth above the salt washing zone 3, eluting the miscellaneous salts in the adsorbent, and the washing salt after the elution treatment The liquid is returned to the salt-washing backwater area 12, and the adsorbent in the salt-washing backwater area 12 is rinsed, so that the adsorbent adsorbs the adsorbent and the lithium salt that have been diafiltered in the salt-washing liquid.
经过洗盐区3的吸附剂进入到解吸区4后，通过解吸液的淋洗后，吸附剂中的锂盐被吸出，通过解吸液循环组件10收集后，得到含有锂盐的液体，可以进入到下道工序进行处理。After the adsorbent passed through the salt washing zone 3 enters the desorption zone 4, the lithium salt in the adsorbent is sucked out after being rinsed by the desorption liquid, and is collected by the desorption liquid circulation component 10 to obtain a liquid containing lithium salt, which can enter to the next process for processing.
申请人经过大量实验发现，对于不同的卤水分离，滤布通气量最小应不低于500 L/m2·s才能满足较理想的带式真空过滤机处理能力，不同使用情况的吸附剂泄漏量存在一定差异，但一般小于10%。此时穿过带式真空过滤机滤布的卤水、洗盐液、解吸液中吸附剂的含量一般低于1%。After a lot of experiments, the applicant found that for different brine separation, the minimum ventilation volume of the filter cloth should not be less than 500 L/m2·s to meet the ideal processing capacity of the belt vacuum filter. A certain difference, but generally less than 10%. At this time, the content of the adsorbent in the brine, washing salt solution and desorption solution passing through the filter cloth of the belt vacuum filter is generally less than 1%.
上述固含低于1%的卤水、洗盐液、解吸液经磁选机、精密过滤设备或陶瓷膜二次处理进行固液分离后，向盐田排放或进入后***处理。若吸附剂中含有磁性物，则可用磁选机进行回收，若吸附剂中不含磁性物，则可用精密过滤设备或陶瓷膜进行回收。The above-mentioned brine, washing salt solution and desorption solution with a solid content of less than 1% are subjected to solid-liquid separation after secondary treatment by magnetic separator, precision filtration equipment or ceramic membrane, and then discharged to the salt field or entered into the post-system for treatment. If the adsorbent contains magnetic substances, it can be recovered by a magnetic separator. If the adsorbent does not contain magnetic substances, it can be recovered by precision filtration equipment or ceramic membranes.
从带式真空过滤机穿滤的吸附剂经磁选机、精密过滤设备和陶瓷膜二次捕集后，反冲回到带式真空过滤机对应的给水口，进而回到吸附解吸主体循环。带滤机对吸附剂的捕集率大于90%，后段固液分离设备对吸附剂的捕集率大于99.9%，因此吸附剂在单次吸附解吸循环中的泄漏率小于0.01%。The adsorbent filtered from the belt vacuum filter is collected by the magnetic separator, precision filtration equipment and ceramic membrane for the second time, and then recoiled back to the corresponding water supply port of the belt vacuum filter, and then returned to the main circulation of adsorption and desorption. The capture rate of the adsorbent by the belt filter is greater than 90%, and the capture rate of the adsorbent by the back-end solid-liquid separation equipment is greater than 99.9%, so the leakage rate of the adsorbent in a single adsorption and desorption cycle is less than 0.01%.
本发明提出的带式真空过滤机，可实现吸附剂小水量快速洗涤、吸附剂解吸再生和洗盐流失锂的回收。利用本发明可以得到镁锂比小于1:1，盐锂比（TDS/Li）小于10:1的解吸液，大幅降低了后续除盐提纯工艺的投资和生产成本，最终可以稳定得到电池级碳酸锂或氢氧化锂。本发明提出的新设备可以回收盐分洗涤过程流失的锂离子，进而使卤水吸附解吸过程达到80%以上的锂离子回收率。The belt vacuum filter proposed by the invention can realize the rapid washing of the adsorbent with a small amount of water, the desorption and regeneration of the adsorbent and the recovery of lithium lost by washing salt. The invention can obtain a desorption solution with a magnesium-lithium ratio of less than 1:1 and a salt-to-lithium ratio (TDS/Li) of less than 10:1, which greatly reduces the investment and production cost of the subsequent desalination and purification process, and finally can stably obtain battery-grade carbonic acid. Lithium or Lithium Hydroxide. The new equipment proposed by the invention can recover the lithium ions lost in the salt washing process, and then make the brine adsorption and desorption process reach a lithium ion recovery rate of more than 80%.
