JP2023073299A - Method for producing lithium hydroxide - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a method for producing lithium hydroxide which can easily obtain lithium hydroxide from lithium sulfate at low cost.

SOLUTION: A method for producing lithium hydroxide from lithium sulfate includes: a hydroxylation step of reacting the lithium sulfate with barium hydroxide in a liquid to obtain a lithium hydroxide solution; a barium removal step of removing barium ions in the lithium hydroxide solution using a cation exchange resin and/or a chelate resin; and a crystallization step of depositing lithium hydroxide in the lithium hydroxide solution through the barium removal step.

SELECTED DRAWING: Figure 1

COPYRIGHT: (C)2023,JPO&INPIT

Description

This specification discloses a technique relating to a method for producing lithium hydroxide.

For example, lithium sulfate may be obtained in liquid or solid form in the process of recovering valuable metals from lithium ion secondary battery waste or various electronic devices, or in the processing of salt lake brines or ores and the like.

For example, in one example of treatment of lithium ion secondary battery waste, lithium ion secondary battery waste is subjected to a treatment such as roasting, and then a lithium solution in which lithium contained therein is dissolved is obtained. The lithium solution may be subjected to solvent extraction of lithium ions and back-extraction from the solvent into the aqueous phase to concentrate, and after this extraction and back-extraction the back-extraction liquid is a lithium sulfate solution. There are cases. This type of extraction and back extraction is described in Patent Documents 1 to 3 and the like.

The back-extracted liquid obtained after the above back-extraction is generally carbonated by addition of carbonate or blowing of carbon dioxide gas, as described in Patent Document 3. In this case, lithium is recovered as lithium carbonate.

By the way, Patent Documents 4 and 5 describe a method for producing lithium hydroxide, which can be used as a raw material for a positive electrode material of a lithium ion secondary battery, from lithium carbonate.
Specifically, in Patent Document 4, "In an electrolytic apparatus composed of an anode tank, a cathode tank, and a cation exchange membrane, electrolysis is performed by supplying a lithium carbonate aqueous solution or suspension to the anode tank to perform cation exchange. A process for the production of lithium hydroxide by forming an aqueous solution of lithium hydroxide in a cathodic cell through a membrane is disclosed.
Moreover, Patent Document 5 discloses that "a cation exchange membrane and an anion exchange membrane are alternately arranged between an anode and a cathode, an anode chamber is formed by the anode and the cation exchange membrane, and then from the anode side to the cathode side. Towards, an acid chamber partitioned by the cation exchange membrane and an anion membrane, a salt chamber partitioned by the anion exchange membrane and another cation exchange membrane, and partitioned by this cation exchange membrane and another anion exchange membrane One or more sets of an acid chamber, a salt chamber, an alkali chamber, and a water electrolysis chamber, which are arranged in the order of an alkali chamber divided by this anion exchange membrane and a new cation exchange membrane and a water electrolysis chamber partitioned by the new cation exchange membrane, are arranged. Instead of the cation membrane, the water electrolysis chamber composed of the most cathode-side anion membrane is partitioned by the cathode, and an electrodialyzer is used to make it a cathode chamber, and an aqueous solution of lithium salt is supplied to the salt chamber to acidify it. A method for producing lithium hydroxide, characterized by removing an acid from a chamber and an aqueous solution of lithium hydroxide from an alkali chamber”.

Patent documents 4 and 5 both use lithium carbonate as a raw material, and manufacture lithium hydroxide from the lithium carbonate using electrolysis.

JP 2010-180439 A U.S. Patent Application Publication No. 2011/0135547 JP 2014-162982 A JP 2009-270188 A Japanese Unexamined Patent Application Publication No. 2011-31232

In the production of lithium hydroxide from lithium sulfate as described above, if the technology described in Patent Documents 4 and 5 were to be applied, it would be necessary to first convert lithium sulfate into lithium carbonate, and then Electrolysis not only increases the number of man-hours, but also greatly increases the cost due to the implementation of electrolysis.

