JP2022042982A - Method for separating cobalt and nickel - Google Patents

Abstract

To enable cobalt and nickel to be recovered from a lithium ion secondary battery at a low cost.SOLUTION: A method for separating cobalt and nickel comprises: a heat treatment step of heating a lithium ion secondary battery thereby performing heat treatment; a grinding and sorting step of grinding and sorting the lithium ion secondary battery after the heat treatment, thereby obtaining an electrode material including at least cobalt, nickel, copper and lithium; a leaching step of immersing the electrode material in treatment solution including sulfuric acid and hydrogen peroxide thereby obtaining leachate; a copper separation step of adding hydrogen sulfide compound to the leachate and stirring the solution, and then performing solid-liquid separation thereby obtaining elution solution including cobalt and nickel and residue including copper sulfide; and a cobalt/nickel separation step of adding alkali metal hydroxide to the elution solution and performing pH adjustment, and then adding hydrogen sulfide compound and stirring the liquid, and performing solid-liquid separation, thereby obtaining a sediment including cobalt sulfide and nickel sulfide and residual liquid including lithium.SELECTED DRAWING: Figure 1

Description

The present invention relates to a method for separating cobalt and nickel, which enables accurate separation and recovery of cobalt and nickel contained in a lithium ion secondary battery from other metals.

Lithium-ion secondary batteries are used as power sources in a wide range of fields, from small ones such as various electronic devices to large ones such as electric vehicles. When such a lithium ion secondary battery is discarded, it is required to recover and reuse useful metals.

In a lithium ion secondary battery, a negative electrode material and a positive electrode material are separated by a separator such as porous polypropylene and layered, and aluminum or stainless steel is used together with an electrolyte such as lithium hexafluorophosphate (LiPF ₆ ) and an electrolytic solution. It is formed by enclosing it in a case such as.

The negative electrode material of a lithium ion secondary battery is formed by applying a negative electrode active material such as graphite mixed with a binder to a negative electrode current collector made of copper foil or the like. Further, the positive electrode material is formed by applying a positive electrode active material such as lithium manganate, lithium cobalt oxide, or lithium nickel oxide mixed with a binder to a positive electrode current collector made of aluminum foil or the like.

As described above, the positive electrode active material of the lithium ion secondary battery contains a large amount of cobalt and nickel, but the positive electrode active material previously crushed and separated in the recycling process includes manganese, copper, in addition to cobalt and nickel. Contains aluminum, lithium, etc. Therefore, in order to separate and recover cobalt and nickel from the lithium ion secondary battery in high yield, it is necessary to accurately remove metals other than these.

Conventionally, as a method for separating and recovering cobalt and nickel contained in a lithium ion secondary battery, for example, Patent Documents 1 and 2 describe lithium ion as a method for recovering a valuable metal from a used lithium ion secondary battery. A recovery method is disclosed in which a positive electrode material active material is taken out from a secondary battery, a leachate in which a metal is leached out from the positive electrode active material by acid leaching is obtained, and cobalt and nickel are separated from the leachate by solvent extraction.

Japanese Unexamined Patent Publication No. 2016-113672 Japanese Unexamined Patent Publication No. 2016-186118

In the recovery method disclosed in Patent Documents 1 and 2, as a method for removing impurity elements, a precipitate containing a hydroxide is formed by adding an oxidizing agent or adjusting the pH to perform solid-liquid separation. However, at this time, cobalt and nickel and other metals (copper, aluminum, manganese, iron, etc.) are removed at the same time, so that cobalt and nickel and other metals are separated in the subsequent multiple steps. There is a problem that the separation process is complicated and time-consuming, and the recovery of cobalt and nickel is expensive.

The present invention has been made in view of the above-mentioned circumstances, in which cobalt and nickel contained in a lithium ion secondary battery and other metals are separated with high accuracy in a small number of steps, and the lithium ion secondary battery is used. It is an object of the present invention to provide a method for separating cobalt and nickel capable of recovering cobalt and nickel from a secondary battery at low cost.

In order to solve the above problems, the present invention is a method for separating cobalt and nickel from a lithium ion secondary battery, wherein the lithium ion secondary battery is crushed and classified, and at least copper is used. , A crushing and sorting step to obtain an electrode material containing nickel, copper, and lithium, a leaching step of immersing the electrode material in a treatment liquid containing sulfuric acid and hydrogen peroxide to obtain a leachate, and stirring by adding a hydrogen sulfide compound to the leachate. After that, solid-liquid separation is performed to obtain an eluent containing cobalt and nickel and a residue containing copper sulfide. Copper separation step, alkali metal hydroxide is added to the eluate to adjust the pH, and then hydrogen sulfide is used. It is characterized by comprising a cobalt-nickel separation step of adding a compound, stirring and solid-liquid separation to obtain a precipitate containing cobalt sulfide and nickel sulfide and a residual liquid containing lithium.

