CN112713269A - Production system and production method for reducing content of sodium ions and sulfate ions in precursor of positive electrode material - Google Patents
Production system and production method for reducing content of sodium ions and sulfate ions in precursor of positive electrode material Download PDFInfo
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Abstract
The invention belongs to the field of lithium ion battery materials, and particularly relates to a production system and a production method for reducing the production of sodium ions and sulfate ions as precursors of anode materials in industrial production. Solid content in the precipitation reaction process of the precursor is improved through circulation of materials among the reaction kettle, the overflow tank and the precision filter, so that the acting force among particles is increased, the compactness of primary particles is improved, and the physical adsorption quantity of sodium ions and sulfate ions is reduced; the chemical adsorption quantity of sodium ions and sulfate ions is reduced by reducing the content of free nickel in the reaction process. After the precipitation reaction, the solid content of the materials before washing is improved through a storage tank and a thickener, and physical adsorption of sodium ions and sulfate ions is reduced through the acting force among particles. The production system and method of the inventionThe method greatly reduces Na of the precursor of the anode material+And SO4 2‑And (4) content.
Description
Technical Field
The invention relates to the field of lithium ion battery materials, in particular to a production system and a production method for reducing the content of sodium ions and sulfate ions in a precursor of a positive electrode material.
Background
The new energy industry is rapidly developed due to environmental protection and recycling performance, the new energy automobile technology is continuously improved along with the development of the new energy industry, and a plan that the new energy automobile gradually replaces a fuel automobile is published in various countries. As the most environment-friendly vehicle in the future, the safety performance and the service life of the vehicle become the crucial performance indexes.
The positive electrode material accounts for more than 40% of the total battery cost. The ternary cathode material is the most competitive material at present, and has the advantages of high capacity, high cycle performance, high safety performance and the like. The physical and chemical indexes of the ternary cathode material are mainly determined by precursor materials, the precursor materials are prepared by sulfate and sodium hydroxide solution in a coprecipitation system, and the precursor materials contain a large amount of Na+And SO4 2-And the cycle performance and safety performance of the battery are seriously affected.
The patent with publication number CN107611383A discloses a preparation method of a low-sulfur high-tap density nickel-cobalt-manganese ternary precursor, which uses low-concentration alkali liquor for washing, and obtains the low-sulfur ternary precursor with the S content less than or equal to 0.12% through washing for 1 time, pulp washing for 1-3 times and water washing for 1-3 times, and finally drying. The patent reduces the content of the S impurities physically adsorbed by optimizing the washing process, but the S impurities partially chemically adsorbed in the S impurities cannot be effectively removed, so that the content of the S impurities in the finished product is higher.
The patent with publication number CN103342395A discloses a preparation method of a low-sulfur ternary precursor, which is to filter the prepared ternary precursor to remove mother liquor, transfer the ternary precursor into a turbine stirring alkali washing tank, heat the ternary precursor in a water bath, stir and filter the ternary precursor; filtering and washing the product after alkali washing by using a plate frame until the conductivity of washing water is less than or equal to 20 us/cm; the S impurity content of the obtained low-sulfur ternary precursor is less than or equal to 0.2 percent. The patent reduces the content of S impurities by optimizing the washing process, but the effect is not obvious, and the content of Na impurities has higher risk.
Disclosure of Invention
The technical problem to be solved by the invention is to overcome the defects in the prior art and provide a method for reducing Na in a precursor material+And SO4 2-Content production system and production method.
In order to solve the technical problems, the invention adopts the following technical scheme:
the invention provides a production system for reducing sodium ions and sulfate ions in precursor materials, which comprises a reaction kettle, an overflow tank, a precision filter, a storage tank, a concentrator, a centrifugal machine and drying equipment, wherein the reaction kettle is connected with the overflow tank; the overflow tank is connected with the precision filter, and the storage tank is connected with the thickener; the reaction materials in the reaction kettle overflow into an overflow tank, after the materials in the overflow tank reach a target particle size value, the materials are conveyed into a precision filter, and then the materials concentrated by the precision filter return to the reaction kettle to continue the circulation; extracting supernatant liquid in the precision filter, and conveying the supernatant liquid to a storage tank after the solid content of the material in the precision filter reaches a required value; after the liquid level of the storage tank reaches a target value, further conveying the materials to a concentrator for concentration, returning the concentrated materials to the storage tank, and circulating the materials until the solid content of the materials in the storage tank reaches the target value; and then, the materials in the storage tank enter a centrifugal machine for centrifugation and washing, and are transferred to a drying device for drying.