In particular, this specification discloses a method for producing lithium hydroxide by which lithium hydroxide can be easily obtained from lithium sulfate at low cost.

The method for producing lithium hydroxide disclosed in this specification is a method for producing lithium hydroxide from lithium sulfate, wherein the lithium sulfate is reacted with barium hydroxide in a liquid to obtain a lithium hydroxide solution. a barium removal step of removing barium ions in the lithium hydroxide solution using a cation exchange resin and/or a chelate resin; and an analysis step.

According to the method for producing lithium hydroxide described above, lithium hydroxide can be easily obtained from lithium sulfate at low cost.

1 is a flow chart showing a method for producing lithium hydroxide according to one embodiment; FIG. FIG. 2 is a flowchart showing an example of a process for obtaining lithium sulfate that can be used in the method for producing lithium hydroxide of FIG. 1; 5 is a graph showing the relationship between the lithium concentration and barium concentration of a lithium hydroxide solution after passing through a resin in Test Example 2, and BV (Bed Volume). 4 is a graph showing the temperature dependence of metal concentration in saturation dissolution of compounds of each metal.

Hereinafter, embodiments disclosed in this specification will be described in detail.
A method for producing lithium hydroxide according to one embodiment is a method for producing lithium hydroxide from lithium sulfate. For example, as shown in FIG. A hydroxylation step of obtaining a lithium oxide solution, a barium removal step of adsorbing and removing barium ions in the lithium hydroxide solution using a cation exchange resin and/or a chelate resin, and lithium hydroxide that has undergone the barium removal step. and a crystallization step of precipitating lithium hydroxide in solution.

Lithium hydroxide has a lower melting point than lithium carbonate, and may be effectively used as a raw material for positive electrode materials of lithium ion secondary batteries. Therefore, in this embodiment, lithium hydroxide, rather than lithium carbonate, is easily produced at low cost from lithium sulfate. In particular, the object here is to sufficiently reduce impurities in the lithium hydroxide to be produced, and to produce lithium hydroxide with such a high purity that it can be suitably used as a raw material for a positive electrode material.

Here, lithium hydroxide can be obtained relatively easily by the hydroxylation step of reacting lithium sulfate with barium hydroxide based on the formula Li ₂ SO ₄ +Ba(OH) ₂ →2LiOH+BaSO ₄ . After the reaction, barium sulfate produced by the reaction can be removed to some extent by solid-liquid separation.
However, it is unavoidable that barium ions remain in the lithium hydroxide solution, and even if the solution is crystallized as it is, the presence of the barium reduces the purity of lithium hydroxide.

Therefore, in this embodiment, after the hydroxylation step, barium ions present in the lithium hydroxide solution due to the addition of barium hydroxide in the hydroxylation step are adsorbed with a cation exchange resin and / or a chelate resin. After that, a barium removal step is performed to remove barium, and then a crystallization step is performed. As a result, high-purity lithium hydroxide with a low barium content is obtained.

(lithium sulfate)
Lithium sulfate used as a raw material for producing lithium hydroxide can be obtained, for example, by a process of recovering valuable metals from lithium ion secondary battery waste.

A lithium-ion secondary battery has a housing containing aluminum as an exterior wrapping around the battery. Examples of this housing include those made only of aluminum, those containing aluminum and iron, aluminum laminates, and the like. In addition, the lithium ion secondary battery has a positive electrode active layer made of a single metal oxide selected from the group consisting of lithium, nickel, cobalt and manganese, or a composite metal oxide of two or more types, etc., in the housing. The material, or cathode active material, may include aluminum foil (cathode substrate) that is coated and adhered by, for example, polyvinylidene fluoride (PVDF) or other organic binder or the like. In addition, the lithium ion secondary battery may contain copper, iron, and the like. In addition, lithium ion secondary batteries typically contain an electrolyte within the housing. As the electrolytic solution, for example, ethylene carbonate, diethyl carbonate, etc. may be used.
Examples of lithium sulfate obtained from such lithium ion secondary battery waste are shown below.