According to the present invention, a metal component is eluted from the electrode material with a treatment liquid containing sulfuric acid and hydrogen peroxide, a water-soluble hydrogen sulfide compound is added to the obtained leachate, and the mixture is stirred to contain the metal contained in the leachate. Of the components, only copper is selectively precipitated as an insoluble sulfide and separated. Then, after adjusting the pH, a water-soluble hydrogen sulfide compound is added and stirred to selectively precipitate only cobalt and nickel among the metal components contained in the eluent as insoluble sulfides. Cobalt and nickel can be separated from the lithium ion secondary battery with high accuracy in a small number of steps.

Further, in the present invention, a heat treatment step of heating the lithium ion secondary battery to perform a heat treatment may be provided before the crushing and sorting step.
Further, a redissolving solution containing sulfuric acid is added to the precipitate separated in the cobalt-nickel separation step, and the mixture is stirred and then solid-liquid separated to obtain a cobalt-nickel solution containing cobalt and nickel. A solvent extraction step may be provided in which an extractant solution is added to the cobalt-nickel solution to obtain a cobalt extract and a nickel extract.

Further, in the present invention, in the redissolution step, the immersion time of the precipitate in the redissolution solution may be 1 hour or more.

Further, in the present invention, in the leaching step, the liquid temperature of the treatment liquid may be 60 ° C. or higher and the sulfuric acid concentration may be 2 mol / L or higher.

Further, in the present invention, in the copper separation step, the pH of the leachate is maintained at 1.0 or less from the start to the end of the addition of the hydrogen sulfide compound, and the oxidation / reduction potential (vs Ag / AgCl). An aqueous solution of sodium hydrogen sulfide may be added as the hydrogen sulfide compound until the pH becomes 0 mV or less.

Further, in the present invention, in the cobalt-nickel separation step, an aqueous solution of sodium hydrogen sulfide is used as the hydrogen sulfide compound, and the pH of the eluent from the start to the end of addition of the hydrogen sulfide compound is 2.0. The hydrogen sulfide compound may be added to the eluent until the oxidation / reduction potential (vs Ag / AgCl) is −400 mV or less while maintaining the range of about 5.0.

Further, in the present invention, the pH of the eluate from the start to the end of the addition of the hydrogen sulfide compound may be maintained within the range of 2.0 to 3.5.

Further, in the present invention, in the pH adjustment in the cobalt / nickel separation step, the pH of the eluate may be adjusted in the range of 3.0 to 4.0.

Further, in the present invention, in the re-dissolution step, the precipitate is dissolved in the re-dissolution solution containing sulfuric acid and hydrogen peroxide solution, or the precipitate is added to the re-dissolution solution containing sulfuric acid, and then the precipitate is added. It may be dissolved by performing air bubbling.

Further, in the present invention, in the redissolving step, the liquid temperature of the redissolving solution may be 60 ° C. or higher and the sulfuric acid concentration may be 0.5 mol / L or higher.

Further, the present invention may include a heat treatment step of heating the lithium ion secondary battery to perform a heat treatment as a pre-step of the crushing and sorting step.

According to the present invention, cobalt and nickel contained in a lithium ion secondary battery and other metals are separated with high accuracy in a small number of steps, and cobalt and nickel can be recovered from the lithium ion secondary battery at low cost. It is possible to provide a method for separating cobalt and nickel that can be used.

It is a flowchart which showed the recycling method of the electrode material of the lithium ion secondary battery including the separation method of cobalt and nickel of this invention step by step.

Hereinafter, a method for separating cobalt and nickel according to an embodiment of the present invention will be described with reference to the drawings. It should be noted that each of the embodiments shown below is specifically described in order to better understand the gist of the invention, and is not limited to the present invention unless otherwise specified.

FIG. 1 is a flowchart showing a stepwise recycling method of an electrode material of a lithium ion secondary battery including the method for separating cobalt and nickel of the present invention.

(Heat treatment step S1)
As a pretreatment step for separating the electrode material constituting the discarded lithium ion secondary battery (hereinafter referred to as waste LIB), the waste LIB is heated in a heating furnace, for example, with superheated steam to about 500 ° C. for heat treatment. ..

The heat treatment may be vacuum or normal pressure, but heating in an oxygen-free inert atmosphere is preferable. The waste LIB has a large adhesive force between the positive electrode active material and the negative electrode active material and the aluminum foil and the copper foil which are the current collectors due to the presence of the binder and the electrolytic solution. Therefore, by performing a heat treatment step of 400 ° C. or higher, the separation between these active materials and the current collector is facilitated. By setting the heating temperature of the waste LIB to 650 ° C. or lower, it is possible to prevent aluminum from melting, entraining the active material, cooling and solidifying, and making it difficult to take out only the active material.

(Crushing and sorting step S2)
Next, after pulverizing the waste LIB after heat treatment, the electrode material is sorted and separated by sieving. The waste LIB is crushed by using, for example, a twin-screw shear crusher or a hammer mill.

