CA3198115A1

CA3198115A1 - Process for recovering and purifying lithium

Info

Publication number: CA3198115A1
Application number: CA3198115A
Authority: CA
Inventors: Paula Kivela; Peik EKMAN; Pasi Kauppinen; Kenneth Ekman; Ville Yrjana
Original assignee: Fortum Oyj
Current assignee: Fortum Oyj
Priority date: 2020-11-10
Filing date: 2021-11-09
Publication date: 2022-05-19
Also published as: US20230399720A1; ES3034961T3; WO2022101549A1; EP3995597C0; HUE072224T2; CN116670311A; PL3995597T3; KR20230115993A; RS67066B1; EP3995597B1; EP3995597A1; AU2021380050A1

Abstract

The present invention relates to the recovery and purification of lithium from lithium containing sources, like lithium ion battery materials, using ion exchange. A lithium salt containing solution is passed through an acid cation exchange resin, and a lithium raffinate and a mixture of other elements such as metals like nickel, cobalt and manganese, are recovered as products. The lithium raffinate can then be processed into other lithium products such as lithium carbonate and lithium hydroxide.

Description

PROCESS FOR RECOVERING AND PURIFYING LITHIUM
Field of the invention The present invention relates to the recovery and purification of lithium from lithium containing sources, like lithium ion battery materials.
Background of the invention As both customer demand and technology readiness for electric appliances and vehicles increase, lithium ion batteries (LIBs) are becoming more important to fill the role for mobile energy storage. While invented in 1985, recent developments to increase energy density and production costs have seen a large increase in demand for LlBs. The current most common LIB types for electric mobility are based on NCM (nickel, cobalt and manganese) or NCA
(nickel, cobalt, aluminium) as cathode materials and graphite as anode material. Even though effective, the current price for virgin materials make these technologies quite expensive to deploy while also causing significant GHG emissions during mining and processing to battery grade chemicals.
In recent years, there has been a significant uptick in efforts to mitigate the prices and emissions caused by LIB production by recycling end-of-life batteries. Routes for recycling are several, including pyro- and hydrometallurgical routes for metal recovery and separation.
Currently, the majority of the batteries that are recycled are introduced in existing pyrometallurgical facilities such as smelters. Hydrometallurgical routes, or combinations of routes, are currently being built and tested around the world, and reductive roasting followed by leaching of lithium is emerging as a technology for recovery of lithium.
This technology is a first-step lithium recovery method requiring high temperatures (>500 C) and expensive reducing agents (e.g. hydrogen or coal) which increase the CO2 footprint of the process significantly.

2 The primary lithium production is concentrated to South America, where lithium-rich brine is pumped into massive evaporation pools where it is concentrated by solar evaporation. This process takes up to two years. The lithium concentrate is then processed into lithium carbonate, and then eventually turned into lithium hydroxide by a conversion reaction with lime and crystallized by evaporation. The emergence of low-cobalt cathode materials favor hydroxide as lithium source, which is more readily processed from solid ore.
JP 2019 125464 A discloses a lithium recovery method in which lithium is recovered from wastewater in a manufacturing step of containing lithium and calcium of a positive electrode material for a lithium secondary battery. This method includes: a suction step of bringing wastewater in the manufacturing step into contact with a plurality of ion exchange resins connected in series; and an elution step of separating the plurality of ion exchange resins after the suction step and bringing an eluent into contact with each ion exchange resin.
WO 2019/160982 discloses the extraction of lithium from liquid resources, such as natural and synthetic brines, leachate solutions from clays and minerals, and recycled products.
A novel method for recovering and purifying lithium from lithium containing sources has been invented. The method according to the present invention is a one-step purification and separation route in which a lithium containing solution is purified using chromatographic separation. The method can be used to recover and purify any lithium containing solution such as process liquors from LIB recycling or primary lithium production. In comparison to currently known processes, the described method according to the present invention is low-emission, simple and produces a high-purity lithium intermediate that can be used in battery grade lithium production.
Summary of the invention The present invention relates to the recovery and purification of lithium from lithium containing sources, like lithium ion battery materials, using ion exchange. A
lithium salt