(Lithium dissolution process)
As exemplified in FIG. 2, the lithium-ion secondary battery waste is processed by roasting, crushing, sieving, etc. as necessary, and then the lithium contained therein is dissolved in water or an acidic solution. Lithium dissolving process Then, a solution containing lithium (hereinafter referred to as a lithium solution) is obtained. Since the step of dissolving lithium shows alkalinity as lithium dissolves, the pH may be adjusted as necessary so that the final pH of the lithium solution is 7-10. In this case, if the pH is 7 to 10, the elution of cobalt, nickel, aluminum, etc. can be suppressed, and mainly lithium can be selectively dissolved. A lithium solution obtained by treating lithium ion secondary battery waste by roasting or the like and then dissolving it in water or an acidic solution contains few impurities and is suitable as a raw material for lithium hydroxide, which will be described later. In addition, the residue generated in the lithium dissolution step can be used in the process of recovering valuable metals such as cobalt and nickel by acid leaching, neutralization, solvent extraction, and the like.

Alternatively, the lithium dissolution solution is obtained by leaching all elements and removing impurities without first recovering lithium from the sieved material obtained by roasting, crushing, and sieving the lithium ion battery waste. Alternatively, valuable metals such as cobalt, nickel, and manganese may be recovered to form a solution in which lithium remains.

(lithium concentration step)
Next, as shown in FIG. 2, a lithium concentration step is performed to extract the lithium ions in the lithium solution with a solvent and back extract the lithium ions in the solvent to concentrate the lithium ions and obtain a lithium sulfate solution. Here, in the lithium concentration step, the solvent after extracting lithium ions can be scrubbed with a lithium solution containing lithium ions. In this case, back extraction is performed on the solvent after scrubbing.

As will be described later, sodium hydroxide is often used as a pH adjuster during extraction, and in this case, the solvent after extraction contains sodium ions in addition to lithium ions. Therefore, it is preferable to perform the scrubbing between extraction and back extraction. This is because scrubbing the solvent with a lithium solution is effective in removing sodium ions extracted into the solvent.

The lithium sulfate solution obtained in the lithium concentration step can be used as lithium sulfate in the embodiment shown in FIG.

Specifically, the extraction is performed, for example, by contacting a lithium solution (aqueous phase) and a solvent (organic phase), stirring and mixing them with a mixer, and transferring lithium ions and the like in the lithium solution to the solvent. After that, the settler separates the organic phase and the aqueous phase based on the difference in specific gravity. The O/A ratio, which is the volume ratio of the organic phase to the aqueous phase, can be greater than 1.5/1.0, depending on the lithium ion concentration and other conditions. In order to increase the extraction rate of lithium ions, the O/A ratio can be adjusted and the number of extraction stages can be increased.

Here, for the lithium dissolution solution, as the extractant that is the solvent, a phosphonate extractant alone, a phosphate ester extractant alone, or a phosphonate ester extractant and a phosphate ester extractant are used. Mixed extractants can be used. As the phosphonate extractant, 2-ethylhexyl 2-ethylhexylphosphonate (trade name: PC-88A, Ionquest 801) is preferable from the viewpoint of separation efficiency of nickel and cobalt. Examples of the phosphate extractant include di-2-ethylhexyl phosphate (trade name: D2EHPA or DP8R).

The extractant can be diluted with an aromatic, paraffinic, naphthenic, or other hydrocarbon organic solvent, if necessary, before use. In this case, the concentration of the extractant can be, for example, 15% to 35% by volume.

The equilibrium pH during extraction is preferably 7-8. This is because if the equilibrium pH is less than 7, the lithium extraction rate may be low and phase separation may be poor. This is because the extractant and diluent may separate. From this point of view, it is more preferable to set the equilibrium pH at the time of extraction to 7.2 to 7.5. The term "equilibrium pH" as used herein refers to the pH of the liquid-aqueous phase when the liquid-aqueous phase and the oil phase are separated by standing still after the solvent extraction operation, scrubbing operation, and back-extraction operation.

