WO2024055514A1

WO2024055514A1 - High-nickle ternary precursor, preparation method therefor, and use thereof

Info

Publication number: WO2024055514A1
Application number: PCT/CN2023/077444
Authority: WO
Inventors: 石倩茜; 李长东; 张世杰; 方珍奇; 刘更好; 阮丁山
Original assignee: 广东邦普循环科技有限公司; 湖南邦普循环科技有限公司
Priority date: 2022-09-13
Filing date: 2023-02-21
Publication date: 2024-03-21
Also published as: CN115448382B; FR3139564A1; CN115448382A

Abstract

Disclosed are a high-nickel ternary precursor, a preparation method therefor, and use thereof. The preparation method comprises the following steps: separately adding a metal salt, ammonia water, and a precipitant into a base solution, which contains a precipitant and ammonia water and has an oxygen content of less than 1%, for a coprecipitation reaction to prepare the high-nickel ternary precursor. The coprecipitation reaction comprises: introducing protective gas first for a reaction, and then introducing oxygen-containing gas for a reaction, wherein the temperature of the coprecipitation reaction is 25-40 °C, and the concentration of ammonia water is 0.5-2.5 g/L. According to the preparation method in the present invention, the base solution with an oxygen content of less than 1% is used and nitrogen is introduced for nucleation in the early stage of the reaction, such that an agglomeration problem in the early stage of the reaction is alleviated. Primary particles can be refined at an extremely low ammonia concentration in the whole preparation process. A relatively low reaction temperature is adopted in the present invention, which has a positive effect on refining primary particles in one aspect, and can avoid secondary nucleation in a low-ammonia environment in another aspect.

Description

A high-nickel ternary precursor and its preparation method and application

Technical field

The invention belongs to the field of lithium-ion batteries, and specifically relates to a high-nickel ternary precursor and its preparation method and application.

Background technique

Lithium-ion batteries are widely used in electric vehicles, power tools, 3C and other fields with the advantages of stable voltage, high capacity, high energy density, low self-discharge, stable cycle, low consumption, and environmental friendliness. With the development of science and technology, the energy density of batteries has increased. and safety requirements are getting higher and higher. Ternary materials have high reversible specific capacities, which can better meet the increasingly miniaturized and multifunctional requirements of electronic products. The morphology, particle size, specific surface area, and Physical and chemical indicators such as tap density largely determine the performance of ternary cathode materials.

High-nickel single crystal ternary cathode material has the advantages of high specific capacity, low pollution, moderate price, and good match with electrolyte. It has become the focus of cathode materials and is considered to be a very promising cathode material for lithium-ion batteries. There is a very broad market in the field of power batteries. Compared with high-nickel polycrystalline ternary cathode materials, high-nickel single crystal ternary cathode materials have fewer grain boundaries, low internal resistance, and better cycle performance. In addition, the mechanical strength of high-nickel single crystal ternary cathode materials is higher than that of high-nickel polycrystalline ternary cathode materials and has a higher compaction density.

In actual production, when the co-precipitation method is used to prepare ternary precursors, the particles are prone to agglomeration, resulting in twin balls or agglomerates with poor sphericity. The agglomeration of ternary precursor particles has a negative impact on the physical and chemical indicators and electrical properties of subsequent products. In order to improve the energy density and charge-discharge performance of ternary lithium-ion batteries, ternary precursor materials need to have both high tap density (TD) and high specific surface area (BET). Refining primary particles is an effective way to simultaneously increase tap density and specific surface area, but the existing preparation method is to refine primary particles, usually using higher pH or lower ammonia concentration to refine primary particles. This This method can easily lead to secondary nucleation of the precursor in the subsequent reaction process, destroying the particle size distribution of the primary particles, and forming more serious agglomeration, resulting in a lower energy density and poor charge and discharge performance of the prepared cathode material. In order to solve the above-mentioned problems existing in the prior art in refining primary particles, it is urgent to develop a method for preparing a highly dispersed high-nickel ternary precursor.

Contents of the invention

In order to overcome the above-mentioned problems in the prior art, one of the objects of the present invention is to provide a method for preparing a high-nickel ternary precursor. The high-nickel ternary precursor prepared by the preparation method has high dispersibility.

The second object of the present invention is to provide a high-nickel ternary precursor.

The third object of the present invention is to provide an application of a high-nickel ternary precursor in the field of lithium-ion batteries.

