METHOD FOR MANUFACTURING A PRECURSORY ACTIVE MATERIAL FOR A POSITIVE ELECTRODE

Claims

1. A method for producing a precursor of a positive electrode active material using a batch reactor, the method comprising the following steps: (S1) formation of the precursor nucleus; (S2) growth of the nucleus formed in stage S1; (S3) additional growth of the nucleus grown in stage S2; and (S4) additional growth of the nucleus grown at stage S3, in this case, the mixing speed in the reactor with periodic loading is set as follows: 200-900 rpm during stage S2, 800 rpm or less during stage S3, and 700 rpm or less during stage S4, and the reaction solution is designed to overflow when the batch reactor is filled with it.

2. The method according to claim 1, characterized in that the coprecipitation reaction is carried out for 1-20 hours at step S2.

3. The method according to claim 1, characterized in that the precursor has an average particle size D 50 6.5-13.0 µm after completion of stage S3.

4. The method according to claim 1, characterized in that the stirring speed inside the reactor with periodic loading during stage S1 is 250-1000 rpm.

5. The method according to paragraph 1, characterized in that the complex solution of the transition metal is fed into the reactor with periodic loading at the following flow rate: 5-40 ml / min during stages S2 and S3, and 2-30 ml / min during stage S4.

6. The method according to claim 5, characterized in that the complex solution of the transition metal contains at least one element selected from the group consisting of nickel, cobalt and manganese.

7. The method according to paragraph 5, characterized in that the complex solution of the transition metal contains: nickel in the amount of 60-96 mol.%; cobalt in an amount of 0-20 mol.%; and manganese in the amount of 4-40 mol.%.

8. The method according to paragraph 1, characterized in that the nitrogen-containing complex solution is supplied at the following flow rate: 1.0-10.0 ml / min during stages S2 and S3, and 1.2-8.0 ml / min during stage S4.

9. The method according to paragraph 1, characterized in that the main complex solution is supplied at the following flow rate: 3-35 ml / min during stages S2 and S3, and 2-30 ml / min during stage S4.

10. The method according to claim 1, characterized in that the reaction solution in the batch reactor has a pH of 10.5-13.5 at step S1.

11. The method according to claim 1, characterized in that the reaction solution in the reactor with periodic loading has a pH of 10.5-13.0 at stages S2, S3 and S4.

12. The method according to claim 1, characterized in that the reaction solution in the batch reactor has an ammonia concentration of 3000-7000 ppm at stages S2, S3 and S4.

13. The method according to claim 1, characterized in that the reaction solution in the batch reactor has a residual nickel concentration of 250 ppm or less in steps S2, S3 and S4.

14. The method according to claim 1, characterized in that the positive electrode active material precursor generated in steps S1-S4 has a Span value of 0.38 or less, measured according to equation 1 below: Span = (particle size D 90 - particle size D 10 ) / average particle size D 50 . [Equation 1] 15. The method according to claim 1, characterized in that it further includes the step (S5) of washing and drying the precursor of the active material of the positive electrode obtained in steps S1-S4.