3 containing solution is passed through an acid cation exchange resin, and a lithium raffinate and a mixture of other elements such as metals like nickel, cobalt and manganese, are recovered as products. The lithium raffinate can then be processed into other lithium products such as lithium carbonate and lithium hydroxide.
More precisely the present inventions relates to a method for recovering and purifying lithium from a lithium containing material comprising the steps of; passing a process solution containing lithium salt and other elements through an acid cation exchange resin; collecting a lithium raffinate; optionally flushing out residual lithium as lithium hydroxide with a monoprotic hydroxide; eluting the other elements from the acid cation exchange resin with a strong acid solution to obtain an eluate and regenerating the acid cation exchange resin with a monoprotic hydroxide solution.
According to one embodiment of the invention the lithium containing material is a lithium ion battery material.
According to another embodiment of the invention the lithium salt is a lithium sulphate.
According to still another embodiment of the present invention the process solution has a pH
of 3-5.5.
According to a further embodiment of the invention the monoprotic hydroxide is sodium hydroxide.
According to still a further embodiment of the invention sulphuric acid is used as the strong acid in the acid solution.
According to one embodiment of the invention the acid cation exchange resin is a weak acid cation having carboxylic acids as a functional group.
According to still another embodiment of the invention the process solution is passed through at a rate of 0.5-6 BVs/h.

4 Brief description of the drawingError! Reference source not found. 1. A
schematic flow chart of the method according to the present invention.
Figure 2. Relative concentration curves of elements in Example 1.
Figure 3. Breakthrough curves of columns 1, 2 and 3 in Example 6.
Figure 4. Breakthrough curves of columns 1-6 in Example 7.
Definitions Black mass, a mixture of cathode and anode active materials, separated from battery components BV or BVs mean bed volume or bed volumes; the volume of a resin bed when packed into a column DC means dry content ICP-MS means Inductively Coupled Plasma Mass Spectrometer LIB, lithium ion battery MP-AES means Microwave Plasma Atomic Emission Spectrometer NCA, a type of cathode material based on nickel, cobalt and aluminium NCM, a type of cathode material based on nickel, cobalt and manganese WAC, weak acid cation SAC, strong acid cation Detailed description of the invention The present invention relates to the recovery and purification of lithium from lithium containing sources. The raw material i.e. the lithium containing source can be e.g. lithium ion battery (LIB) material or any other lithium containing source such as off-specification material or by-product from primary lithium production.

5 In primary lithium production from both brine and ore, common impurities present are calcium, magnesium and potassium that can be processed by different hydrometallurgical methods. In the lithium carbonate conversion reaction, calcium hydroxide is used as hydroxide source. These elements are difficult to prevent from co-precipitation during lithium precipitation or crystallization and thus some amount of the lithium products are considered unusable for battery materials. Lithium content in these materials is highly variable and for the process, according to the present invention, are pre-treated with sulfuric acid, hydrochloric acid or other applicable acids to transform them into lithium salt containing solutions. Any potential insoluble impurities are filtered.
Typically, lithium content in any battery material directly relates to the amount of other cathode elements present in the material, such as nickel, cobalt, manganese (NCM-based) or aluminium (NCA-based). Black mass is expected to contain 3-4 wt% lithium. In a typical LIB
recycling hydrometallurgical process, this black mass is subjected to a leaching step to dissolve the soluble elements after which the insoluble materials (e.g.
graphite) can be separated by filtration. The resulting filtrate is expected to contain 2.5-4.5 g/1 of lithium, but the lithium content may also be higher depending on the black mass or the leaching step parameters.
The term "process solution" as used in the context of the present invention means a lithium salt containing solution with a pI4 of 3-5.5, preferably 4-4.5. The adjustment of pH of the lithium salt containing solution, if needed, can be done with a monoprotic hydroxide or with the acid already present in the mentioned solution.
Filtrate obtained from the filtration step of the above described leaching process presents a typical lithium salt containing solution. The metal composition of that solution will vary depending on the raw material, e.g. cathode elements present or impurities present, and may contain both aluminium and manganese as well as other elements, such as iron, magnesium and calcium, depending on the source material.

6 The recovery and purification process according to the present invention is now described in detail referring to the schematic flow chart of Figure 1.
In the chromatographic separation, which is the first step of the recovery and purification process according to the present invention, the process solution containing lithium salt and other elements, like nickel, cobalt and manganese, depending on the elements present in the raw material, with a pH of 3-5.5, preferably 4-4.5, is passed through an acid cation exchange resin bed, such as carboxylic or sulfonic acid resin bed, at a rate of 0.5-6 BVs/h, preferably 2-4 BVs/h. