Method for recycling battery by incomplete extraction

Patent metadata

Field	Value
Publication number	US-11920213-B2
Application number	US-202118246671-A
Country	US
Kind code	B2
Filing date	Apr 30, 2021
Priority date	Oct 29, 2020
Publication date	Mar 5, 2024
Grant date	Mar 5, 2024

Abstract

Disclosed is an incomplete extraction method for recycling batteries, which may include: introducing a pretreatment gas into a device loaded with a waste battery powder, and bringing a gas outlet into communication with absorption liquid A and absorption liquid B in order; raising the temperature and introducing the pretreatment gas; reducing the temperature and introducing a reaction gas; raising the temperature, introducing the reaction gas, and then introducing the pretreatment gas; and reducing the temperature, and turning off the pretreatment gas; adding an extractant to absorption liquid A, mixing the mixture, taking organic phase A, adding a stripping agent, and taking aqueous phase A; and adjusting the pH to acidity, then adding an extractant, taking organic phase B, adding a stripping agent to obtain a stock solution enriched in Li, Mn, Ni and Co.

First claim

The invention claimed is:

1. A method for recycling a battery by incomplete extraction, characterized by comprising:
(1) subjecting waste batteries to discharging, crushing, and pyrolysis to obtain a waste battery powder;
(2) introducing a pretreatment gas into a device loaded with the waste battery powder, and bringing a gas outlet of the device into communication with absorption liquid A and absorption liquid B in order;
(3) performing the following operations on the device loaded with the waste battery powder: raising the temperature and continuing to introduce the pretreatment gas; reducing the temperature and introducing a reaction gas; raising the temperature, introducing the reaction gas, and then introducing the pretreatment gas; and reducing the temperature, and turning off the pretreatment gas;
(4) adding a first extractant to absorption liquid A, mixing the mixture, carrying out liquid separation, taking organic phase A, adding a first stripping agent for liquid separation, and taking aqueous phase A; and
(5) adjusting the pH of aqueous phase A to acidity, then adding a second extractant for liquid separation, taking organic phase B, adding a second stripping agent for liquid separation to obtain a stock solution enriched in Li, Mn, Ni and Co;
wherein the pretreatment gas is at least one of nitrogen, helium, argon or neon; the reaction gas is one of chlorine gas, fluorine gas or bromine gas; absorption liquid A is an acid solution, the acid solution is HCl; and absorption liquid B is an alkaline solution, the alkaline solution is a NaOH or KOH solution; wherein, in step (4), the first extractant is [(CH 3 ) 3 C(CH 2 ) 5 CH(CH 3 )CH 2 ]HPO 2 and the first stripping agent is diethylenetriamine pentaacetic acid; in step (5), the second extractant is [CH 3 (CH 2 ) 4 CH(CH 3 )CH 2 ] 2 HPO 2 and the second stripping agent is triethylenetetraamine hexaacetic acid.

2. The method of claim 1 , wherein, in step (2), the introduced pretreatment gas has a flow rate of 10-30 mL/min and a temperature of 20-40° C.

3. The method of claim 1 , wherein, the specific operation of step (3) involves: raising the temperature to 300-400° C. at a ramp rate of 3-5° C./min, maintaining the flow rate, continuing to introduce the pretreatment gas for 20-60 min, and maintaining the gas flow rate; reducing the temperature to 20-40° C. and then introducing the reaction gas at a flow rate of 10-50 mL/min; raising the temperature to 200-240° C. at a ramp rate of 3-5° C./min, maintaining the temperature and introducing the reaction gas for 1-3 h; raising the temperature to 280-320° C. at a ramp rate of 3-5° C./min, maintaining the temperature and introducing the reaction gas for 2-3 h; further raising the temperature to 360-380° C. at a ramp rate of 3-5° C./min, maintaining the temperature and introducing the reaction gas for 1-3 h; and finally raising the temperature to 450-470° C. at a ramp rate of 3-5° C./min, maintaining the temperature, introducing the reaction gas for 2-4 h, turning off the reaction gas, introducing the pretreatment gas, and reducing the temperature to 20-35° C.

4. The method of claim 1 , wherein, in step (4), the volume ratio of absorption liquid A to the first extractant is 1:(1-5); and in step (4), the volume ratio of organic phase A to the first stripping agent is 1:(1-5).

5. The method of claim 1 , wherein, in step (5), the volume ratio of organic phase B to the second stripping agent is 1:(1-5).

6. Use of the method of claim 1 in metal recovery.

Assignees

• Guangdong Brunp Recycling Technology Co Ltd
• Hunan Brunp Recycling Tech Co Ltd
• Hunan Brunp Ev Recycling Co Ltd

Inventors

• Yu Haijun
• Peng Ting
• Xie Yinghao
• Zhang Xuemei

Classifications

• C22B3/3842 Primary

  Phosphinic acid, e.g. H2P(O)(OH) · CPC title

• C22B1/02

  Roasting processes (C22B1/16 takes precedence) · CPC title

• C22B1/24

  Binding; Briquetting {; Granulating} · CPC title

• C22B7/006 Primary

  Wet processes · CPC title

• C22B23/0453

  Treatment or purification of solutions, e.g. obtained by leaching (C22B23/0407 takes precedence) · CPC title