Furthermore, the overflow tank and the precision filter are connected through a diaphragm pump, and the storage tank and the thickener are connected through the diaphragm pump.
Further, the precision filter returns the concentrated material to the reaction kettle through a return pipeline.
Further, the concentrated material returns to the storage tank through a thickener slag discharge pipeline.
By the production system, the content of sodium ions and sulfate ions in the precursor material produced in an industrialized mode can be reduced, the content of the sodium ions is reduced to be below 0.015wt%, and the content of the sulfate ions is reduced to be below 0.1 wt%. In view of the reduction of the content of sodium ions and sulfate ions, the safety performance and the cycle performance of the precursor material are further improved.
Based on the same inventive concept, the invention provides a method for reducing sodium ions and sulfate ions in a precursor material produced in an industrialized mode, which comprises the following steps:
step (1), preparing a mixed salt solution;
adding pure water into a reaction kettle, heating, introducing ammonia water into the reaction kettle after the temperature of the pure water reaches a target temperature, and then introducing an alkali solution to adjust the pH value of the solution in the reaction kettle;
step (3), on the basis of the step (2), adding the mixed salt solution prepared in the step (1) into a reaction kettle, and adjusting the ammonia concentration, the pH value and the concentration of free nickel;
overflowing the materials in the reaction kettle to an overflow tank, conveying the materials in the overflow tank to a precision filter through a diaphragm pump when the granularity of the materials in the overflow tank reaches a required value, returning the materials to the reaction kettle through a backflow pipeline after the materials are concentrated by the precision filter, and keeping circulation;
step (5), extracting supernatant in the precision filter, and conveying the material to a storage tank after the solid content of the material in the precision filter meets the requirement;
step (6), when the liquid level of the storage tank reaches a required value, transferring the material to a thickener at a constant speed through a diaphragm pump for thickening, conveying the thickened material to a storage tank through a slag discharge pipeline of the thickener, and circulating until the solid content of the material in the storage tank is improved to a required range;
and (7) after the solid content of the materials in the storage tank reaches the required range, conveying the materials to a centrifugal machine for dehydration, washing and drying.
Further, in the step (2), the target temperature of the pure water is 50-70 ℃, the reaction kettle is provided with a heating and cooling system, the temperature of the reaction kettle is maintained at 50-80 ℃, ammonia water is introduced into the reaction kettle until the ammonia concentration is 7.8-8.7g/L, and the pH value of the solution in the reaction kettle is 10.8-11.5.
Further, in the step (3), the ammonia concentration is adjusted to 7.8-8.7g/L, the pH value is adjusted to 10.8-11.8, the free nickel concentration is adjusted to be less than 250ppm, and the flow rate of the mixed salt solution is 300-380L/h.
Further, in the step (4), the required value of the granularity of the material in the overflow tank is 9-12 um.
Further, in the step (5), the solid content of the material in the precision filter is required to be in the range of 150-180 g/L.
Further, in the step (6) and the step (7), the required range of the solid content of the material in the storage tank is 250-300 g/L.
Further, in the step (67), the washing is performed by first washing with a dilute alkali solution and then washing with hot pure water.
The dilute alkali solution is a diluted sodium hydroxide solution, the mass concentration of the dilute alkali solution is 2.8 +/-0.5%, and the temperature is 85 +/-1 ℃.
According to the invention, the solid content of the precursor in the precipitation reaction process is improved through the circulation of the materials among the reaction kettle, the overflow tank and the precision filter, the acting force among particles is increased, the compactness of primary particles is improved, and the physical adsorption quantity of sodium ions and sulfate ions is reduced; the chemical adsorption quantity of sodium ions and sulfate ions is reduced by reducing the content of free nickel in the reaction process. After the precipitation reaction, the solid content of the materials before washing is improved through a storage tank and a thickener, physical adsorption of sodium ions and sulfate ions is reduced through the acting force among particles, the sulfate ions in the precursor are reduced through alkali washing in the washing process, the sodium ions in the precursor are reduced through water washing, and the purpose of reducing the content of the sodium ions and the sulfate ions in the precursor material in industrial production is further achieved.
Compared with the prior art, the invention has the following beneficial effects:
(1) the production system and the process are simple, and the large-scale industrial application is facilitated;
(2) not only can reduce the physical adsorption quantity of sodium ions and sulfate ions, but also can reduce the chemical adsorption quantity of the sodium ions and the sulfate ions, and greatly reduces the content of the sodium ions and the sulfate ions in the precursor material;
(3) the production system and the process are very environment-friendly and have low energy consumption.
Detailed Description
The following examples are given to further illustrate the embodiments of the present invention:
example 1
Step (1), adding half-kettle 60 ℃ hot pure water into a batching kettle for carrying out half-kettle dry distillation at 26m, adding 1678.1Kg of nickel sulfate, 726.1Kg of cobalt sulfate and 848.5Kg of manganese sulfate, stirring for 3h, adding hot pure water again to reach a constant volume plate position of the batching kettle, and stirring for 1h to obtain a mixed salt solution with the concentration of 120g/L, wherein the molar ratio of nickel, cobalt and manganese is 5:2: 3;
step (2), setting the stirring speed of the reaction kettle to 220r/min, adding 60 ℃ hot water full of the reaction kettle, setting the temperature of the reaction kettle to 65 ℃, controlling the temperature of the reaction kettle to 65 ℃ in the process, adding ammonia water, testing the ammonia concentration in the reaction kettle by titration, stopping adding the ammonia water when the ammonia concentration reaches 7.8g/L, adding a sodium hydroxide solution, controlling the pH value, and stopping adding alkali when the actually measured pH value reaches 10.8;
step (3), introducing the mixed salt solution at a flow rate of 360L/h, simultaneously starting to feed ammonia water and sodium hydroxide solution, controlling the ammonia concentration within the range of 7.8-8.7g/L and the pH within the range of 10.8-11.8 in the process, and continuously reacting, wherein the content of free nickel is controlled within the range of 100-250 ppm;
overflowing the materials in the reaction kettle to an overflow tank, pumping the materials in the overflow tank to a precision filter through a diaphragm pump when the granularity reaches a required value, returning the materials to the reaction kettle through a backflow pipeline by the precision filter, and keeping circulation for 24 hours;
step (5), starting to clear the precision filter in a circulating state, increasing the solid content, controlling the solid content to be 165g/L, and conveying the material with the solid content meeting the requirement to a storage tank;
step (6), after the liquid level of the storage tank reaches 1m, transferring the materials to a thickener at a constant speed through a diaphragm pump, concentrating the materials through the thickener, and discharging the concentrated materials back to the storage tank through a slag discharge pipeline of the thickener until the solid content of the materials in the storage tank is improved to 290 g/L;
step (7), after the solid content of the storage tank reaches 290g/L, 2000L of materials are thrown into the centrifuge and are dried for 15 min;
step (8), adding a 32% sodium hydroxide solution with a concentration of 0.16m into the dilute alkali preparation tank, then adding 80 ℃ hot pure water for carrying out labor intensity cultivation under 1.84m, preparing the dilute alkali solution for carrying out labor intensity cultivation under 2m, wherein the concentration of the dilute alkali solution is 3.0%, and heating to 85 ℃;
step (9), after the material in the centrifuge is dried, adding dilute alkali solution at the flow rate of 3.4 m/h for 35min, and then drying for 10 min;
step (10), adding hot pure water at the temperature of 80 +/-1 ℃ for 90min at the flow rate of 5.0 m/h, and then carrying out spin-drying for 30 min;
and (11) drying the materials in a rotary kiln, sieving the materials by a batch mixing machine, and then inspecting the materials.
The content of impurities Na and S in the ternary cathode material precursor prepared by the steps is 0.012% and 0.096% respectively.