In order to achieve the above objects, the technical solutions adopted by the present invention are:

A first aspect of the invention provides a method for preparing a high-nickel ternary precursor, which includes the following steps:

Add metal salt, ammonia water and precipitant to a bottom liquid containing a precipitant and ammonia water with an oxygen content of less than 1% respectively to perform a co-precipitation reaction to prepare the high-nickel ternary precursor;

The co-precipitation reaction is as follows: first, a protective gas is introduced to carry out the reaction, and then an oxygen-containing gas is introduced to react,

The temperature of the co-precipitation reaction is 25-40°C, and the ammonia concentration is 0.5-2.5g/L.

In the present invention, the use of a bottom liquid with an oxygen content of less than 1% and the introduction of protective gas (nitrogen) are beneficial to improving the sphericity in the initial stage of the reaction; then the oxygen-containing gas is introduced through air oxidation, which on the one hand increases the reaction rate and on the other hand further refines the Primary particles; the entire preparation process uses a combination of lower temperature and extremely low ammonia concentration to refine the primary particles, avoid secondary nucleation and agglomeration of primary particles, and optimize sphericity.

Preferably, the pH of the bottom liquid is 10.5-11.0.

Preferably, the ammonia concentration in the bottom liquid is 0.5-2.5g/L.

Preferably, the temperature of the bottom liquid is 25-40°C.

Preferably, the preparation method of the bottom liquid is: passing protective gas into the bottom liquid containing the precipitant and ammonia water so that the oxygen content in the bottom liquid is less than 1%.

Preferably, in the preparation method of the bottom liquid, the time required for introducing the protective gas is 4 to 6 hours. The time and amount of introducing protective gas into the bottom liquid are determined according to the oxygen content in the bottom liquid. When the oxygen content in the bottom liquid is less than 1%, the introduction of protective gas can be stopped.

Preferably, the metal salt is a metal salt solution.

Preferably, the addition flow rate of the metal salt solution is 100-800L/h.

Preferably, the total concentration of metal ions in the metal salt solution is 115-125g/L.

Preferably, the metal salt solution is a soluble salt solution of nickel, cobalt and manganese.

Preferably, the molar ratio of nickel ions, cobalt ions and manganese ions in the metal salt solution is x:y:z, where x+y+z=100, 90≤x<98, 0<y<5, z>0.

Preferably, the soluble salt solution of nickel, cobalt and manganese includes at least one of a sulfate solution, a nitrate solution, and a hydrochloride solution.

Preferably, the sulfate solution includes at least one of nickel sulfate solution, cobalt sulfate solution, and manganese sulfate solution.

Preferably, the nitrate solution includes at least one of nickel nitrate solution, cobalt nitrate solution, and manganese nitrate solution.

Preferably, the hydrochloride solution includes at least one of nickel hydrochloride solution, cobalt hydrochloride solution, and manganese hydrochloride solution.

Preferably, the addition flow rate of the precipitant is 50-400L/h.

Preferably, the concentration of the precipitating agent is 6 to 10 mol/L; further preferably, the concentration of the precipitating agent is 7 to 9 mol/L; Still further preferably, the concentration of the precipitating agent is 8 mol/L.

Preferably, the precipitating agent includes alkaline solution.

Preferably, the alkali solution is at least one of sodium hydroxide and potassium hydroxide.

Preferably, the alkali liquid is industrial liquid alkali.

Preferably, the addition flow rate of the ammonia water is 1 to 100L/h.

Preferably, the concentration of the ammonia water is 0.4-0.8 mol/L; further preferably, the concentration of the ammonia water is 0.5-0.7 mol/L; still further preferably, the concentration of the ammonia water is 0.6 mol/L.

Preferably, the time required for the step of adding metal salt, ammonia water and precipitant is 60 to 70 hours.

Preferably, the flow ratio of the protective gas to the metal salt solution is (2-3):1.

Preferably, the flow ratio of the oxygen-containing gas to the metal salt solution is (0.1-0.5):1.

Preferably, in the co-precipitation reaction, the time required for introducing protective gas is 4 to 6 hours.

Preferably, the protective gas used in the present invention includes at least one of nitrogen, argon, and helium; further preferably, the protective gas is nitrogen.

Preferably, in the co-precipitation reaction, the time required for introducing oxygen-containing gas is 54 to 66 hours.

Preferably, the oxygen-containing gas includes at least one of air and oxygen; further preferably, the oxygen-containing gas is air.

Preferably, the pH of the coprecipitation reaction is 9.5-10.

Preferably, the co-precipitation reaction time is 60 to 70 hours.

Preferably, the preparation method is carried out in a reaction vessel with a stirrer.

Preferably, the liquid inlets of the metal salt solution, ammonia water and precipitant are at the same height as the nitrogen gas inlet, and the nitrogen gas outlet is located above the stirrer in the reaction vessel.

Preferably, the oxygen content in the reaction vessel is <1%.

Preferably, the stirring speed of the coprecipitation reaction is 300-500 r/min; further preferably, the stirring speed of the coprecipitation reaction is 350-450 r/min.

Preferably, the preparation method further includes the steps of aging, washing and drying; the steps of aging, washing and drying are located after the co-precipitation reaction step.

Preferably, the base liquid also contains an antioxidant, and the antioxidant is at least one of ascorbic acid and hydrazine hydrate. Adding antioxidants to the reaction bottom solution can further reduce the surface viscosity of small particles, thereby reducing the early agglomeration of small particles and optimizing sphericity.

Preferably, the preparation method further includes the step of monitoring particle size; the step of monitoring particle size is located in the co-precipitation reaction. should be in the process of steps. During the co-precipitation reaction process, the particle size needs to be continuously monitored. Before the particle size does not meet the requirements, a high-efficiency thickener will be used during the reaction process to collect all particles and return them to the reactor at any time to continue the reaction and grow. When the particle size D50 reaches 2.0-4.0 μm, stop feeding until the material reaction is complete, and obtain an ultra-fine high-nickel ternary precursor with a nickel content of 90-98 mol%.

A second aspect of the present invention provides a high-nickel ternary precursor, which is produced by the method provided by the first aspect of the present invention.

Preferably, the molar ratio of nickel element, cobalt element and manganese element in the precursor is x:y:z, where x+y+z=100, 90≤x<98, 0<y<5, z >0.

Preferably, the nickel content in the precursor is 90% to 98%.

Preferably, the _D50 of the precursor is 2 to 4 μm.

Preferably, the specific surface area of the precursor is 45 to 70 m ² /g.

The third aspect of the present invention provides the application of the above-mentioned high-nickel ternary precursor in the field of lithium-ion batteries.

The beneficial effects of the present invention are: the preparation method of the present invention can alleviate the agglomeration problem in the early stage of the reaction to a certain extent by using a bottom liquid with an oxygen content of less than 1% and passing in protective gas (nitrogen) for nucleation in the early stage of the reaction; The entire preparation process is carried out under extremely low ammonia concentration to refine the primary particles. However, the existing conventional process using low ammonia concentration reaction will cause secondary nucleation in the later stage, seriously affecting the particle distribution and sphericity. In order to avoid this phenomenon, The present invention adopts a lower reaction temperature, which on the one hand has a positive effect on primary particle refinement, and on the other hand, can avoid the generation of secondary nucleation in a low ammonia environment; in addition, in the later stage of the preparation process, through quantitative oxidation with air, a On the one hand, the reaction rate is increased, and on the other hand, the primary particles are further refined, thereby increasing the specific surface area and tap density of the prepared high-nickel ternary precursor.

The high-nickel ternary precursor in the present invention has a nickel content of 90-98%, has high dispersion, no agglomeration, and ultra-fine primary particles, and also has high specific surface area and tap density, of which the specific surface area can reach 45～70m ² /g. Applying this ternary precursor to lithium-ion batteries can significantly improve the electrical performance of the battery.

BRIEF DESCRIPTION OF THE DRAWINGS

Figure 1 is an SEM image of the high-nickel ternary precursor prepared in Example 1 of the present invention.

Figure 2 is an SEM image of the high-nickel ternary precursor prepared in Example 2 of the present invention.

Figure 3 is an SEM image of the high-nickel ternary precursor prepared in Comparative Example 1 of the present invention.

Figure 4 is an SEM image of the high-nickel ternary precursor prepared in Comparative Example 2 of the present invention.

Figure 5 is an SEM image of the high-nickel ternary precursor prepared in Comparative Example 3 of the present invention.

Detailed ways

The specific implementation of the present invention will be further described in detail below in conjunction with the accompanying drawings and examples, but the implementation and protection of the present invention are not limited to Limited to this. It should be pointed out that any process that is not specifically described in detail below can be implemented or understood by those skilled in the art with reference to the existing technology. If the manufacturer of the reagents or instruments used is not indicated, they are regarded as conventional products that can be purchased commercially.