A pH adjuster such as sodium hydroxide, lithium hydroxide, aqueous ammonia, or other alkaline solutions can be used to adjust the pH during extraction. Among them, sodium hydroxide is preferred because it is less expensive than other reagents and has no odor. Moreover, even if sodium hydroxide is added as a pH adjuster, the resulting sodium ions can be effectively removed by scrubbing, which will be described later in detail, so that an increase in sodium that becomes an impurity can be suppressed.

Scrubbing the solvent with a lithium solution is effective in removing sodium ions extracted into the solvent. By adjusting the lithium ion concentration in the lithium solution or the like, the sodium ions in the solvent can be effectively removed because the lithium ions in the lithium solution are replaced with the sodium ions in the solvent. At this time, lithium ions and sodium ions are generally substituted in the same number of moles. Therefore, if the number of moles of lithium ions in the lithium solution is equal to or greater than the number of moles of sodium ions in the solvent, the sodium ions in the solvent can be removed more effectively.

The lithium ion concentration in the lithium solution used for scrubbing is preferably 1.0 g/L to 10.0 g/L, more preferably 1.0 g/L to 5.0 g/L.

During scrubbing, it is preferable to adjust the pH of the mixture of the solvent and the lithium solution to 5.0 to 9.0, and further to adjust the pH to 6.0 to 8.0. is even more preferable.

Through the scrubbing process, the sodium ion concentration in the solvent can be preferably reduced to 1 mg/L or less.

The lithium ions contained therein are then back-extracted from the scrubbed solvent. In the back extraction, for example, a pre-back extraction liquid, which is an acidic aqueous solution, is stirred and mixed with a mixer or the like. As a result, the lithium ions contained in the solvent are transferred to the aqueous phase.

The pre-back-extraction solution used for back-extraction may be any inorganic acid such as sulfuric acid, hydrochloric acid, nitric acid, etc. Among them, sulfuric acid is preferred. This is because, by using sulfuric acid, the liquid after back extraction becomes a lithium sulfate liquid, which can be used as a raw material for lithium hydroxide.

Back extraction maintains a pH such that the equilibrium pH is preferably within the range of 0.5 to 2.0, more preferably within the range of 1.0 to 1.5. If the equilibrium pH at the time of back extraction deviates from the range and becomes low, the amount of the pH adjuster at the time of extraction may increase. Moreover, when the equilibrium pH exceeds the range, there is concern that lithium ions may remain in the solvent. If back extraction is performed in multiple stages, the pH may increase as the number of stages is increased. It is preferable to manage the
Other conditions are appropriately set, but the O/A ratio can be, for example, 1.0 or more, preferably 1.0 to 1.5.

The post-back extraction liquid obtained in the back extraction step can be further subjected to the back extraction step as a pre-back extraction liquid, thereby further increasing the lithium ion concentration. In addition, the post-reverse extraction liquid can also be used in the scrubbing step as a lithium solution.

The post-reverse extraction solution (lithium sulfate solution) has a lithium ion concentration of, for example, 10 g/L to 30 g/L, typically 20 g/L to 25 g/L. Also, the sodium ion concentration in the post-back extraction liquid is preferably 3 mg/L or less, more preferably 1 mg/L or less.

In particular, the lithium ion concentration in the lithium sulfate solution obtained from the lithium ion secondary battery waste as described above is, for example, 10.0 g/L to 30.0 g/L, typically 20.0 g/L. ~25.0 g/L. The sodium ion concentration in the lithium sulfate solution is, for example, less than 10.0 mg/L, typically 3.0 mg/L or less, more typically 1.0 mg/L or less. Impurities other than sodium, such as potassium, calcium, iron, copper, zinc, aluminum, nickel, cobalt, manganese, etc., are kept low even before solvent extraction. On the other hand, impurities such as phosphorus and chlorine are removed prior to solvent extraction, resulting in low concentrations.

However, it can be applied not only to the process of recovering valuable metals from lithium ion secondary battery waste but also to various processes for obtaining liquid or solid lithium sulfate.