Then, the crushed waste LIB is classified using a sieve having an appropriate opening, and the positive electrode active material (LiCoO ₂ , etc.) and the negative electrode active material are classified by using a battery container, an aluminum foil, a copper foil, and a nickel terminal as a sieve. The electrode material containing (graphite) is recovered as a product of the sieve. Such an electrode material may be, for example, a material that has passed through a sieve having an opening of about 0.5 mm.

The separated electrode material mainly contains the constituent materials of the positive electrode active material and impurities such as cobalt, nickel, manganese, copper, iron, aluminum, lithium and calcium, and carbon which is a constituent material of the negative electrode active material. There is.

(Leaching step S3)
Next, the electrode material separated in the pulverization and sorting step S2 is immersed in the treatment liquid to obtain a leachate. As the treatment liquid, a mixture of sulfuric acid (H ₂ SO ₄ ) and hydrogen peroxide (H ₂ O ₂ ) is used.

Co and Ni contained in the waste LIB also contain trivalent and tetravalent states that are difficult to dissolve in sulfuric acid. Therefore, by using hydrogen peroxide as a reducing agent, divalent Co and Ni that are more easily dissolved in sulfuric acid can be obtained. Can be reduced.
As an example of the treatment liquid, 100 ml of dilute sulfuric acid having a concentration of 2 mol / L or more is mixed with hydrogen peroxide solution having a concentration of 30 wt% at a ratio of 5 ml or more. By setting the concentration of dilute sulfuric acid to 2 mol / L or more and the addition amount of hydrogen peroxide solution to 5 ml or more, the leaching rate of cobalt and nickel can be increased. Although there is no particular limitation, the upper limit of the sulfuric acid concentration is 18 mol / L and the upper limit of the amount of hydrogen peroxide solution added is 30 ml because further improvement in the leaching rate cannot be expected.

As a specific example of the leaching step S3, for example, the powdery electrode material separated in the pulverizing and sorting step S2 is added to the treatment liquid heated to 60 ° C. or higher, and the mixture is immersed for 4 hours or more. At this time, it is preferable to further stir.
By setting the treatment liquid temperature to 60 ° C. or higher and the leaching (immersion) time to 4 hours or longer, the leaching rate of cobalt and nickel can be increased. Although there is no particular limitation, the upper limit of the treatment liquid temperature is 90 ° C. and the upper limit of the leaching time is 15 hours because further improvement in the leaching rate cannot be expected.
By such leaching step S3, among the electrode materials, the metal components derived from the positive electrode active material (cobalt, nickel, manganese, copper, iron, aluminum, lithium, calcium, etc.) are dissolved in the treatment liquid, and the carbon derived from the negative electrode active material is dissolved. , Does not dissolve and remains as a carbon residue.

(Copper Separation Step S4)
Next, a hydrogen sulfide compound is added to the leachate obtained in the leachation step S3, and the mixture is stirred and then solid-liquid separated to obtain an eluent containing cobalt and nickel and a residue containing copper sulfide (CuS).

In the present invention, the hydrogen sulfide compound means a compound containing sulfur and having the sulfur content in the form of _H2S , ^{HS- or} S2- when dissolved in water.
As the hydrogen sulfide compound used in the copper separation step S4, a water-soluble alkali metal hydride is used, and in this embodiment, an aqueous solution of sodium hydrogen sulfide (NaSH) is used. As a specific example of the copper separation step S4, after diluting the leachate with ion-exchanged water, an aqueous solution of sodium hydrogen sulfide is added to the diluted leachate and stirred.

The addition of the aqueous solution of sodium hydrogen sulfide is carried out, for example, until the oxidation / reduction potential (vs Ag / AgCl) becomes 0 mV or less. By adding sodium hydrogen sulfide until the oxidation / reduction potential becomes 0 mV or less, almost all of the copper contained in the leachate can be precipitated.
It is preferable to maintain the pH of the leachate from the start to the end of the addition of the hydrogen sulfide compound to 1.0 or less. If the pH of the leachate exceeds 1.0, sulfides of cobalt and nickel may be generated, and the recovery rate of these eluates may decrease.
The hydrogen sulfide compound may be, for example, sodium sulfide, sodium thiosulfate, or sodium dithionite, in addition to sodium hydrogen sulfide.

By adding the hydrogen sulfide compound to the leachate, copper and sulfur among the metal components dissolved in the leachate react with each other to generate copper sulfide (CuS) and precipitate. On the other hand, the metal components (cobalt, nickel, manganese, iron, aluminum, lithium, calcium, etc.) excluding copper remain in the liquid phase, and an eluent containing cobalt and nickel can be obtained.

After that, by solid-liquid separation using a filter medium or the like, the solid phase consisting of the carbon residue generated in the leaching step S3 and the residue generated in the copper separation step S4 and the eluate (liquid phase) are separated.

