CN115849411A - Continuous production process of lithium hydroxide - Google Patents
Continuous production process of lithium hydroxide Download PDFInfo
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- CN115849411A CN115849411A CN202211515771.5A CN202211515771A CN115849411A CN 115849411 A CN115849411 A CN 115849411A CN 202211515771 A CN202211515771 A CN 202211515771A CN 115849411 A CN115849411 A CN 115849411A
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- WMFOQBRAJBCJND-UHFFFAOYSA-M Lithium hydroxide Chemical compound [Li+].[OH-] WMFOQBRAJBCJND-UHFFFAOYSA-M 0.000 title claims abstract description 230
- 238000000034 method Methods 0.000 title claims abstract description 32
- 238000010924 continuous production Methods 0.000 title claims abstract description 12
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 57
- 239000007788 liquid Substances 0.000 claims abstract description 33
- INHCSSUBVCNVSK-UHFFFAOYSA-L lithium sulfate Inorganic materials [Li+].[Li+].[O-]S([O-])(=O)=O INHCSSUBVCNVSK-UHFFFAOYSA-L 0.000 claims abstract description 29
- RBTVSNLYYIMMKS-UHFFFAOYSA-N tert-butyl 3-aminoazetidine-1-carboxylate;hydrochloride Chemical compound Cl.CC(C)(C)OC(=O)N1CC(N)C1 RBTVSNLYYIMMKS-UHFFFAOYSA-N 0.000 claims abstract description 29
- 239000000047 product Substances 0.000 claims abstract description 28
- 238000001914 filtration Methods 0.000 claims abstract description 17
- 238000005406 washing Methods 0.000 claims abstract description 17
- 238000001704 evaporation Methods 0.000 claims abstract description 11
- 230000008014 freezing Effects 0.000 claims abstract description 11
- 238000007710 freezing Methods 0.000 claims abstract description 11
- 238000009993 causticizing Methods 0.000 claims abstract description 10
- PQVSTLUFSYVLTO-UHFFFAOYSA-N ethyl n-ethoxycarbonylcarbamate Chemical compound CCOC(=O)NC(=O)OCC PQVSTLUFSYVLTO-UHFFFAOYSA-N 0.000 claims abstract description 10
- GLXDVVHUTZTUQK-UHFFFAOYSA-M lithium hydroxide monohydrate Substances [Li+].O.[OH-] GLXDVVHUTZTUQK-UHFFFAOYSA-M 0.000 claims abstract description 10
- 229940040692 lithium hydroxide monohydrate Drugs 0.000 claims abstract description 10
- 239000013078 crystal Substances 0.000 claims abstract description 9
- 238000001035 drying Methods 0.000 claims abstract description 9
- 239000000706 filtrate Substances 0.000 claims abstract description 8
- 239000002002 slurry Substances 0.000 claims abstract description 8
- 239000012530 fluid Substances 0.000 claims abstract description 7
- 238000010438 heat treatment Methods 0.000 claims abstract description 6
- 150000001450 anions Chemical class 0.000 claims abstract description 3
- 150000001768 cations Chemical class 0.000 claims abstract description 3
- 239000000243 solution Substances 0.000 claims description 46
- 238000007599 discharging Methods 0.000 claims description 13
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 12
- 239000002893 slag Substances 0.000 claims description 12
- 239000007787 solid Substances 0.000 claims description 12
- 239000012535 impurity Substances 0.000 claims description 11
- 239000000463 material Substances 0.000 claims description 11
- 238000005341 cation exchange Methods 0.000 claims description 10
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 9
- RSIJVJUOQBWMIM-UHFFFAOYSA-L sodium sulfate decahydrate Chemical compound O.O.O.O.O.O.O.O.O.O.[Na+].[Na+].[O-]S([O-])(=O)=O RSIJVJUOQBWMIM-UHFFFAOYSA-L 0.000 claims description 9
- 238000005349 anion exchange Methods 0.000 claims description 8
- XGZVUEUWXADBQD-UHFFFAOYSA-L lithium carbonate Chemical compound [Li+].[Li+].[O-]C([O-])=O XGZVUEUWXADBQD-UHFFFAOYSA-L 0.000 claims description 7
- 229910052808 lithium carbonate Inorganic materials 0.000 claims description 7
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 claims description 6
- 230000008020 evaporation Effects 0.000 claims description 6
- 229910052744 lithium Inorganic materials 0.000 claims description 6
- 229910052938 sodium sulfate Inorganic materials 0.000 claims description 5
- 235000011152 sodium sulphate Nutrition 0.000 claims description 5
- 239000003957 anion exchange resin Substances 0.000 claims description 4
- 150000003440 styrenes Chemical class 0.000 claims description 4
