A manganese-lithium separation process and a pre-extraction solution preparation process in comprehensive recovery of ternary battery wastes, and a method for comprehensive recovery of cobalt, nickel, manganese and lithium elements from the ternary battery wastes, relates to a method for recycling battery wastes. According to the present disclosure, cobalt and nickel ions are separated from an impurity-removed solution by a hydrolysis method; manganese, lithium and other ions in the impurity-removed solution are free from an extraction procedure, so that most manganese ions are separated and removed by a wet method before extraction, to prevent the manganese ions from entering the extraction system; nickel ions are free from an extraction procedure of full extraction and full back-extraction; and nickel hydroxide is directly precipitated after related impurities are removed by extraction.

A method for recovering NiSO.sub.4.6H.sub.2O crystals from a nickel rich organic phase is provided. The method includes contacting a nickel rich organic phase with an aqueous strip solution of sufficient H.sub.2SO.sub.4 concentration to extract nickel from the organic phase and of sufficient Ni.sup.2+ concentration to precipitate NiSO.sub.4.6H.sub.2O crystals and form a nickel lean organic phase. Also provided are methods for recovering NiSO.sub.4.6H.sub.2O crystals that include preceding processing steps, including low temperature pressure oxidation (LTPOX) autoclaving of a nickel sulphide concentrate to afford a pregnant leach solution (PLS).

The present disclosure relates to a process for the recovery of transition metals from batteries comprising treating a transition metal material with a leaching agent to yield a leach which contains dissolved salts of nickel and/or cobalt, injecting hydrogen gas in the leach at a temperature above 100° C. and a partial pressure above 5 bar to obtain a nickel and/or cobalt precipitate in elemental form, and separating the obtained nickel and/or cobalt precipitate.

The present invention is a process for directly recovering lithium and valuable transition metals such as cobalt, nickel and manganese from waste cathode and anode powder of spent lithium ion batteries into high grade products through a cascade reduction reaction scheme, followed by digestion and precipitation circuit using CO.sub.2 as media, and a series of physical separation procedures.

Provided are: an alloy powder that can be obtained from a waste lithium ion battery, wherein the alloy powder can be dissolved in an acid solution and enables recovery of metals contained in the alloy powder; and a method for producing the alloy powder. This alloy powder contains Cu and at least one of Ni and Co as constituent components, wherein a portion having a higher concentration of the at least one of Ni and Co than the average concentration in the entire alloy powder is distributed on at least the surface, and the phosphorus grade is less than 0.1% by mass. The method for producing the alloy powder includes a powdering step for powdering a molten alloy using a gas atomization method, the molten alloy containing Cu and at least one of Ni and Co as constituent components and having a phosphorus grade of less than 0.1% by mass.

A method for processing lithium ion battery scrap includes a leaching step of leaching lithium ion battery scrap and subjecting the resulting leached solution to solid-liquid separation to obtain a first separated solution; an iron removal step of adding an oxidizing agent to the first separated solution and adjusting a pH of the first separated solution in a range of from 3.0 to 4.0, then performing solid-liquid separation and removing iron in the first separated solution to obtain a second separated solution; and an aluminum removal step of neutralizing the second separated solution to a pH range of from 4.0 to 6.0, then performing solid-liquid separation and removing aluminum in the second separated solution to obtain a third separated solution.

A method of selectively leaching a metal such as nickel from an ore or ore processing intermediate comprising the metal and cobalt. The ore or ore processing intermediate is contacted with an acidic leach solution comprising an amount of an oxidising agent sufficient to oxidise a major portion of the cobalt to thereby cause it to be stabilised in the solid phase while a major portion of the metal is dissolved for subsequent recovery.

A method for recovering NiSO.sub.4.6H.sub.2O crystals from a nickel rich organic phase is provided. The method includes contacting a nickel rich organic phase with an aqueous strip solution of sufficient H.sub.2SO.sub.4 concentration to extract nickel from the organic phase and of sufficient Ni.sup.2+ concentration to precipitate NiSO.sub.4.6H.sub.2O crystals and form a nickel lean organic phase. Also provided are methods for recovering NiSO.sub.4.6H.sub.2O crystals that include preceding processing steps, including low temperature pressure oxidation (LTPOX) autoclaving of a nickel sulphide concentrate to afford a pregnant leach solution (PLS).

A separation method for a separation target metal uses a metal ligand having an oxide of the separation target metal as a core. The separation method for the separation target metal includes a step of dispersing the metal ligand in a solution containing the separation target metal and separating the separation target metal in the solution as the oxide of the separation target metal. A metal coordination polymer includes: a metal oxide; and a ligand polymer that carries the metal oxide. The metal oxide is an oxide of any one, two, or more of cobalt, nickel, and manganese, and the ligand polymer is a copolymer of (1) an optionally substituted divinylbenzene and (2) acrylic acid or methacrylic acid.

A method for processing lithium ion battery scrap includes a leaching step of leaching lithium ion battery scrap and subjecting the resulting leached solution to solid-liquid separation to obtain a first separated solution; an iron removal step of adding an oxidizing agent to the first separated solution and adjusting a pH of the first separated solution in a range of from 3.0 to 4.0, then performing solid-liquid separation and removing iron in the first separated solution to obtain a second separated solution; and an aluminum removal step of neutralizing the second separated solution to a pH range of from 4.0 to 6.0, then performing solid-liquid separation and removing aluminum in the second separated solution to obtain a third separated solution.