本文中所描述的具体实施例仅仅是对本发明精神作举例说明。本发明所属技术领域的技术人员可以对所描述的具体实施例做各种各样的修改或补充或采用类似的方式替代，但并不会偏离本发明的精神。The specific embodiments described herein are merely illustrative of the spirit of the invention. Those skilled in the art to which the present invention pertains can make various modifications or additions to the described specific embodiments or substitute in similar manners, but will not deviate from the spirit of the present invention.

Claims (10)

  1. 一种用于吸附法卤水提锂的设备，包括带式真空过滤机（100），其特征在于，所述的带式真空过滤机（100）连接有用于将卤水和吸附剂混合的固液混合机构（1），带式真空过滤机（100）上并沿着带式真空过滤机（100）的传动方向依次设有相互连接的原料卤水区（2）、洗盐区（3）和解吸区（4），固液混合机构（1）连接原料卤水区（2），输送洗盐液的第一液体输送机构（5）和输送解吸液的第二液体输送机构（6）分别连接洗盐区（3）和解吸区（4）。A device for extracting lithium from brine by adsorption method, comprising a belt vacuum filter (100), characterized in that the belt vacuum filter (100) is connected with a solid-liquid mixing device for mixing brine and adsorbent Mechanism (1), on the belt vacuum filter (100) and along the transmission direction of the belt vacuum filter (100), there are sequentially connected raw material brine area (2), salt washing area (3) and desorption area. (4), the solid-liquid mixing mechanism (1) is connected to the raw material brine area (2), the first liquid conveying mechanism (5) for conveying the washing salt solution and the second liquid conveying mechanism (6) for conveying the desorption liquid are respectively connected to the washing salt area (3) and desorption zone (4).
  2. 根据权利要求1所述的用于吸附法卤水提锂的设备，其特征在于，所述的第一液体输送机构（5）包括至少两个相互独立且依次连接的洗盐液循环组件（7），不同的洗盐液循环组件（7）由靠近解吸区（4）的一侧向另一侧逐个连接。The apparatus for extracting lithium from brine by adsorption method according to claim 1, characterized in that, the first liquid conveying mechanism (5) comprises at least two washing salt liquid circulation components (7) which are independent of each other and are connected in sequence , the different washing salt solution circulation components (7) are connected one by one from one side close to the desorption zone (4) to the other side.
  3. 根据权利要求2所述的用于吸附法卤水提锂的设备，其特征在于，最靠近原料卤水区（2）的洗盐液循环组件（7）的出料口连接带式真空过滤机（100）尾部，最靠近解吸区（4）的洗盐液循环组件（7）上方设有洗盐液输送器，每相邻的两个洗盐液循环组件（7）中靠近解吸区（4）一侧的洗盐液循环组件（7）的出料口位于带式真空过滤机（100）上方并与另一个洗盐液循环组件（7）的进料口对应。The equipment for extracting lithium from brine by adsorption method according to claim 2, characterized in that the discharge port of the washing salt liquid circulation component (7) closest to the raw brine area (2) is connected to a belt vacuum filter (100). ) at the tail of the washing salt solution circulation component (7) closest to the desorption zone (4) is provided with a washing salt solution conveyor, and each adjacent two washing salt solution circulation components (7) are close to the desorption zone (4). The discharge port of the side washing salt liquid circulation assembly (7) is located above the belt vacuum filter (100) and corresponds to the feed port of the other washing salt liquid circulation assembly (7).
  4. 根据权利要求3所述的用于吸附法卤水提锂的设备，其特征在于，所述的洗盐液循环组件（7）包括连接带式真空过滤机（100）的洗盐液真空盒（8），以及连接洗盐液真空盒（8）的洗盐液输送组件（9），每相邻的两个洗盐液循环组件（7）中靠近解吸区（4）一侧的洗盐液循环组件（7）上的洗盐液输送组件（9）的出料口位于带式真空过滤机（100）上方并与另一个洗盐液循环组件（7）上的洗盐液真空盒（8）对应。The apparatus for extracting lithium from brine by adsorption method according to claim 3, characterized in that, the washing salt solution circulation assembly (7) comprises a washing salt solution vacuum box (8) connected to a belt vacuum filter (100). ), and the washing salt solution conveying assembly (9) connected to the washing salt solution vacuum box (8); The discharge port of the salt washing liquid conveying assembly (9) on the assembly (7) is located above the belt vacuum filter (100) and is connected with the washing salt liquid vacuum box (8) on the other washing salt liquid circulation assembly (7). correspond.
  5. 根据权利要求1所述的用于吸附法卤水提锂的设备，其特征在于，所述的第二液体输送机构（6）包括至少两个相互独立且依次连接的解吸液循环组件（10），不同的解吸液循环组件（10）由远离洗盐区（3）的一侧向另一侧逐个连接。The device for extracting lithium from brine by adsorption method according to claim 1, characterized in that, the second liquid conveying mechanism (6) comprises at least two desorption liquid circulation components (10) which are independent of each other and are connected in sequence, Different desorbing liquid circulation assemblies (10) are connected one by one from one side away from the salt washing area (3) to the other side.