Example 1:

The high-nickel ternary precursor in this example is prepared using the following preparation method, which specifically includes the following steps:

(1) Prepare sulfate solution A containing nickel ions, cobalt ions and manganese ions with a total ion concentration of 120g/L, in which the molar ratio of nickel ions, cobalt ions and manganese ions is 94:2:4, Industrial liquid caustic soda with a concentration of 8 mol/L is used as the precipitant solution B, and ammonia water with a concentration of 0.6 mol/L is used as the complexing agent solution C;

(2) Add 6000L distilled water to the reaction kettle, then add 8mol/L precipitant solution B and 0.6mol/L complexing agent solution C to obtain bottom liquid D with a pH of 11.00 and an ammonia concentration of 1.5g/L. The temperature of liquid D is 35°C, and nitrogen gas is passed into bottom liquid D for about 5 hours to make the dissolved oxygen content of bottom liquid D less than 1 mg/L. Then add sulfate solution A, precipitant solution B, and complexing agent solution C into the above-mentioned bottom liquid D at flow rates of 600L/h, 240L/h, and 8L/h respectively to perform a co-precipitation reaction. During the co-precipitation reaction, The ammonia concentration of the reaction system is 1.5g/L, the reaction pH is 9.60, the temperature is 35°C, and the stirring speed is 400rpm. After the co-precipitation reaction starts, continue to introduce nitrogen for 5 hours, with a nitrogen flow rate of 1000L/h, and then start to introduce air to continue the reaction for about 60 hours. The flow ratio of air flow to sulfate solution A is 0.8; the current precursor particles have grown to the target When the particle size is 3 μm, stop feeding the sulfate solution A, precipitant solution B, and complexing agent solution C until the reaction is complete, end the reaction, and obtain a spherical high-nickel ternary precursor, and perform centrifugation, washing, drying, and removal of magnetic foreign matter, etc. After processing, a spherical high-nickel ternary precursor finished material is obtained.

Example 2:

(1) Prepare sulfate solution A containing nickel ions, cobalt ions and manganese ions with a total ion concentration of 120g/L, in which the molar ratio of nickel ions, cobalt ions and manganese ions is 96:1:3, Industrial liquid caustic soda with a concentration of 8 mol/L is used as the precipitant solution B, and ammonia water with a concentration of 0.6 mol/L is used as the complexing agent solution C;

(2) Add 6000L distilled water to the reaction kettle, then add 8mol/L precipitant solution B and 0.6mol/L complexing agent solution C to obtain bottom liquid D with a pH of 11.00 and an ammonia concentration of 1.0g/L. The temperature of liquid D is 40°C, and nitrogen gas is passed into bottom liquid D for about 5 hours so that the dissolved oxygen content of bottom liquid D is less than 1 mg/L. Then add sulfate solution A, precipitant solution B, and complexing agent solution C into the above-mentioned bottom liquid D at flow rates of 600L/h, 240L/h, and 8L/h respectively to perform a co-precipitation reaction. During the co-precipitation reaction, The ammonia concentration of the reaction system is 1.5g/L, the reaction pH is 9.60, the temperature is 40°C, and the stirring speed is 400rpm. After the co-precipitation reaction begins, continue to introduce nitrogen for 5 hours, with a nitrogen flow rate of 1000L/h, and then start to introduce air to continue the reaction for about 60 hours. The flow ratio of air flow to sulfate solution A is 0.6. The current precursor particles grow to the target. Stop when particle size is 3μm Stop the flow of sulfate solution A, precipitant solution B and complexing agent solution C until the reaction is complete, end the reaction, and obtain a spherical high-nickel ternary precursor. After centrifugation, washing, drying, and removal of magnetic foreign matter, we obtain Spherical high-nickel ternary precursor finished material.

Comparative example 1:

(2) Add 6000L distilled water to the reaction kettle, then add 8mol/L precipitant solution B and 0.6mol/L complexing agent solution C to obtain bottom liquid D with a pH of 11.00 and an ammonia concentration of 6g/L. The temperature of D is 35°C, and nitrogen gas is passed into the bottom liquid D for about 5 hours so that the dissolved oxygen content of the bottom liquid D is less than 1 mg/L. Then add sulfate solution A, precipitant solution B, and complexing agent solution C into the above-mentioned bottom liquid D at flow rates of 600L/h, 240L/h, and 35L/h respectively to perform a co-precipitation reaction. During the co-precipitation reaction, the reaction system The ammonia concentration is 6g/L, the reaction pH is 9.60, the temperature is 35°C, and the stirring speed is 400rpm. After the co-precipitation reaction starts, nitrogen gas is continuously introduced for 5 hours, the nitrogen flow rate is 1000L/h, and then air is introduced to continue the reaction. For about 60 hours, the flow ratio of air flow to sulfate solution A is 0.8; when the precursor particles grow to the target particle size of 3 μm, stop feeding sulfate solution A, precipitant solution B, and complexing agent solution C until the reaction is complete and end. After the reaction, a spherical high-nickel ternary precursor is obtained, and after centrifugation, washing, drying, and removal of magnetic foreign matter, a spherical high-nickel ternary precursor finished material is obtained.

