Method for preparing nickel sulfate from nickel-iron-copper alloy

Patent metadata

Field	Value
Publication number	US-2023399240-A1
Application number	US-202218260238-A
Country	US
Kind code	A1
Filing date	Jun 6, 2022
Priority date	Jul 15, 2021
Publication date	Dec 14, 2023
Grant date	—

Abstract

Disclosed in the present invention is a method for preparing nickel sulfate from a nickel-iron-copper alloy. The method comprises: in a high-pressure oxygen environment, mixing a nickel-iron-copper alloy crushed material, aqueous ammonia, ammonium sulphate, and a corrosion assisting agent, leaching, then performing solid-liquid separation on the leached slurry, adding a precipitant into a filtrate, and performing ammonia distillation to obtain a nickel-containing leachate; then adding an extractant into the nickel-containing leachate to extract nickel so as to obtain a nickel-containing extraction organic phase; and then adding sulfuric acid into the nickel-containing extraction organic phase to perform back extraction of nickel so as to obtain a nickel sulfate solution. According to the present invention, the nickel-iron-copper alloy is separated by using different properties of nickel and iron, nickel is dissolved in a hexamine complex of nickel, iron cannot be dissolved and then continues to be remained in a solid, after the filtrate is collected, the precipitant is added and ammonia distillation is performed to remove copper, the aqueous ammonia is recycled, and the copper ions react with the precipitant to generate a copper sulfide precipitate, and thus, copper in the filtrate is removed, and the purity of nickel sulfate is further improved.

First claim

What is claimed is:

1 . A method for preparing nickel sulfate from a nickel-iron-copper alloy, comprising the following steps:
S 1 : mixing a crushed nickel-iron-copper alloy, ammonia water, ammonium sulfate and a corrosion aid in a high-pressure oxygen environment and performing leaching; the corrosion aid is at least one of ammonium sulfide, persulfate, or ammonium thiosulfate; a pressure of the leaching is 2.5 MPa to 4.0 MPa, and a temperature of the leaching is 50° C. to 65° C.; S 2 : performing a solid-liquid separation on a slurry obtained by the leaching in step S 1 to obtain a first filtrate and a first residue, adding a precipitant to the first filtrate, then distilling ammonia, and then performing filtration to obtain a nickel-containing leaching solution; and the precipitant is at least one of thiosulfate, sodium sulfide, or ammonium sulfide; and S 3 : adding an extractant into the nickel-containing leaching solution to extract nickel, allowing the system to stand and then separating to obtain a nickel-containing extracted organic phase, and then adding sulfuric acid into the nickel-containing extracted organic phase to perform a back extraction of nickel to obtain a nickel sulfate solution.

2 . The method according to claim 1 , wherein, in step S 2 , the method further comprises mixing the first residue with ammonia water, ammonium sulfate and a corrosion aid and performing second-stage leaching, then performing a solid-liquid separation to obtain a second residue and a second filtrate, and subjecting the second filtrate back to the leaching in step S 1 .

3 . The method according to claim 2 , wherein, in step S 2 , the method further comprises mixing the second residue with ammonia water, ammonium sulfate and a corrosion aid and performing third-stage leaching, then performing a solid-liquid separation to obtain a third residue and a third filtrate, subjecting the third filtrate back to the leaching in step S 1 or the second-stage leaching, and washing the third residue to obtain an iron dreg.

4 . (canceled)

5 . The method according to claim 1 , wherein, in step S 1 , a molar ratio of nitrogen in ammonia water to ammonium sulfate is (0.1-20):1; and a total molar concentration of nitrogen in ammonia water and ammonium sulfate is 8 mol/L to 15 mol/L.

6 . (canceled)

7 . (canceled)

8 . The method according to claim 2 , wherein, a pressure of the second-stage leaching is 3.5 MPa to 6.0 MPa, and a temperature of the second-stage leaching is 60° C. to 75° C.

9 . The method according to claim 3 , wherein, a pressure of the third-stage leaching is MPa to 7.0 MPa, and a temperature of the third-stage leaching is 70° C. to 85° C.

10 . The method according to claim 1 , wherein, in step S 3 , the extractant is at least one of P204, P507, DEHPA or Cyanex272.

Assignees

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

Inventors

• Yu Haijun
• Xie Yinghao
• Li Aixia
• Zhang Xuemei
• Li Changdong

Classifications

• Y02P10/20

  Recycling · CPC title

• C22B3/3846

  Phosphoric acid, e.g. (O)P(OH)3 · CPC title

• C22B3/3842

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

• C22B23/0446

  with an ammoniacal liquor or with a hydroxide of an alkali or alkaline-earth metal · CPC title

• C22B15/00

  Obtaining copper · CPC title