  6. 根据权利要求5所述的用于吸附法卤水提锂的设备，其特征在于，最靠近洗盐区（3）的解吸液循环组件（10）的出料口连接后续精加工工段，最远离洗盐区（3）的解吸液循环组件（10）的进料口连接位于带式真空过滤机（100）上方的解吸液输送器，每相邻的两个解吸液循环组件（10）中远离洗盐区（3）一侧的解吸液循环组件（10））的出料口位于带式真空过滤机（100）上方并与另一个解吸液循环组件（10）的进料口对应。The equipment for extracting lithium from brine by adsorption method according to claim 5, characterized in that the discharge port of the desorbing liquid circulation component (10) closest to the salt washing area (3) is connected to the subsequent finishing section, and is farthest from the washing area. The feed port of the desorption liquid circulation assembly (10) in the salt zone (3) is connected to the desorption liquid conveyor located above the belt vacuum filter (100), and each adjacent two desorption liquid circulation assemblies (10) are far away from the washing machine. The discharge port of the desorption liquid circulation assembly (10) on one side of the salt zone (3) is located above the belt vacuum filter (100) and corresponds to the feed port of the other desorption liquid circulation assembly (10).
  7. 根据权利要求6所述的用于吸附法卤水提锂的设备，其特征在于，所述的解吸液循环组件（10）包括连接带式真空过滤机（100）的解吸液真空盒（11），以及连接解吸液真空盒（11）的解吸液输送组件（11a），每相邻的两个解吸液循环组件（10）中远离洗盐区（3）一侧的解吸液循环组件（10）上的解吸液输送组件（11a）位于带式真空过滤机（100）上方并与另一个解吸液循环组件（10）上的解吸液真空盒（11）对应。The device for extracting lithium from brine by adsorption method according to claim 6, characterized in that the desorption liquid circulation assembly (10) comprises a desorption liquid vacuum box (11) connected to a belt vacuum filter (100), and the desorbing fluid conveying component (11a) connected to the desorbing fluid vacuum box (11), on the desorbing fluid circulating component (10) on the side away from the salt washing area (3) in each of the two adjacent desorbing fluid circulating components (10). The desorption liquid conveying assembly (11a) is located above the belt vacuum filter (100) and corresponds to the desorption liquid vacuum box (11) on the other desorption liquid circulation assembly (10).
  8. 根据权利要求1所述的用于吸附法卤水提锂的设备，其特征在于，还包括连接解吸区（4）的洗盐回水区（12），所述的第一液体输送机构（5）的出料口连接洗盐回水区（12）。The apparatus for extracting lithium from brine by adsorption method according to claim 1, characterized in that it further comprises a washing salt return water area (12) connected to the desorption area (4), and the first liquid conveying mechanism (5) The discharge port is connected to the washing salt backwater area (12).
  9. 根据权利要求2所述的用于吸附法卤水提锂的设备，其特征在于，还包括连接解吸区（4）的洗盐回水区（12），最靠近原料卤水区（2）的洗盐液循环组件（7）的出料口连接洗盐回水区（12），洗盐回水区（12）通过输送带（13）连接固液混合机构（1）。The device for extracting lithium from brine by adsorption method according to claim 2, characterized in that it further comprises a salt washing backwater zone (12) connected to the desorption zone (4), and a washing salt return zone (12) closest to the raw brine zone (2) The discharge port of the liquid circulation component (7) is connected to the salt-washing backwater area (12), and the salt-washing backwater area (12) is connected to the solid-liquid mixing mechanism (1) through a conveyor belt (13).
  10. 根据权利要求8或9所述的用于吸附法卤水提锂的设备，其特征在于，所述的洗盐回水区（12）包括连接带式真空过滤机（100）的洗盐回水真空盒（14），洗盐回水真空盒（14）通过洗盐回水输送组件（15）连接洗盐回收固液分离器（16），原料卤水区（2）通过原料卤水输送组件（17）连接原料卤水固液分离器（18）。The equipment for extracting lithium from brine by adsorption method according to claim 8 or 9, characterized in that, the washing salt return water area (12) comprises a washing salt return water vacuum connected to a belt vacuum filter (100). The box (14), the washing salt return water vacuum box (14) is connected to the washing salt recovery solid-liquid separator (16) through the washing salt return water conveying assembly (15), and the raw brine area (2) passes through the raw brine conveying assembly (17) Connect the raw material brine solid-liquid separator (18).
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