In the present embodiment, the carbon residue generated in the leaching step S3 is also filtered off by the solid-liquid separation in the copper separation step S4, but the copper separation step S4 is performed by performing the solid-liquid separation also in the leaching step S3. It is also possible to separate the carbon residue in advance before performing this.

Further, in the copper separation step S4, before performing solid-liquid separation, the pH of the leachate is set to about 3.0 to 4.0 using sodium hydroxide (NaOH), and the aluminum contained in the leachate is aluminum hydroxide (aluminum hydroxide). It can also be precipitated in Al (OH) ₃ ) and separated from the leachate by solid-liquid separation together with the carbon residue and the residue.

The separated solid phase may be treated as waste after being repulped (purified by adding water to the solid phase, resuspending it, and then dehydrating it).

(Cobalt / Nickel Separation Step S5)
Next, after adjusting the pH by adding an alkali metal hydroxide to the eluent, a hydrogen sulfide compound is added and stirred to perform solid-liquid separation. A precipitate containing cobalt sulfide and nickel sulfide and a residual liquid containing lithium. And get.

Examples of the alkali metal hydroxide for adjusting the pH of the eluent in the initial stage of the cobalt-nickel separation step S5 include sodium hydroxide (NaOH) and potassium hydroxide (KOH). In this embodiment, a 25 wt% sodium hydroxide aqueous solution was used.
By such pH adjustment, the pH of the eluate is set in the range of 3.0 to 4.0, for example, 3.5.

At this time, if the pH is low, the hydrogen sulfide compound may not easily react with cobalt and nickel, but the pH of the eluent decreases with the addition of the hydrogen sulfide compound. If the pH at the start of the addition of the hydrogen sulfide compound is less than 3.0 after the pH adjustment, an excessive pH drop occurs before the end of the addition of the hydrogen sulfide compound, and the pH adjustment needs to be performed again. Therefore, it is more efficient to set the pH to 3.0 or higher at the time of pH adjustment, which is a pretreatment for sulfurization.
Further, if the pH is set to a value exceeding 4.0 at the time of pH adjustment, it takes time to adjust the pH, but it is inefficient because the pH becomes 4.0 or less immediately after the addition of the hydrogen sulfide compound. Therefore, the pH adjustment range is preferably in the range of 3.0 to 4.0.

By adding a water-soluble hydrogen sulfide compound to the pH-adjusted eluate, the cobalt and nickel contained in the eluent become water-insoluble cobalt sulfide (CoS) and nickel sulfide (NiS), respectively. Precipitate.

Examples of the hydrogen sulfide compound for sulfurizing cobalt / nickel include water-soluble alkali metal sulfide compounds. The hydrogen sulfide compound may be the same as that used in the copper separation step S4, or may be different. In this embodiment, an aqueous solution of sodium hydrogen sulfide having a concentration of 250 g / L was used.
The addition of the aqueous solution of sodium hydrogen sulfide is carried out, for example, until the oxidation / reduction potential (vs Ag / AgCl) becomes −400 mV or less. By adding sodium hydrosulfide until the oxidation / reduction potential becomes −400 mV or less, almost all of the cobalt and nickel contained in the eluate can be precipitated.

The pH of the leachate from the start to the end of the addition of the hydrogen sulfide compound is preferably maintained in the range of 2.0 to 5.0, preferably 2.0 to 3.5. When the pH of the leachate is less than 2.0, a reaction between sodium hydrogen sulfide and sulfuric acid (NaSH + H ₂ SO ₄ → H ₂ S + Na ₂ SO ₄ ) occurs, sodium hydrogen sulfide is consumed, and cobalt and nickel are sulfurized. It becomes difficult to proceed. On the other hand, if the pH of the leachate exceeds 5.0, hydroxides of other metals may be generated and the purity of the precipitate may decrease. Also, it is difficult to control the pH in the high range.

The cobalt sulfide referred to here may contain cobalt sulfide compounds having various compositions such as cobalt sulfide (II), cobalt disulfide (CoS ₂ ), and cobalt octasulfide (Co ₉ S ₈ ). Similarly, nickel sulfide (NiS) has various compositions such as nickel sulfide (II), nickel disulfide (NiS ₂ ), trinickel tetrasulfide (Ni ₃ S ₄ ), and trinickel disulfide (Ni ₃ S ₂ ). Nickel sulfide compound may be contained.

On the other hand, metal components (manganese, iron, aluminum, lithium, calcium, etc.) excluding cobalt and nickel remain in the liquid phase (residual liquid) after the addition of the hydrogen sulfide compound. The liquid phase obtained here can be separated and recovered from manganese, iron, aluminum, lithium, calcium and the like contained therein by solvent extraction or the like by adjusting the pH.

(Redissolution step S6)
Next, a redissolved solution containing sulfuric acid is added to the precipitate obtained in the cobalt-nickel separation step S5 and stirred, and then solid-liquid separation is performed to obtain a cobalt-nickel solution containing cobalt and nickel.