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims description 3
- 229920001429 chelating resin Polymers 0.000 claims description 3
- 239000012141 concentrate Substances 0.000 claims description 3
- 238000002425 crystallisation Methods 0.000 claims description 3
- 230000008025 crystallization Effects 0.000 claims description 3
- 239000011259 mixed solution Substances 0.000 claims description 3
- 238000000746 purification Methods 0.000 claims description 3
- 230000035484 reaction time Effects 0.000 claims description 3
- 239000002253 acid Substances 0.000 claims description 2
- 239000003463 adsorbent Substances 0.000 claims description 2
- 238000013019 agitation Methods 0.000 claims description 2
- CNLWCVNCHLKFHK-UHFFFAOYSA-N aluminum;lithium;dioxido(oxo)silane Chemical compound [Li+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O CNLWCVNCHLKFHK-UHFFFAOYSA-N 0.000 claims description 2
- 239000006227 byproduct Substances 0.000 claims description 2
- 239000003729 cation exchange resin Substances 0.000 claims description 2
- 150000002500 ions Chemical class 0.000 claims description 2
- 238000002386 leaching Methods 0.000 claims description 2
- 229910052751 metal Inorganic materials 0.000 claims description 2
- 239000002184 metal Substances 0.000 claims description 2
- 239000010413 mother solution Substances 0.000 claims description 2
- 238000011084 recovery Methods 0.000 claims description 2
- 229910052642 spodumene Inorganic materials 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 abstract description 16
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000005086 pumping Methods 0.000 description 18
- 239000012047 saturated solution Substances 0.000 description 5
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- 238000005342 ion exchange Methods 0.000 description 3
- TZCXTZWJZNENPQ-UHFFFAOYSA-L barium sulfate Chemical compound [Ba+2].[O-]S([O-])(=O)=O TZCXTZWJZNENPQ-UHFFFAOYSA-L 0.000 description 2
- 229910000019 calcium carbonate Inorganic materials 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000001953 recrystallisation Methods 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 229960003010 sodium sulfate Drugs 0.000 description 2
- 229940056729 sodium sulfate anhydrous Drugs 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- WDIHJSXYQDMJHN-UHFFFAOYSA-L barium chloride Chemical compound [Cl-].[Cl-].[Ba+2] WDIHJSXYQDMJHN-UHFFFAOYSA-L 0.000 description 1
- 229910001626 barium chloride Inorganic materials 0.000 description 1
- RQPZNWPYLFFXCP-UHFFFAOYSA-L barium dihydroxide Chemical compound [OH-].[OH-].[Ba+2] RQPZNWPYLFFXCP-UHFFFAOYSA-L 0.000 description 1
- 229910001863 barium hydroxide Inorganic materials 0.000 description 1
- 229910001422 barium ion Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- -1 chlorine ions Chemical class 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
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Abstract
The invention discloses a continuous production process of lithium hydroxide, which comprises the following steps: 1) Inputting the lithium sulfate purified solution and the sodium hydroxide purified solution into a pipeline reactor for carrying out causticizing reaction, and outputting causticized solution; 2) Filtering the causticized liquid to obtain causticized filtrate; 3) Freezing the causticized liquid and separating out lithium hydroxide refrigerating liquid; 4) Heating the lithium hydroxide refrigerating fluid, and then exchanging cations and anions to obtain a lithium hydroxide refined solution; 5) Evaporating and crystallizing the lithium hydroxide refined solution to obtain lithium hydroxide crystal slurry, and separating and washing the crystal slurry to obtain a lithium hydroxide wet product; 6) And drying the lithium hydroxide wet product to obtain a lithium hydroxide monohydrate product. The invention realizes the continuity and automation of the whole process of the lithium hydroxide production, shortens the process flow, reduces the labor intensity, the energy consumption and the production cost, obviously improves the production efficiency, and obtains the product with high purity and good quality.