Example 2
Step (1), adding half-kettle 70 ℃ hot pure water into a batching kettle for carrying out dry distillation at 26m, adding 1678.1Kg of nickel sulfate, 726.1Kg of cobalt sulfate and 848.5Kg of manganese sulfate, stirring for 3h, adding hot pure water again to reach a constant volume plate position of the batching kettle, and stirring for 1h to obtain a mixed solution with the concentration of 120g/L and the ratio of nickel, cobalt and manganese of 5:2: 3;
step (2), setting the stirring speed of the reaction kettle to 220r/min, adding hot water at 70 ℃ full of the reaction kettle, setting the temperature of the reaction kettle to 70 ℃, controlling the temperature of the reaction kettle to 70 ℃ in the process, adding ammonia water, testing the ammonia concentration in the reaction kettle by titration, stopping adding the ammonia water when the ammonia concentration reaches 8.0g/L, adding a sodium hydroxide solution, controlling the pH value, and stopping adding alkali when the actually measured pH value reaches 11.0;
step (3), introducing the mixed salt solution at a flow rate of 320L/h, simultaneously starting to feed ammonia water and sodium hydroxide solution, controlling the ammonia concentration within the range of 7.8-8.7g/L and the pH within the range of 10.8-11.8 in the process, and continuously reacting to control the content of free nickel within the range of 100-250 ppm;
overflowing the materials in the reaction kettle to an overflow tank, pumping the materials in the overflow tank to a precision filter through a diaphragm pump when the granularity reaches a required value, returning the materials to the reaction kettle through a backflow pipeline by the precision filter, and keeping circulation for 24 hours;
step (5), after circulation is carried out for 24 hours, the precision filter starts to discharge clear under the condition of keeping the circulation, so that the solid content is improved, the solid content is controlled at 180g/L, and the material with the solid content meeting the requirement is conveyed to a storage tank;
step (6), after the liquid level of the storage tank reaches 1m, transferring the materials to a thickener at a constant speed through a diaphragm pump, concentrating the materials through the thickener, and discharging the concentrated materials back to the storage tank through a slag discharge pipeline of the thickener until the solid content of the materials in the storage tank is increased to 250 g/L;
step (7), after the solid content of the storage tank reaches 250g/L, 2000L of materials are thrown into a centrifugal machine and are dried for 15 min;
step (8), adding a 32% sodium hydroxide solution with a concentration of 0.16m into a dilute alkali preparation tank, adding 80 ℃ hot pure water for carrying out thin film plantation at 1.84m, preparing the dilute alkali solution for carrying out thin film plantation at 2m, wherein the concentration of the dilute alkali solution is 3.0%, and heating to 85 ℃;
step (9), after the material in the centrifuge is dried, adding dilute alkali solution at the flow rate of 3.4 m/h for 35min, and then drying for 10 min;
step (10), after the alkali is added, carrying out dry cultivation on the material, and then carrying out dry cultivation for 30min after water feeding, wherein hot pure water with the temperature of 80 ℃ is fed at the flow rate of 5.0 m/h;
step (11), drying the materials in a rotary kiln, sieving the materials by a batch mixing machine, and then inspecting the materials;
the content of impurities Na and S in the precursor of the ternary cathode material prepared by the steps is 0.013% and 0.086%.
Example 3
Step (1), adding half-kettle 65 ℃ hot pure water into a batching kettle for carrying out labor-saving cultivation at 26m, adding 1678.1Kg of nickel sulfate, 726.1Kg of cobalt sulfate and 848.5Kg of manganese sulfate, stirring for 3h, adding the hot pure water again to reach a constant volume plate position of the batching kettle, and stirring for 1h to obtain a mixed solution with the concentration of 120g/L and the ratio of nickel, cobalt and manganese of 5:2: 3;
step (2), setting the stirring speed of the reaction kettle to 220r/min, adding 65 ℃ hot water in the full reaction kettle, setting the temperature of the reaction kettle to 65 ℃, controlling the temperature of the reaction kettle to 65 ℃ in the process, adding ammonia water, testing the ammonia concentration in the reaction kettle by titration, stopping adding the ammonia water when the ammonia concentration reaches 8.5g/L, adding a sodium hydroxide solution, controlling the pH value, and stopping adding alkali when the actually measured pH value reaches 11.2;
step (3), introducing a mixed salt solution at a flow rate of 350L/h, simultaneously starting to feed ammonia water and a sodium hydroxide solution, controlling the ammonia concentration within the range of 7.8-8.7g/L and the pH within the range of 10.8-11.8 in the process, and continuously reacting to control the content of free nickel within the range of 100-250 ppm;
overflowing the materials in the reaction kettle to an overflow tank, pumping the materials in the overflow tank to a precision filter through a diaphragm pump when the granularity reaches a required value, returning the materials to the reaction kettle through a backflow pipeline by the precision filter, and keeping circulation for 24 hours;
step (5), after circulation is carried out for 24 hours, the precision filter starts to discharge clear under the condition of keeping the circulation, so that the solid content is improved, the solid content is controlled at 150g/L, and the material with the solid content meeting the requirement is conveyed to a storage tank;
step (6), after the liquid level of the storage tank reaches 1m, transferring the material to a thickener at a constant speed through a diaphragm pump, concentrating the material through the thickener, and discharging the concentrated material back to the storage tank through a slag discharge pipeline of the thickener until the solid content of the material in the storage tank is increased to 275 g/L;
step (7), after the solid content of the storage tank reaches 275g/L, 2000L of materials are thrown into a centrifugal machine and are dried for 15 min;
step (8), adding a 32% sodium hydroxide solution with a concentration of 0.16m into a dilute alkali preparation tank, adding 80 ℃ hot pure water for carrying out thin film plantation at 1.84m, preparing the dilute alkali solution for carrying out thin film plantation at 2m, wherein the concentration of the dilute alkali solution is 3.0%, and heating to 85 ℃;
step (9), after the material in the centrifuge is dried, adding dilute alkali solution at the flow rate of 3.4 m/h for 35min, and then drying for 10 min;
step (10), after the alkali is added, carrying out dry cultivation on the material, and then carrying out dry cultivation for 30min after water is added, wherein hot pure water with the temperature of 80 +/-1 ℃ is fed at the flow rate of 5.0 m/h;
and (11) drying the materials in a rotary kiln, sieving the materials by a batch mixing machine, and then inspecting the materials.
The content of impurities Na and S in the precursor of the ternary cathode material prepared by the steps is 0.013% and 0.088%.
Example 4
Step (1), adding half-kettle 60 ℃ hot pure water into a batching kettle for carrying out dry distillation at 26m, adding 1678.1Kg of nickel sulfate, 726.1Kg of cobalt sulfate and 848.5Kg of manganese sulfate, stirring for 3h, adding hot pure water again to reach a constant volume plate position of the batching kettle, and stirring for 1h to obtain a mixed solution with the concentration of 120g/L and the ratio of nickel, cobalt and manganese of 5:2: 3;
step (2), setting the stirring speed of the reaction kettle to 220r/min, adding hot water at 70 ℃ full of the reaction kettle, setting the temperature of the reaction kettle to 70 ℃, controlling the temperature of the reaction kettle to 70 ℃ in the process, adding ammonia water, testing the ammonia concentration in the reaction kettle by titration, stopping adding the ammonia water when the ammonia concentration reaches 8.5g/L, adding a sodium hydroxide solution, controlling the pH value, and stopping adding alkali when the actually measured pH value reaches 11.5;
step (3), introducing mixed salt solution at the flow rate of 340L/h, simultaneously starting to feed ammonia water and sodium hydroxide solution, controlling the ammonia concentration within the range of 7.8-8.7g/L and the pH within the range of 10.8-11.8 in the process, continuously reacting, and controlling the content of free nickel within the range of less than 250 ppm;
overflowing the materials in the reaction kettle to an overflow tank, pumping the materials in the overflow tank to a precision filter through a diaphragm pump when the granularity reaches a required value, returning the materials to the reaction kettle through a backflow pipeline by the precision filter, and keeping circulation for 24 hours;
step (5), after circulation is carried out for 24 hours, the precision filter starts to discharge clear under the condition of keeping the circulation, so that the solid content is improved, the solid content is controlled at 160g/L, and the material with the solid content meeting the requirement is conveyed to a storage tank;
step (6), after the liquid level of the storage tank reaches 1m, transferring the materials to a thickener at a constant speed through a diaphragm pump, concentrating the materials through the thickener, and discharging the concentrated materials back to the storage tank through a slag discharge pipeline of the thickener until the solid content of the materials in the storage tank is increased to 300 g/L;
step (7), after the solid content of the storage tank reaches 300g/L, 2000L of materials are thrown into a centrifugal machine and are dried for 15 min;
step (8), adding a 32% sodium hydroxide solution with a concentration of 0.16m into a dilute alkali preparation tank, adding 80 ℃ hot pure water for carrying out thin film plantation at 1.84m, preparing the dilute alkali solution for carrying out thin film plantation at 2m, wherein the concentration of the dilute alkali solution is 3.0%, and heating to 85 ℃;
step (9), after the material in the centrifuge is dried, adding dilute alkali solution at the flow rate of 3.4 m/h for 35min, and then drying for 10 min;
step (10), after the alkali is added, carrying out dry cultivation on the material, and then carrying out dry cultivation for 30min after feeding hot pure water at the temperature of 80 ℃ at the flow rate of 5.2 m/h;
and (11) drying the materials in a rotary kiln, sieving the materials by a batch mixing machine, and then inspecting the materials.
The ternary positive electrode material precursor prepared by the steps has the impurity Na content of 0.014% and the S content of 0.096%.
Example 5
Step (1), adding half-kettle 60 ℃ hot pure water into a batching kettle for carrying out dry distillation at 26m, adding 1678.1Kg of nickel sulfate, 726.1Kg of cobalt sulfate and 848.5Kg of manganese sulfate, stirring for 3h, adding hot pure water again to reach a constant volume plate position of the batching kettle, and stirring for 1h to obtain a mixed solution with the concentration of 120g/L and the ratio of nickel, cobalt and manganese of 5:2: 3;
step (2), setting the stirring speed of the reaction kettle to 220r/min, adding 60 ℃ hot water full of the reaction kettle, setting the temperature of the reaction kettle to 60 ℃, controlling the temperature of the reaction kettle to be 60 ℃ in the process, adding ammonia water, testing the ammonia concentration in the reaction kettle by titration, stopping adding the ammonia water when the ammonia concentration reaches 8.7g/L, adding a sodium hydroxide solution, controlling the pH value, and stopping adding alkali when the actually measured pH value reaches 11.5;
step (3), introducing a mixed salt solution at a flow rate of 350L/h, simultaneously starting to feed ammonia water and a sodium hydroxide solution, controlling the ammonia concentration to be within a range of 7.8-8.7g/L and the pH to be within a range of 10.8-11.8 in the process, continuously reacting, and controlling the content of free nickel to be less than 100 ppm;
overflowing the materials in the reaction kettle to an overflow tank, pumping the materials in the overflow tank to a precision filter through a diaphragm pump when the granularity reaches a required value, returning the materials to the reaction kettle through a backflow pipeline by the precision filter, and keeping circulation for 24 hours;
after circulation for 24 hours, the precision filter starts to discharge clear under the condition of keeping the circulation, so that the solid content is improved, the solid content is controlled at 175g/L, and the material with the solid content meeting the requirement is conveyed to a storage tank;
step (6), transferring the material to a thickener at a constant speed through a diaphragm pump after the liquid level of the material storage tank reaches 1m, concentrating the material through the thickener, and discharging the concentrated material back to the material storage tank through a slag discharge pipeline of the thickener until the solid content of the material in the material storage tank is improved to 280 g/L;
step (7), after the solid content of the storage tank reaches 280g/L, 2000L of materials are thrown into a centrifugal machine and are dried for 15 min;
step (8), adding a 32% sodium hydroxide solution with a concentration of 0.16m into a dilute alkali preparation tank, adding 80 ℃ hot pure water for carrying out thin film plantation at 1.84m, preparing the dilute alkali solution for carrying out thin film plantation at 2m, wherein the concentration of the dilute alkali solution is 3.0%, and heating to 85 ℃;
step (9), after the material in the centrifuge is dried, adding dilute alkali solution at the flow rate of 3.6 m/h for 35min, and then drying for 10 min;
step (10), after the alkali is added, carrying out dry cultivation on the material, and then carrying out dry cultivation for 30min after water feeding, wherein hot pure water with the temperature of 80 ℃ is fed at the flow rate of 5.0 m/h;
step (11), drying the materials in a rotary kiln, sieving the materials by a batch mixing machine, and then inspecting the materials;
the content of impurities Na and S in the ternary cathode material precursor prepared by the steps is 0.012% and 0.096% respectively.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (10)
1. A production system for reducing sodium ions and sulfate ions in precursor materials is characterized by comprising a reaction kettle, an overflow tank, a precision filter, a storage tank, a concentrator, a centrifugal machine and drying equipment; the overflow tank is connected with the precision filter, and the storage tank is connected with the thickener; the reaction materials in the reaction kettle overflow into an overflow tank, after the materials in the overflow tank reach a target particle size value, the materials are conveyed into a precision filter, and then the materials concentrated by the precision filter return to the reaction kettle to continue the circulation; extracting supernatant liquid in the precision filter, and conveying the supernatant liquid to a storage tank after the solid content of the material in the precision filter reaches a required value; after the liquid level of the storage tank reaches a target value, further conveying the materials to a concentrator for concentration, returning the concentrated materials to the storage tank, and circulating the materials until the solid content of the materials in the storage tank reaches the target value; and then, the materials in the storage tank enter a centrifugal machine for centrifugation and washing, and are transferred to a drying device for drying.