As the resolving solution, for example, a mixture of sulfuric acid and hydrogen peroxide as an oxidizing agent is used. An example of the redissolved solution is a mixture of 100 ml of dilute sulfuric acid having a concentration of 1.5 mol / L and 20 ml of hydrogen peroxide solution having a concentration of 30 wt%.

As a specific example of the redissolving step S6, for example, a precipitate is added to the redissolving solution heated to 60 ° C. or higher, and the mixture is immersed for 4 hours or longer. At this time, it is preferable to further stir. It is also possible to perform air bubbling when immersing the precipitate without adding hydrogen peroxide solution to the redissolution solution.
At this time, the dissolution rate of cobalt and nickel can be increased by setting the treatment liquid temperature to 60 ° C. or higher and the leaching time to 1 hour or longer. Although there is no particular limitation, the upper limit of the treatment liquid temperature is 90 ° C. and the upper limit of the leaching time is 15 hours because further improvement in the dissolution rate cannot be expected.

Cobalt and nickel are dissolved in the redissolved solution by treating the precipitate with such a redissolved solution. In addition, impurities that do not dissolve in the redissolution solution, elemental sulfur generated in the cobalt / nickel separation step S5, and the like remain as a solid phase. After that, solid-liquid separation is performed using a filter medium or the like to obtain a (purified) cobalt-nickel solution in which the purity of cobalt and nickel is increased.

The cobalt-nickel solution thus obtained contains almost no other components (copper, iron, aluminum, lithium, calcium, etc.) of the electrode material other than cobalt and nickel, and high-purity recovery of cobalt and nickel. Suitable as a raw material.

As a pre-step of the redissolution step S6, it is also preferable to remove impurities other than cobalt sulfide and nickel sulfide by repulping the precipitate.
The procedure for removing aluminum before performing solid-liquid separation in the copper separation step S4 has been described above, but if such a procedure is not performed, the precipitate may contain an aluminum compound. In this case, the aluminum compound can be removed by repulping the precipitate.

(Solvent extraction step S7)
Next, an extractant solution is added to the cobalt-nickel solution obtained in the redissolution step S6 to obtain a cobalt extract and a nickel extract.
As the extractant solution, a mixed solution in which a metal extractant and a diluent are mixed can be used. For example, a mixed solution in which 2-ethylhexyl 2-ethylhexylphosphonate (PC88A: manufactured by Daihachi Chemical Co., Ltd.) is mixed at a ratio of 20 vol% and kerosene (diluent) at a ratio of 80 vol% can be used.

Using the above-mentioned extractant solution, the cobalt-nickel solution is separated and recovered as a cobalt sulfate (CoSO ₄ ) solution and a nickel sulfate (NiSO ₄ ) solution by a mixer settler.

By the above steps, cobalt and nickel can be recovered from the waste LIB in high yield. For example, when the amounts of cobalt and nickel in the electrode material taken out from the waste LIB are 100% each, cobalt and nickel are recovered in high yields of 95% or more by the method for separating cobalt and nickel of the present embodiment. can do.

Although the embodiments of the present invention have been described above, these embodiments are presented as examples and are not intended to limit the scope of the invention. These embodiments can be implemented in various other embodiments, and various omissions, replacements, and changes can be made without departing from the gist of the invention. These embodiments and variations thereof are included in the scope of the invention described in the claims and the equivalent scope thereof, as are included in the scope and gist of the invention.

The effect of the cobalt and nickel separation method of the present invention was verified.
(Procedure of the Example of the Present Invention)
14.5 g of the electrode material taken out from the waste LIB was added to a treatment solution containing 100 mL of sulfuric acid having a concentration of 2 mol / L and 5 mL of a hydrogen peroxide solution having a concentration of 30%, and the mixture was heated and stirred at a solution temperature of 60 ° C. for 4 hours (leaching step). ). After that, the solution was allowed to cool to room temperature, and the sodium hydrogen sulfide aqueous solution was stirred and dissolved in ion-exchanged water so as to reach 250 g / L of the leachate. The oxidation / reduction potential (ORP) of the leachate was 0 mV (vs Ag / AgCl) or less. It was added and stirred until it became (copper separation step).

At this stage, the carbon of the negative electrode material of the waste LIB, which is insoluble at the time of sulfuric acid leaching, and the generated residue (copper sulfide) were filtered to perform solid-liquid separation. To the eluate obtained here, a sodium hydroxide solution having a concentration of 25 wt% was added to adjust the pH to 3.5, and a sodium hydrogen sulfide aqueous solution having a concentration of 250 g / L was added to the pH at -400 mV (vs). Ag / AgCl) The mixture was stirred while being added until the concentration became less than or equal to.

Then, after confirming that a black precipitate (cobalt sulfide, nickel sulfide) was sufficiently produced, the precipitate was recovered by performing solid-liquid separation (cobalt-nickel separation step). On the other hand, impurities such as manganese, aluminum, iron, lithium, and calcium remained in the residual liquid, and the liquid was disposed of as a metal-containing waste liquid.