Description
Technical Field
The invention relates to a lithium hydroxide production process.
Background
In recent years, with the rapid development of new energy, new materials, electronics, aerospace and other fields, the demand for lithium products such as lithium hydroxide and lithium carbonate is increasing. The current methods for preparing lithium hydroxide mainly comprise a lithium sulfate causticization method and a lithium carbonate causticization method (CN 111235591A). The causticizing method of lithium sulfate is to remove impurities from lithium sulfate solution extracted from lithium ore or salt lake and then to stir the lithium sulfate solution and sodium hydroxide in a kettle for reaction, discharge and freeze to separate out sodium sulfate decahydrate after the causticizing reaction is finished, separate the lithium hydroxide solution from sodium sulfate crystals, concentrate, crystallize and separate the separated lithium hydroxide solution to obtain crude lithium hydroxide, dissolve the crude lithium hydroxide monohydrate and then add barium hydroxide or barium chloride, form insoluble barium sulfate after stirring reaction, filter and remove sulfate radicals, and the filtrate is subject to re-evaporation, re-crystallization, separation and drying to obtain lithium hydroxide monohydrate (CN 106629787B); the difference from the causticizing method of lithium sulfate is that the causticizing method of lithium carbonate is to prepare lithium sulfate into lithium carbonate or directly carry out causticizing reaction on industrial grade lithium carbonate and calcium hydroxide to generate calcium carbonate and lithium hydroxide, and then the lithium hydroxide and the calcium carbonate are separated and then subjected to a series of steps of impurity removal, evaporation, crystallization, separation, drying and the like to obtain the lithium hydroxide monohydrate (CN 108821313A, CN 106673022B). The existing method for preparing lithium hydroxide has the obvious defects of complex steps, long process route, large equipment investment, high evaporation energy consumption and low yield, namely intermittent production, so that the production efficiency is low and the production cost is high.
Therefore, development of a continuous production process of lithium hydroxide is urgently needed to improve production efficiency, reduce production cost and realize production automation.
Disclosure of Invention
In order to overcome the defects of the existing lithium hydroxide production process, the invention aims to provide a lithium hydroxide continuous production process with simple process, short flow and high efficiency.
The technical solution of the invention is as follows:
a continuous production process of lithium hydroxide is characterized by comprising the following steps:
1) Continuously inputting the lithium sulfate purified solution and the sodium hydroxide purified solution into a pipeline reactor for carrying out causticizing reaction, and continuously outputting a lithium hydroxide and sodium sulfate mixed solution, namely causticized solution, from the pipeline reactor;
2) Filtering the causticized liquid to obtain causticized filtrate;
3) Freezing the causticized liquid and separating sodium sulfate decahydrate from the lithium hydroxide frozen liquid;
4) Heating the lithium hydroxide refrigerating fluid, and then exchanging cations and anions to obtain a lithium hydroxide refined solution;
5) Evaporating and crystallizing the lithium hydroxide refined solution to obtain lithium hydroxide crystal slurry, and separating and washing the lithium hydroxide crystal slurry to obtain a lithium hydroxide wet product;
6) And drying the lithium hydroxide wet product to obtain a lithium hydroxide monohydrate product.