(Hydroxylation process)
In the hydration step, lithium sulfate as the liquid after back extraction or the like is reacted with barium hydroxide in the liquid to obtain a lithium hydroxide solution. The reaction here can be expressed as Li ₂ SO ₄ +Ba(OH) ₂ →2LiOH+BaSO ₄ . As a result, a lithium hydroxide solution in which lithium hydroxide is dissolved is produced, and barium sulfate is precipitated. The use of barium hydroxide is effective in that a lithium hydroxide solution can be produced by a chemical conversion reaction with lithium sulfate.

More specifically, in the case of a lithium sulfate solution, barium hydroxide is added to the lithium sulfate solution and reacted in the liquid. Alternatively, in the case of solid lithium sulphate, the lithium sulphate and barium hydroxide are added to a liquid such as water to form a slurry to cause the reaction to occur. Although barium hydroxide can be added in a solid state, the efficiency of the reaction can be improved by adding barium hydroxide in a liquid state as a barium hydroxide solution. In particular, as shown in FIG. 4, the saturated solubility of barium hydroxide increases between 40° C. and 100° C. Therefore, it is more preferable to bring a barium hydroxide solution at 40° C. to 100° C. into contact with lithium sulfate for reaction. preferable. Preferably, the barium hydroxide solution is a saturated aqueous solution.

Barium hydroxide is 1.05 times to 1.70 times the equivalent of the total of lithium hydroxide and free sulfate ions in the above reaction formula. Double addition is preferred. Sulfuric acid ions can be removed by adding a certain amount of excess barium hydroxide. Even if a relatively large amount of barium hydroxide is added, barium ions can be effectively removed in the barium removing step described later. If the amount of barium hydroxide added is too small, there is concern that unreacted lithium sulfate will precipitate during crystallization and the amount of lithium hydroxide recovered will decrease. Moreover, when the sulfate ion is excessive, there is a possibility that the sulfate ion remains as an impurity during crystallization. On the other hand, if the amount of barium hydroxide added is excessive, the amount of barium hydroxide that does not contribute to the reaction increases. Since barium hydroxide that does not contribute to the reaction becomes an impurity during crystallization, the burden of the barium removal step increases, which may increase the total cost.

In addition, the above-mentioned free sulfate ions means the difference when there are more sulfate ions than lithium ions. Therefore, the total equivalent of lithium ions and free sulfate ions means the equivalent of lithium ions when the number of lithium ions is greater than that of sulfate ions, and the equivalent of sulfate ions when the number of sulfate ions is greater than that of lithium ions.

When reacting lithium sulfate and barium hydroxide, the pH of the liquid should be 9 or higher. Although the upper limit is not specified, 12 or less is preferable because if the pH exceeds 12, it becomes excessive. A low pH may result in insufficient reaction of lithium sulfate to lithium hydroxide, while a high pH may result in excess barium hydroxide, chemical costs, and removal costs. There is a risk.

Most of the barium sulfate produced in the above reaction can be removed by solid-liquid separation using a thickener, filter press, or the like after the reaction. That is, most of the barium sulfate can be separated from the lithium hydroxide solution by solid-liquid separation after the reaction.

However, even if solid-liquid separation is performed, barium may remain dissolved in the lithium hydroxide solution. Since the barium ions contained in the lithium hydroxide solution lower the grade of the lithium hydroxide after crystallization, in this embodiment, barium ions are removed by performing the barium removal step described below.

(Barium removal step)
In the barium removal step, in order to remove the barium ions in the lithium hydroxide solution obtained in the hydroxylation step, the lithium hydroxide solution is brought into contact with a cation exchange resin and / or a chelate resin to remove the impurities. . Specifically, a lithium hydroxide solution is passed through the resin. As a result, barium ions that may be contained in the lithium hydroxide solution are adsorbed by the resin, so barium can be removed from the lithium hydroxide solution. As a result, high-purity lithium hydroxide can be obtained after the crystallization step described later.

Here, it is important to select the resin and conditions in the barium removal step so that the barium ions in the lithium hydroxide solution are efficiently removed.