2. The production system of claim 1, wherein the overflow tank and the fine filter are connected by a diaphragm pump, and the holding tank and the thickener are connected by a diaphragm pump; and the precision filter returns the concentrated material to the reaction kettle through a return pipeline.
3. The production system of claim 1, wherein the concentrated material is returned to the holding tank through a thickener reject conduit.
4. A method for reducing sodium ions and sulfate ions in a precursor material produced in an industrialized mode is characterized by comprising the following steps:
step (1), preparing a mixed salt solution;
adding pure water into a reaction kettle, heating, introducing ammonia water into the reaction kettle after the temperature of the pure water reaches a target temperature, and then introducing an alkali solution to adjust the pH value of the solution in the reaction kettle;
step (3), on the basis of the step (2), adding the mixed salt solution prepared in the step (1) into a reaction kettle, and adjusting the ammonia concentration, the pH value and the concentration of free nickel;
overflowing the materials in the reaction kettle to an overflow tank, conveying the materials in the overflow tank to a precision filter through a diaphragm pump when the granularity of the materials in the overflow tank reaches a required value, returning the materials to the reaction kettle through a backflow pipeline after the materials are concentrated by the precision filter, and keeping circulation;
step (5), extracting supernatant in the precision filter, and conveying the material to a storage tank after the solid content of the material in the precision filter meets the requirement;
step (6), when the liquid level of the storage tank reaches a required value, transferring the material to a thickener at a constant speed through a diaphragm pump for thickening, conveying the thickened material to a storage tank through a slag discharge pipeline of the thickener, and circulating until the solid content of the material in the storage tank is improved to a required range;
and (7) after the solid content of the materials in the storage tank reaches the required range, conveying the materials to a centrifugal machine for dehydration, washing and drying.
5. The method according to claim 4, wherein in the step (2), the target temperature of the pure water is 50-70 ℃, the reaction kettle is provided with a heating and cooling system, and the temperature of the reaction kettle is maintained at 50-80 ℃; and (3) introducing ammonia water into the reaction kettle until the ammonia concentration is 7.8-8.7g/L and the pH value of the solution in the reaction kettle is 10.8-11.5.
6. The method as claimed in claim 4, wherein in step (3), the ammonia concentration is adjusted to 7.8-8.7g/L, the pH value is adjusted to 10.8-11.8, the free nickel concentration is adjusted to < 250ppm, and the flow rate of the mixed salt solution is 300-380L/h.
7. The method according to claim 4, wherein in the step (4), the required value of the particle size of the material in the overflow tank is 9-12 um.
8. The method as claimed in claim 4, wherein in the step (5), the solid content of the material in the precision filter is required to be in the range of 150-180 g/L.
9. The method as claimed in claim 4, wherein in step (6) and step (7), the required range of the solid content of the storage tank material is 250-300 g/L.
10. The method according to claim 4, wherein in step (7), the washing is performed by washing with an alkaline solution and then washing with hot pure water.
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