The continuous production process of the lithium hydroxide comprises the following specific steps:
1) Inputting lithium sulfate purifying liquid axially from an inlet of the pipeline reactor, inputting sodium hydroxide purifying liquid radially from an inlet on the side surface of the pipeline reactor, and outputting causticized liquid from an axial outlet of the reactor. The amount of the reaction material input into the pipeline reactor is controlled according to the molar ratio of the sodium hydroxide to the lithium sulfate of 2.2-2.4, and the causticization reaction temperature is 10-50 ℃, preferably 15-30 ℃. The flow velocity of the reaction materials in the pipeline reactor is 0.15-1.8 m/min, preferably 0.6-1.2 m/min, and the reaction time of the reaction materials in the pipeline reactor is 15-40 min, preferably 20-30 min;
2) Inputting the causticized liquid output from the outlet of the reactor into a precision filter or a filter press, filtering and washing to obtain causticized filtrate and causticized slag, collecting the causticized slag, and performing additional agitation washing and recovery;
3) The causticized filtrate is input into a freezing and crystallizing system for freezing and crystallizing, and the discharge temperature is controlled between-10 ℃ and 0 ℃, preferably between-7 ℃ and-5 ℃. Discharging, separating sodium sulfate decahydrate from lithium hydroxide refrigerating fluid by a liquid-solid separator, and producing a byproduct anhydrous sodium sulphate by the separated sodium sulfate decahydrate;
4) Inputting lithium hydroxide refrigerating fluid into a heat exchanger to raise the temperature to 5-40 ℃, then flowing through a cation exchange column and an anion exchange column to remove impurities such as residual metal impurity ions, sulfate radicals and the like to obtain lithium hydroxide refined solution, wherein the cation exchange resin is macroporous strong acid type styrene series chelating resin, and the anion exchange resin is strong base type styrene series anion exchange resin;
5) Inputting the lithium hydroxide refined solution into an evaporator for evaporation and crystallization, discharging lithium hydroxide crystal slurry to a liquid-solid separator when the solid content of the concentrated solution reaches 10-15%, separating and washing to obtain a lithium hydroxide wet product, and returning the mother solution to the cation exchange column in the step 4);
6) And (4) inputting the lithium hydroxide wet product into a vacuum drier for drying, and discharging to obtain a lithium hydroxide product.
The lithium sulfate purification solution in the step 1) is a purified and impurity-removed lithium sulfate solution, and the lithium sulfate solution is any one or a mixed solution of any more of a lithium sulfate solution obtained by leaching spodumene concentrate with sulfuric acid, a lithium sulfate solution obtained by dissolving lithium carbonate with sulfuric acid, and a lithium sulfate solution obtained by desorbing lithium adsorbed by an adsorbent with sulfuric acid. The sodium hydroxide purification solution is a sodium hydroxide solution prepared by precisely filtering a solution prepared from pure water and sodium hydroxide to remove impurities, and preferably a sodium hydroxide saturated solution;
the liquid-solid separator in the steps 3) and 5) is a piston pushing type filtering centrifuge, a spiral discharging filtering centrifuge or a cone blue centrifuge.
Compared with the prior art, the invention has the following beneficial effects:
1. the invention adopts the pipeline reactor to continuously feed, continuously react and continuously discharge, shortens the causticizing reaction time, reduces the labor intensity of workers and improves the causticizing efficiency.
2. According to the invention, impurities are removed by a method that lithium hydroxide solution flows through the ion exchange column, so that the continuity of the impurity removal process is realized, the impurity removal efficiency is high, and the effect is good. Not only barium ions and chlorine ions are prevented from being brought into the product, but also the steps of re-dissolution evaporation and re-crystallization are avoided.
3. The continuous and automatic production process of the lithium hydroxide is realized, the process flow is shortened, the energy consumption and the production cost are reduced, and the production efficiency is obviously improved.
4. The process is stable and reliable, the product quality is stable and reaches the GB/26008-2010 battery-grade lithium hydroxide monohydrate standard.
Drawings
The invention is further illustrated by the following figures and examples.
FIG. 1 is a process flow diagram of the present invention.
Detailed Description
Example 1
Mixing Li 2 The lithium sulfate purified solution with the O concentration of 40.15g/L is pumped into an axial inlet of an inlet end of a pipeline reactor of DN200 at a flow rate of 18.17L/min, a sodium hydroxide saturated solution is pumped into the axial inlet of a side surface of the pipeline reactor at a flow rate of 2.81L/min, a causticized solution flows out of an axial outlet of an outlet end of the pipeline reactor, the reaction temperature is maintained at 30 ℃, and a reaction material flows in the pipeline reactor for 30min.