At least one of a cation exchange resin and a chelate resin is used as the resin for removing barium ions and the like. The lithium hydroxide solution may be brought into contact with either the cation exchange resin or the chelate resin, and then the other. In other words, the resin adsorption process may be performed in multiple stages.

A cation exchange resin is a synthetic resin that binds cations by having acidic groups on its surface. A chelating resin is a resin having functional groups that form complexes with metal ions. Since the lithium hydroxide solution contains lithium ions and the like in addition to barium ions, it is desirable to use a cation exchange resin and/or a chelate resin having a high selectivity difference with respect to lithium ions in this impurity removal step.

When a cation exchange resin is used, it is preferable to use a weakly acidic cation exchange resin having a carboxyl group as a functional group. Strongly acidic cation exchange resins have a small difference in selectivity between monovalent metals and divalent metals, so there is a risk that divalent metals will leak from a relatively early stage of liquid flow. On the other hand, the weakly acidic cation exchange resin adsorbs a metal by sandwiching it between two carboxyl groups, so it has high selectivity to divalent metals. In particular, a weakly acidic cation exchange resin having a high ion exchange capacity and excellent physical strength is suitable.

The chelate resin has high selectivity for specific metals due to the chelate effect of ion exchange and coordination bonding of functional groups. In particular, a chelate resin can be effectively used in a lithium hydroxide solution in which lithium ions and the like coexist. There are iminodiacetic acid type and aminophosphoric acid type chelating resins. Among them, aminophosphoric acid type chelating resins are preferable because they have higher selectivity for barium and the like with respect to monovalent ions than other chelating resins.

When a cation exchange resin or chelate resin is packed in a column and a lithium hydroxide solution is passed through the column, the space velocity (SV) in the column is preferably in the range of 5-20. The space velocity (SV) means the ratio (double amount) of the passage amount of the lithium hydroxide solution per hour to the cation exchange resin or chelate resin packed in the column. In general, if the space velocity (SV) is too high, there is a concern that the barium ions in the lithium hydroxide solution will not be sufficiently removed due to insufficient adsorption time of barium ions to the resin. If the spatial velocity (SV) is too slow, the processing speed will decrease and the processing time will increase.

When the lithium hydroxide solution is brought into contact with the cation exchange resin and/or the chelate resin, it is preferable that the pH of the lithium hydroxide solution is 9 or higher, that is, the lithium hydroxide solution is alkaline. This is because when the pH of the lithium hydroxide solution is less than 9, the efficiency of removing barium ions may decrease, or even lithium ions may be adsorbed, depending on the resin used. It is from. The pH of the lithium hydroxide solution to be brought into contact with the resin may be changed depending on the type of resin selected.

(Crystallization step)
In the crystallization step, lithium hydroxide is deposited in the lithium hydroxide solution from which impurities have been removed in the barium removal step. Thereby, lithium hydroxide can be obtained.

In the crystallization step, a crystallization operation such as heat concentration or vacuum distillation can be performed in order to deposit lithium hydroxide. In the case of concentration by heating, the higher the temperature during crystallization, the faster the treatment, which is preferable. However, after crystallization, it is preferable to dry the crystallized product at a temperature of less than 60° C. at which water of crystallization does not desorb. This is because when the water of crystallization is desorbed, it becomes anhydrous lithium hydroxide, which has deliquescence and is difficult to handle.

After that, pulverization treatment or the like can be performed in order to adjust the above lithium hydroxide to the required physical properties.

The lithium hydroxide thus obtained has a barium content sufficiently reduced to, for example, 10 ppm by mass or less due to the above-described barium removal step. Such high-purity lithium hydroxide is suitable for use as a raw material for manufacturing lithium-ion secondary batteries.

Next, the method for producing lithium hydroxide as described above was carried out on a trial basis, and the effect was confirmed, which will be described below. However, the description herein is for illustrative purposes only and is not intended to be limiting.

(Test example 1)
After adding 250 g of lithium sulfate and 648 g of barium hydroxide to 5000 mL of water, solid-liquid separation was performed by filtration to obtain a lithium hydroxide solution. Li concentration in the lithium hydroxide solution was 6.0 g/L, Ba concentration was 1.3 g, and pH was 12.