The precipitate was added to a redissolution solution of 100 mL of sulfuric acid having a concentration of 1.5 mol / L and 20 mL of hydrogen peroxide solution having a concentration of 30 wt%, heated at a solution temperature of 60 ° C., and stirred for 1 hour (redissolution step). ). Then, after allowing to cool to room temperature, the undissolved component and the elemental sulfur produced by the reaction in the previous step were removed by filtration.

From the cobalt-nickel solution thus obtained, the metal extractor PC88A (manufactured by Daihachi Chemical Co., Ltd.) was mixed at a ratio of 20 vol% and kerosine at a ratio of 80 vol%, and a mixer settler was used. The solution was separated and recovered as a cobalt sulfate solution and a nickel sulfate solution (solvent extraction step).

In the above procedure of the example of the present invention, when cobalt and nickel in the electrode material taken out from the waste LIB are 100%, the cobalt obtained in the back extract by solvent extraction is 96.4%, and the nickel is 95. It was 3%. Therefore, it was confirmed that the cobalt and nickel separation method of the present embodiment can recover cobalt and nickel from the waste LIB with a high yield.
The metal concentration was measured by ICP-AES, the pH was measured by a pH meter, and the ORP was measured by an ORP meter. The% value is based on mass.

(Leaching process)
Regarding the leaching step of the above-mentioned example of the present invention, the leaching rate of cobalt and nickel into the liquid phase was determined for Experimental Examples 1 to 9 in which the concentration of the treatment liquid, the amount of the hydrogen peroxide solution, the temperature, and the leaching time were changed with each other. It was measured. The results are shown in Table 1.

According to the results shown in Table 1, it was confirmed from Experimental Examples 1 to 3 that the sulfuric acid concentration of the treatment liquid was preferably 2 mol / L or more. Further, from Experimental Examples 3 to 5, it was confirmed that the amount of the hydrogen peroxide solution of the treatment liquid is preferably 5 mL (at a concentration of 30 wt%) or more. Further, from Experimental Examples 3, 6 and 7, it was confirmed that the temperature (liquid temperature) of the treatment liquid is preferably 60 ° C. or higher. Further, from Experimental Examples 5, 8 and 9, it was confirmed that the leaching time is preferably 4 hours or more.

(Copper separation process)
Next, regarding the copper separation step of the above-mentioned example of the present invention, an aqueous sodium hydrogen sulfide solution was added to the leachate obtained in Experimental Example 5, and changes in pH, ORP, and metal concentration in the leachate were investigated. In Experimental Example 10, measurement was carried out for the leachate before addition. The addition and measurement of the aqueous sodium hydrogen sulfide solution were repeated, and the process was terminated when the ORP became 0 mV or less (Experimental Examples 11 to 13). The pH measurement is continuously carried out from the start of the addition of the sodium hydrosulfide aqueous solution, and when the pH stabilizes after each addition, the pH at that time and the elapsed time from the start of the first addition are recorded. , Other items were measured.
The results are shown in Table 2.

According to the results shown in Table 2, if the hydrogen sulfide compound is added until the ORP becomes 0 mV or less while maintaining the pH of the leachate at 1.0 or less, almost all of the copper contained in the leachate is precipitated, and nickel and cobalt are deposited. It was confirmed that solid-liquid separation was possible with other components such as.

(Cobalt / nickel separation process)
Next, regarding the cobalt-nickel separation step of the above-mentioned example of the present invention, the influence of the pH of the eluate during the addition of the hydrogen sulfide compound on the reaction was investigated.
[PH 2.0-3.0]
In Experimental Example 14, the eluate obtained in Experimental Example 13 was used, and the eluate before addition was measured. Next, a pH-adjusted solution was measured by adding an aqueous sodium hydroxide solution (Experimental Example 15). After that, the addition and measurement of the aqueous sodium hydrogen sulfide solution were repeated (Experimental Examples 16 to 23). In order to maintain the pH during the addition in the range of 2.0 to 3.0, an aqueous sodium hydroxide solution and sulfuric acid were appropriately added together with the aqueous sodium hydrogen sulfide solution.
Table 3 shows the cumulative amount of various aqueous solutions added after the start of the addition of the sodium hydrosulfide aqueous solution, the amount of the solution at that time, the pH, the ORP, and the metal concentration.
The pH measurement is continuously carried out from the start of the addition of the sodium hydrogen sulfide aqueous solution, and when the pH stabilizes after each addition, the pH at that time and the elapsed time from the start of the first addition are recorded. , Other items were measured.

[PH 2.5-3.5]
The same aqueous solution addition and measurement as in Experimental Examples 14 to 23 were carried out except that the pH was changed. Experimental Example 24 is an eluate before addition, Experimental Example 25 is a solution after pH adjustment, and Experimental Examples 26 to 33 are eluates at each stage of addition. The measurement results are shown in Table 4.