Pumping causticized liquid into a precision filter for filtering and washing to obtain causticized filter liquid and causticized slag, collecting the causticized slag into a causticized slag storage tank for additionally stirring and washing lithium in the recycled slag, pumping the causticized filter liquid into a freezing crystallizer for freezing to-7 ℃, then discharging to a horizontal spiral discharge filtering centrifuge for separating and washing, sending separated sodium sulfate decahydrate to a sodium sulfate anhydrous production workshop for producing anhydrous sodium sulfate, pumping separated lithium hydroxide refrigerating liquid into a heat exchanger for heating to 10 ℃, then pumping into the top of a cation exchange column (resin is Suqing chelating resin D402), performing cation exchange, then entering an anion exchange column (resin is 201 x 4 ion exchange resin) from the top of the anion exchange column, pumping lithium hydroxide refined liquid flowing out from the bottom of the anion exchange column into an MVR evaporator for evaporating until the solid content in the concentrated liquid reaches 10%, starting discharging to the horizontal spiral discharge filtering centrifuge, separating and washing to obtain a lithium hydroxide wet product, pumping a mother liquid back to the ion exchange system from an inlet of the cation exchange column; and (3) sending the lithium hydroxide wet product into a vacuum solid continuous dryer for drying to obtain a lithium hydroxide monohydrate product.
Example 2
Mixing Li 2 Pumping lithium sulfate purified liquid with the O concentration of 40.15g/L into an axial inlet at the inlet end of a pipeline reactor of DN200 at the flow rate of 35.9L/min, simultaneously pumping sodium hydroxide saturated solution into a radial inlet from a side inlet of the pipeline reactor at the flow rate of 6.06L/min, enabling causticized liquid to flow out from an axial outlet at the outlet end of the pipeline reactor, maintaining the reaction temperature at 30 ℃, and enabling reaction materials to flow in the pipeline reactor for 20min; the rest of the procedure was the same as in example 1.
Example 3
Mixing Li 2 Pumping the lithium sulfate purified solution with the O concentration of 33.28g/L into an axial inlet at the inlet end of a pipeline reactor of DN200 at the flow rate of 17.95L/min, simultaneously pumping the sodium hydroxide saturated solution into a radial inlet at the side surface of the pipeline reactor at the flow rate of 3.03L/min, enabling the causticized solution to flow out from an axial outlet at the outlet end of the pipeline reactor, maintaining the reaction temperature at 15 ℃, and enabling the reaction material to flow in the pipeline reactor for 30min.
Pumping causticized liquid into a precision filter for filtering and washing to obtain causticized filter liquid and causticized slag, collecting the causticized slag into a causticized slag storage tank for additionally stirring and washing lithium in the recycled slag, pumping the causticized filter liquid into a freezing crystallizer for freezing to-5 ℃, discharging to a horizontal spiral discharge filtering centrifuge for separating and washing, sending separated sodium sulfate decahydrate to a sodium sulfate anhydrous production workshop for producing anhydrous sodium sulfate, pumping separated lithium hydroxide refrigerating liquid into a heat exchanger for heating to 5 ℃, pumping into the top of a cation exchange column, performing cation exchange, then entering an anion exchange column from the top of the anion exchange column, pumping lithium hydroxide refining liquid flowing out from the bottom of the anion exchange column into an MVR evaporator for evaporation until the solid content in concentrated liquid reaches 15%, starting discharging to the horizontal spiral discharge filtering centrifuge, separating and washing to obtain a lithium hydroxide wet product, pumping mother liquid back, and returning to an ion exchange system from an inlet of the cation exchange column; and (3) sending the lithium hydroxide wet product into a vacuum solid continuous dryer for drying to obtain a lithium hydroxide monohydrate product.
Example 4
Mixing Li 2 Pumping the lithium sulfate purified solution with the O concentration of 33.28g/L into an axial inlet at the inlet end of a pipeline reactor of DN200 at the flow rate of 35.44L/min, simultaneously pumping the sodium hydroxide saturated solution into a radial inlet at the side surface of the pipeline reactor at the flow rate of 6.52L/min, enabling the causticized solution to flow out from an axial outlet at the outlet end of the pipeline reactor, maintaining the reaction temperature at 15 ℃, and enabling the reaction material to flow in the pipeline reactor for 20min; the rest of the procedure was the same as in example 3.
The lithium hydroxide monohydrate products obtained in the above examples 1 to 4 were tested, and the obtained technical indexes are shown in table 1;
TABLE 1
As can be seen from Table 1, the lithium hydroxide product produced by the continuous production process has high purity and stable quality, and the quality of the lithium hydroxide product meets the requirements of the national standard GB/26008-2010 battery-grade lithium hydroxide LiOH. H2O-D1.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the present invention, and any modifications, equivalents and improvements made without departing from the spirit of the present invention are intended to be included in the scope of the present invention.