In Example 1, the lithium hydroxide solution obtained as described above was passed at room temperature through a column packed with 20 mL of a cation exchange resin having a carboxyl group (AMBERLITE IRC76 manufactured by Organo Co., Ltd.) to remove impurities. removed. The lithium hydroxide solution had a pH of 12 and a space velocity (SV) of 9 during this passage.

In Example 2, impurities were removed by passing the above lithium hydroxide solution at room temperature through a column filled with 20 mL of a chelate resin (AMBERLITE IRC747UPS manufactured by Organo Co., Ltd.). The lithium hydroxide solution had a pH of 12 and a space velocity (SV) of 9 during this passage.

In Comparative Example 1, resin adsorption was not performed on the above lithium hydroxide solution.

After that, for both Examples 1 and 2 and Comparative Example 1, the lithium hydroxide solution was heated and concentrated at a temperature of 50° C. to crystallize lithium hydroxide.

Table 1 shows the impurity contents of the lithium hydroxides obtained in Examples 1 and 2 and Comparative Example 1 above.

From Table 1, in both Examples 1 and 2, compared to Comparative Example 1, the Ba content in lithium hydroxide was sufficiently reduced. It can be seen that the ions were effectively removed.

(Test example 2)
For each of the cation exchange resin used in Example 1 and the chelate resin used in Example 2, when changing the BV (Bed Volume), which is a multiple of the water flow rate with respect to the resin amount, the Changes in the Li concentration and Ba concentration in the lithium hydroxide solution after passing through the resin were confirmed. BV is represented by BV=flow rate (L)/resin volume (L). Here, the same lithium hydroxide solution as in Test Example 1 was used. The results are shown graphically in FIG.

From FIG. 3, it can be seen that the high Li concentration and the low Ba concentration in the lithium hydroxide solution after flowing are maintained over a relatively wide range of BV. Therefore, according to this, it turned out that it can contribute to manufacture of relatively high-purity lithium hydroxide from lithium sulfate.

(Test example 3)
Lithium in lithium ion secondary battery waste after roasting is dissolved in water or an acidic solution, lithium ions are extracted from the resulting lithium solution with a solvent, and the solvent after extraction is scrubbed with a lithium solution, followed by scrubbing. Lithium ions were back-extracted from the solvent after passing through, thereby obtaining a lithium sulfate solution as a post-back-extraction liquid. Table 2 shows the impurity composition of the liquid after back extraction.

After barium hydroxide was added to the above lithium sulfate solution, solid-liquid separation was performed by filtration to obtain a lithium hydroxide solution. Using each of the cation exchange resin used in Example 1 and the chelate resin used in Example 2, the lithium hydroxide solution after passing through the resin was heated and concentrated at a temperature of 50 ° C., and hydroxylated. Lithium was crystallized.
As a result, high-purity lithium hydroxide of the same level as in Examples 1 and 2 in Table 1 was obtained.

(Test example 4)
A test was conducted to confirm the difference in reaction efficiency between the case of using lithium sulfate and barium hydroxide in the form of a solid and the case of using them as a solution in the hydroxylation step.

In Example 3, solid lithium sulfate and barium hydroxide were added to pure water and reacted. Specifically, 419 g (1.7 equivalents) and 493 g (2.0 equivalents) of solid barium hydroxide were prepared for 100 g of solid lithium sulfate. The above lithium sulfate and each barium hydroxide were added to 500 mL of pure water, and the mixture was stirred and held at 60° C. for 24 hours, followed by solid-liquid separation to recover a lithium hydroxide solution.

In Example 4, both lithium sulfate and barium hydroxide were mixed as solutions and allowed to react, and then the lithium hydroxide solution was recovered. More specifically, 200 mL of solution obtained by dissolving 50 g of lithium sulfate in pure water at 60 ° C., 123 g (1.0 equivalent), 130 g (1.05 equivalent) and 136 g (1.1 equivalent) of barium hydroxide ) was mixed with pure water at 60° C. to form a solution of 800 mL, and after stirring and holding at 60° C. for 24 hours, solid-liquid separation was performed to obtain a lithium hydroxide solution.