Comparative example 2:

The high-nickel ternary precursor in this example is prepared by the following preparation method, which specifically includes the following steps:

(2) Add 6000L distilled water to the reaction kettle, then add 8mol/L precipitant solution B and 0.6mol/L complexing agent solution C to obtain bottom liquid D with a pH of 11.00 and an ammonia concentration of 1.5g/L. The temperature of liquid D is 60°C, and nitrogen gas is passed into bottom liquid D for about 5 hours so that the dissolved oxygen content of bottom liquid D is less than 1 mg/L. Then add sulfate solution A, precipitant solution B, and complexing agent solution C into the above bottom liquid D at flow rates of 600L/h, 240L/h, and 8L/h respectively to perform a co-precipitation reaction. During the co-precipitation reaction, the reaction system The ammonia concentration is 1.5g/L, the reaction pH is 9.60, the temperature is 60°C, and the stirring speed is 400rpm. After the reaction starts, nitrogen gas is continuously introduced for 5h, the nitrogen flow rate is 1000L/h, and then air is introduced to continue the reaction for about 60h. , the flow ratio of air flow to sulfate solution A is 0.8. When the precursor particles grow to the target particle size of 3 μm, the flow of sulfate solution A, precipitant solution B, and complexing agent solution C is stopped until the reaction is complete, the reaction is terminated, and a spherical high-nickel ternary precursor is obtained. After centrifugation, washing, drying, and removal of magnetic foreign matter, a spherical high-nickel ternary precursor finished product material is obtained.

Comparative example 3:

(2) Add 6000L distilled water to the reaction kettle, then add 8mol/L precipitant solution B and 0.6mol/L complexing agent solution C to obtain bottom liquid D with a pH of 11.5 and an ammonia concentration of 12g/L. D temperature is 50℃. Then add sulfate solution A, precipitant solution B, and complexing agent solution C into the above-mentioned bottom liquid D at flow rates of 600L/h, 240L/h, and 70L/h respectively to perform a co-precipitation reaction. During the co-precipitation reaction, the reaction system The ammonia concentration is 12g/L, the reaction pH is 11.4, the temperature is 50°C, and the stirring speed is 400rpm; when the precursor particles grow to the target particle size of 3 μm, the flow of sulfate solution A, precipitant solution B and complexing agent is stopped. Solution C is used until the reaction is complete, the reaction is terminated, and a spherical high-nickel ternary precursor is obtained. After centrifugation, washing, drying, and magnetic foreign matter removal, the spherical high-nickel ternary precursor finished product material is obtained.

Performance Testing:

The primary particle length, primary particle diameter, specific surface area, tap density, D ₅₀ and D _max data of the high nickel ternary precursors in Examples 1 to 2 and Comparative Examples 1 to 3 were tested respectively, where the specific surface area was measured in shell. Stetech 3H-2000PS2 BET tester was used for testing; tap density was tested using Rico FT-100A tap density meter; D ₅₀ and D _max data were tested using Malvern Laser Particle Size Analyzer 3000; the specific test results are as shown in the table 1 shown.

Table 1 Performance data of high-nickel ternary precursors in Examples 1 to 2 and Comparative Examples 1 to 3

It can be seen from Table 1 that compared with Comparative Example 3, the primary particle size of the high-nickel ternary precursor in Examples 1 and 2 is greatly reduced, and the specific surface area and tap density are increased; similar to the D ₅₀ case Below, D _max of Example 1 and Example 2 is significantly smaller than Comparative Example 3, indicating that the dispersion and sphericity of the high-nickel ternary precursor in Examples 1 and 2 are significantly better; the primary particle size of the high-nickel ternary precursor in Comparative Example 1 is larger, Although the primary particles of the high-nickel ternary precursor in Comparative Example 2 are obviously refined, their agglomeration is serious, and Dmax is extremely large under the same D ₅₀ condition.