According to the results shown in Tables 3 and 4, the addition of the aqueous sodium hydrogen sulfide solution reduces the nickel concentration and the cobalt concentration while the manganese concentration in the eluate does not change. When an aqueous sodium hydrogen sulfide solution is added to an ORP of −400 mV or less, nickel and cobalt precipitate as sulfides without precipitating manganese, so that nickel and cobalt can be separated into solid and liquid.

[PH 3.5-5.0]
The same aqueous solution addition and measurement as in Experimental Examples 14 to 23 were carried out except that the pH was changed. Experimental Example 34 is a solution after adjusting the pH, and Experimental Examples 35 to 38 are eluates at each stage of addition. The measurement results are shown in Table 5.

According to the results shown in Table 5, the addition of the aqueous sodium hydrogen sulfide solution reduces the nickel concentration and the cobalt concentration while the manganese concentration in the eluate does not change. When an aqueous sodium hydrogen sulfide solution is added to ORP up to −400 mV, manganese and the like do not precipitate, and nickel and cobalt precipitate as sulfides, so that nickel and cobalt can be separated into solid and liquid.
It is not easy to control the pH in the pH range of 3.5 to 5.0, and the time until the pH stabilizes after each addition of the sodium hydrosulfide aqueous solution is longer than in other experimental examples. .. Further, when the pH becomes 3.5 or higher, hydroxides having low solubility other than nickel and cobalt may start to be produced.

[PH 1.6-2.3]
The same aqueous solution addition and measurement as in Experimental Examples 14 to 23 were carried out except that the pH was changed. Experimental Example 39 is a solution after adjusting the pH, and Experimental Examples 40 to 43 are eluates at each stage of addition. The measurement results are shown in Table 6.

According to the results shown in Table 6, when the pH of the eluate was not maintained above 2.0 and was temporarily below 2.0, or when the pH was maintained above 2.0 (Table 3). It can be seen that a large amount of sodium hydrogen sulfide is required to convert cobalt and nickel into sulfides as compared with 5). In Experimental Examples 42 and 43 in the latter half of the test, the pH reached 2.0 or higher, but in Experimental Examples 40 and 41 in the first half of the test, the pH was less than 2.0, so sodium hydrogen sulfide reacted with sulfuric acid. , Cobalt, nickel sulfurization, could not be effectively used for precipitation formation. Compared to Tables 3, 4, and 5, in Table 6, cobalt and nickel remained in the liquid even though the sodium hydrogen sulfide aqueous solution was used most. The ORP was also -400 mV or higher.

From the above, in the cobalt-nickel separation step, the pH of the eluate is maintained in the range of 2.0 to 5.0, more preferably the pH is maintained in the range of 2.0 to 3.5, and the ORP is -400 mV. It was found that the aqueous solution of sodium hydrogen sulfide should be added until the following results were obtained.

(Procedure of the conventional example)
A leaching step and a copper separation step were carried out in the same manner as in the procedure of the example of the present invention to obtain an eluate. Subsequently, instead of the cobalt-nickel separation step, the manganese separation step and the aluminum separation step, which were carried out in the prior art, were carried out.

An aqueous solution of sodium hypochlorite having a concentration of 12 wt% was added to the eluent, manganese was oxidized to form a precipitate as manganese dioxide (MnO ₂ ), and manganese was removed by solid-liquid separation with a filter medium (manganese). Separation process).

In this manganese separation step, a part of cobalt and nickel is also trivalently oxidized and precipitated as a hydroxide, and solid-liquid separation is performed together with manganese dioxide, so that the yields of cobalt and nickel decrease.

Next, an operation of separating aluminum as a precipitate of hydroxide was performed by adding a 25% aqueous solution of sodium hydroxide to the filtrate obtained in the manganese separation step to adjust the pH of the filtrate to 5.5. (Aluminum separation process).

Also in this aluminum separation step, a part of cobalt and nickel are precipitated as hydroxides, and solid-liquid separation is performed together with aluminum hydroxide, further lowering the yields of cobalt and nickel.

In the above conventional procedure, when cobalt and nickel in the electrode material taken out from the waste LIB are 100%, 38.2% of cobalt and 41.3% of nickel are discharged to the outside of the system in the middle of the process. The direct yield was 61.8% for cobalt and 58.7% for nickel.

[Manganese separation process]
Regarding the above-mentioned conventional manganese separation step, a sodium hypochlorite aqueous solution having a concentration of 5% and a sodium hydroxide aqueous solution having a concentration of 25% were added to the eluate, and the change in the metal concentration in the eluate was measured. .. After measuring the eluate before addition in Conventional Experimental Example 1, addition and measurement of each aqueous solution were repeated in Conventional Experimental Examples 2 to 6. The results are shown in Table 7.

According to the results shown in Table 7, as the amount of each aqueous solution added increases and the precipitation of manganese progresses, a part of cobalt and nickel also precipitates, and up to about 15% of cobalt and nickel are contained in the manganese separation step. It turned out to be a loss.