Table 3 shows the grade of lithium hydroxide produced by shaking the amount of barium hydroxide as in Examples 3 and 4 and crystallizing each lithium hydroxide solution obtained by distillation under reduced pressure. . As for lithium sulfate and barium hydroxide, special grade reagents from Wako were used.

Table 3 shows the values of sulfur and barium as impurity grades in the lithium hydroxide obtained by crystallization. S is derived from unreacted lithium sulfate, and Ba is derived from unreacted barium hydroxide. .

When solids reacted with each other, the grades of sulfur and barium changed between 1.7 and 2.0 equivalents, so it was found that lithium sulfate reacted in the same region. . On the other hand, when the liquids were reacted, it was found that the total amount of lithium sulfate reacted between 1.0 and 1.05 equivalents, and it was found that the reaction efficiency could be improved by adding barium hydroxide as a solution. rice field.

The method for producing lithium hydroxide disclosed in this specification is a method for producing lithium hydroxide from lithium sulfate, wherein the lithium sulfate is reacted with barium hydroxide in a liquid to obtain a lithium hydroxide solution. a barium removal step of removing barium ions in the lithium hydroxide solution using a cation exchange resin and/or a chelate resin; In the hydration step, the lithium sulfate is a lithium sulfate solution, the barium hydroxide is a barium hydroxide solution, the barium hydroxide solution is brought into contact with the lithium sulfate solution, and the water is In the oxidation step, the barium hydroxide solution is brought into contact with the lithium sulfate at a liquid temperature of 40°C to 100°C .

Claims (10)

A method for producing lithium hydroxide from lithium sulfate, comprising:
A hydration step of reacting the lithium sulfate with barium hydroxide in a liquid to obtain a lithium hydroxide solution, and using a cation exchange resin and/or a chelate resin to remove barium ions in the lithium hydroxide solution. A method for producing lithium hydroxide, comprising a barium removing step and a crystallization step of precipitating lithium hydroxide from the lithium hydroxide solution that has undergone the barium removing step. 2. The method for producing lithium hydroxide according to claim 1, wherein in said barium removal step, said lithium hydroxide solution is brought into contact with said cation exchange resin and/or chelate resin at a pH of 9 or higher. The production of lithium hydroxide according to claim 1 or 2, wherein in the barium removal step, the space velocity (SV) when passing the lithium hydroxide solution through the cation exchange resin and/or the chelate resin is 5 to 20. Method. The method for producing lithium hydroxide according to any one of claims 1 to 3, wherein a weakly acidic cation exchange resin having a carboxyl group as a functional group is used in the barium removal step. The lithium sulfate is a lithium sulfate solution,
The lithium sulfate solution dissolves lithium in the lithium ion secondary battery waste after roasting with water or an acidic solution to obtain a lithium solution, and extracting lithium ions from the lithium solution with a solvent. 5. The method for producing lithium hydroxide according to any one of claims 1 to 4, wherein the lithium hydroxide is obtained by a process including a lithium concentration step of back-extracting the lithium ions. 6. The method for producing lithium hydroxide according to claim 5, wherein in the lithium concentration step, after lithium is extracted into a solvent, the solvent is scrubbed with a lithium solution, and lithium ions are back-extracted from the scrubbed solvent. The method for producing lithium hydroxide according to any one of claims 1 to 6, which produces lithium hydroxide used for producing a lithium ion secondary battery. The method for producing lithium hydroxide according to any one of claims 1 to 7, wherein in the hydroxylating step, the barium hydroxide is used as a barium hydroxide solution, and the barium hydroxide solution is brought into contact with the lithium sulfate. 9. The method for producing lithium hydroxide according to claim 8, wherein the barium hydroxide solution is a saturated aqueous solution. 10. The method for producing lithium hydroxide according to claim 8 or 9, wherein in the hydrating step, the barium hydroxide solution is brought into contact with the lithium sulfate at a liquid temperature of 40°C to 100°C.

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