Claims (4)
1. A continuous production process of lithium hydroxide is characterized by comprising the following steps: the method comprises the following steps:
1) Continuously inputting the lithium sulfate purified solution and the sodium hydroxide purified solution into a pipeline reactor for carrying out causticizing reaction, and continuously outputting a lithium hydroxide and sodium sulfate mixed solution, namely causticized solution, from the pipeline reactor;
2) Filtering the causticized liquid to obtain causticized filtrate;
3) Freezing the causticized liquid and separating sodium sulfate decahydrate from the lithium hydroxide frozen liquid;
4) Heating the lithium hydroxide refrigerating fluid, and then exchanging cations and anions to obtain a lithium hydroxide refined solution;
5) Evaporating and crystallizing the lithium hydroxide refined solution to obtain lithium hydroxide crystal slurry, and separating and washing the lithium hydroxide crystal slurry to obtain a lithium hydroxide wet product;
6) And drying the wet lithium hydroxide product to obtain a lithium hydroxide monohydrate product.
2. The continuous production process of lithium hydroxide according to claim 1, wherein: the method comprises the following specific steps:
1) Inputting lithium sulfate purified liquid axially from an inlet of the pipeline reactor, inputting sodium hydroxide purified liquid radially from an inlet on the side surface of the pipeline reactor, and outputting causticized liquid from an axial outlet of the reactor; the amount of the reaction materials input into the pipeline reactor is controlled according to the molar ratio of sodium hydroxide to lithium sulfate of 2.2-2.4, the causticization reaction temperature is 10-50 ℃, the flow rate of the reaction materials in the pipeline reactor is 0.15-1.8 m/min, and the reaction time of the reaction materials in the pipeline reactor is 15-40min;
2) Inputting the causticized liquid output from the outlet of the reactor into a precision filter or a filter press, filtering and washing to obtain causticized filtrate and causticized slag, collecting the causticized slag, and performing additional agitation washing and recovery;
3) Inputting the causticized filtrate into a freezing and crystallizing system for freezing and crystallizing, and controlling the discharging temperature to be-10 to 0 ℃; discharging, separating sodium sulfate decahydrate from lithium hydroxide refrigerating fluid by a liquid-solid separator, and producing a byproduct anhydrous sodium sulphate by the separated sodium sulfate decahydrate;
4) Inputting lithium hydroxide refrigerating fluid into a heat exchanger, heating to 5-40 ℃, flowing through a cation exchange column and an anion exchange column to remove residual metal impurity ions and sulfate radical impurities to obtain lithium hydroxide refined solution, wherein the cation exchange resin is macroporous strong acid type styrene series chelating resin, and the anion exchange resin is strong base type styrene series anion exchange resin;
5) Inputting the lithium hydroxide refined solution into an evaporator for evaporation and crystallization, discharging lithium hydroxide crystal slurry to a liquid-solid separator when the solid content of the concentrated solution reaches 10 to 15%, separating and washing to obtain a lithium hydroxide wet product, and returning the mother solution to the cation exchange column in the step 4);
6) And (4) inputting the lithium hydroxide wet product into a vacuum drier for drying, and discharging to obtain a lithium hydroxide product.
3. The continuous production process of lithium hydroxide according to claim 1 or 2, characterized in that:
the lithium sulfate purified solution in the step 1) is a purified and impurity-removed lithium sulfate solution; the lithium sulfate solution is any one or a mixture of any more of a lithium sulfate solution obtained by leaching spodumene concentrate with sulfuric acid, a lithium sulfate solution obtained by dissolving lithium carbonate with sulfuric acid, and a lithium sulfate solution obtained by desorbing lithium adsorbed by an adsorbent with sulfuric acid; the sodium hydroxide purification solution is a sodium hydroxide solution prepared by precisely filtering a solution prepared from pure water and sodium hydroxide to remove impurities.
4. The continuous production process of lithium hydroxide according to claim 2, wherein: the liquid-solid separator in the steps 3) and 5) is a piston pushing type filtering centrifuge, a spiral discharging filtering centrifuge or a cone blue centrifuge.
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