[Aluminum separation process]
Next, regarding the aluminum separation step of the above-mentioned conventional example, the concentration of the metal (cobalt, nickel, manganese, aluminum) remaining in the filtrate with respect to the conventional experimental examples 7 to 10 in which the amount of the sodium hydroxide aqueous solution added to the filtrate was changed. And pH were measured. Conventional Experimental Example 7 is before the addition of the sodium hydroxide aqueous solution. In the conventional experimental example 10, sulfuric acid was also added. The results are shown in Table 8.

According to the results shown in Table 8, at pH 5.46 (conventional Experimental Example 9) in which almost all of aluminum precipitates as hydroxide, a part of cobalt and nickel also precipitate as hydroxide, and as a result, nickel is deposited. It was found that 23% and 17% of cobalt were lost. Further, since aluminum hydroxide becomes a gel, it is difficult to separate solid and liquid with a filter medium.

The method for separating cobalt and nickel of the present invention makes it possible to accurately separate and recover valuable metals contained in a used lithium ion secondary battery, particularly cobalt and nickel, from other metals. , High-purity recycled resources can be efficiently obtained from lithium-ion secondary batteries. Therefore, it has industrial applicability.

Claims (11)

A method for separating cobalt and nickel, which separates cobalt and nickel from lithium-ion secondary batteries.
A crushing and sorting step of crushing and classifying the lithium ion secondary battery to obtain an electrode material containing at least cobalt, nickel, copper, and lithium.
A leaching step of immersing the electrode material in a treatment liquid containing sulfuric acid and hydrogen peroxide to obtain a leaching liquid.
A copper separation step of adding a hydrogen sulfide compound to the leachate, stirring the mixture, and then performing solid-liquid separation to obtain an eluate containing cobalt and nickel and a residue containing copper sulfide.
After adjusting the pH by adding an alkali metal hydroxide to the eluent, a hydrogen sulfide compound is added and stirred to perform solid-liquid separation, and a precipitate containing cobalt sulfide and nickel sulfide and a residual liquid containing lithium are separated. Obtaining cobalt / nickel separation process,
A method for separating cobalt and nickel, which comprises. A redissolution step containing sulfuric acid is added to the precipitate separated in the cobalt-nickel separation step, and the mixture is stirred and then solid-liquid separated to obtain a cobalt-nickel solution containing cobalt and nickel.
The method for separating cobalt and nickel according to claim 1, further comprising a solvent extraction step of adding an extractant solution to the cobalt-nickel solution to obtain a cobalt extract and a nickel extract. The method for separating cobalt and nickel according to claim 2, wherein in the redissolving step, the immersion time of the precipitate in the redissolving solution is 1 hour or more. The method for separating cobalt and nickel according to any one of claims 1 to 3, wherein in the leaching step, the liquid temperature of the treatment liquid is 60 ° C. or higher and the sulfuric acid concentration is 2 mol / L or higher. In the copper separation step,
The pH of the leachate was maintained at 1.0 or less from the start to the end of the addition of the hydrogen sulfide compound.
The cobalt and nickel according to any one of claims 1 to 4, wherein an aqueous solution of sodium hydrogen sulfide is added as the hydrogen sulfide compound until the oxidation / reduction potential (vs Ag / AgCl) becomes 0 mV or less. Separation method. In the cobalt / nickel separation step,
An aqueous solution of sodium hydrogen sulfide was used as the hydrogen sulfide compound.
The pH of the eluate was maintained in the range of 2.0 to 5.0 during the period from the start to the end of the addition of the hydrogen sulfide compound.
The cobalt and nickel according to any one of claims 1 to 5, wherein the hydrogen sulfide compound is added to the eluent until the oxidation / reduction potential (vs Ag / AgCl) becomes −400 mV or less. Separation method. The separation of cobalt and nickel according to claim 6, wherein the pH of the eluate is maintained in the range of 2.0 to 3.5 from the start to the end of the addition of the hydrogen sulfide compound. Method. The cobalt and the cobalt according to any one of claims 1 to 7, wherein in the pH adjustment in the cobalt-nickel separation step, the pH of the eluate is adjusted in the range of 3.0 to 4.0. Nickel separation method. In the re-dissolution step, the precipitate is dissolved in the re-dissolution solution containing sulfuric acid and hydrogen peroxide solution, or the precipitate is added to the re-dissolution solution containing sulfuric acid, and then air bubbling is performed. The method for separating cobalt and nickel according to claim 2 or 3, which comprises dissolving. The cobalt according to any one of claims 2, 3 and 9, wherein in the redissolving step, the liquid temperature of the redissolving solution is 60 ° C. or higher and the sulfuric acid concentration is 0.5 mol / L or higher. And how to separate nickel. The method for separating cobalt and nickel according to any one of claims 1 to 10, further comprising a heat treatment step of heating the lithium ion secondary battery to perform a heat treatment as a pre-step of the crushing and sorting step. ..

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