Figures 1 to 5 are SEM images of the high-nickel ternary precursors in Examples 1 to 2 and Comparative Examples 1 to 3 respectively, where Figure 1(a) and Figure 1(b) are respectively when the scale bar is 50 μm and 1 μm. SEM image of the high-nickel ternary precursor in Example 1; Figure 2(a) and Figure 2(b) are SEM images of the high-nickel ternary precursor in Example 2 when the scale bar is 50 μm and 1 μm respectively; Figure 3(a) and Figure 3(b) are SEM images of the high-nickel ternary precursor in Comparative Example 1 when the scale bar is 50 μm and 1 μm respectively; Figure 4(a) and Figure 4(b) are respectively when the scale bar is 50 μm and 1 μm. The SEM image of the high-nickel ternary precursor in Comparative Example 2 when the scale is 1 μm; Figure 5(a) and Figure 5(b) are the SEM images of the high-nickel ternary precursor in Comparative Example 3 when the scale bar is 50 μm and 1 μm respectively. ; By comparing Figures 1 to 5, it can be seen that the high-nickel ternary precursor prepared in Comparative Example 3 has a large primary particle size and a large diameter, so its specific surface area is small; while Examples 1 and 2 of the present invention adjust the bottom liquid The primary particle size of the high-nickel ternary precursor prepared under the conditions, reaction temperature and ammonia concentration is small, and the specific surface area and tap density are increased, especially the specific surface area is greatly increased; while Comparative Example 1 adopts low-temperature reaction conditions , but due to its high ammonia concentration, the primary particle refinement of the prepared high-nickel ternary precursor is not obvious; although Comparative Example 2 uses extremely low ammonia concentration, due to its high reaction temperature, the prepared high-nickel ternary precursor Although the primary particles of the precursor are significantly refined, there are obvious secondary nucleations, extremely poor sphericity, and extremely serious agglomeration.

The embodiments of the present invention have been described in detail above. However, the present invention is not limited to the above-mentioned embodiments. Various changes can be made within the knowledge scope of those of ordinary skill in the art without departing from the gist of the present invention. In addition, the embodiments of the present invention and the features in the embodiments may be combined with each other without conflict.

Claims

A method for preparing a high-nickel ternary precursor, which is characterized by: including the following steps:

Add a metal salt, ammonia water and a precipitant to a bottom liquid containing a precipitant and ammonia water with an oxygen content of less than 1% respectively to perform a co-precipitation reaction to prepare the high-nickel ternary precursor;

The co-precipitation reaction is as follows: first, a protective gas is introduced to carry out the reaction, and then an oxygen-containing gas is introduced to react,

The temperature of the co-precipitation reaction is 25-40°C, and the ammonia concentration is 0.5-2.5g/L.
The method for preparing a high-nickel ternary precursor according to claim 1, characterized in that: in the bottom liquid, the pH is 10.5-11.0; the ammonia concentration is 0.5-2.5g/L; and the temperature is 25-40°C.
The preparation method of high-nickel ternary precursor according to claim 1, characterized in that: the metal salt is a metal salt solution, the addition flow rate of the metal salt solution is 100-800L/h, and the metal salt solution The total concentration of metal ions in the solution is 115-125g/L; the adding flow rate of the precipitating agent is 50-400L/h; the adding flow rate of the ammonia water is 1-100L/h; the adding metal salt, ammonia water and precipitating agent The time required for the steps is 60 to 70 hours.
The method for preparing a high-nickel ternary precursor according to claim 3, wherein the flow ratio of the protective gas to the metal salt solution is (2-3):1.
The method for preparing a high-nickel ternary precursor according to claim 3, wherein the flow ratio of the oxygen-containing gas to the metal salt solution is (0.1-0.5):1.
The method for preparing a high-nickel ternary precursor according to claim 4 or 5, characterized in that: in the co-precipitation reaction, the time required for introducing protective gas is 4 to 6 hours; the time required for introducing oxygen-containing gas It is 54~66h.
The method for preparing a high-nickel ternary precursor according to claim 1, wherein the pH of the co-precipitation reaction is 9.5-10.
A high-nickel ternary precursor, characterized in that it is prepared by the method described in any one of claims 1 to 7.
The high-nickel ternary precursor according to claim 8, characterized in that: in the precursor, the molar ratio of nickel element, cobalt element and manganese element is x:y:z, where, x+y+z= 100, 90≤x<98, 0<y<5, z>0.
Application of the high-nickel ternary precursor according to claim 8 or 9 in the field of lithium-ion batteries.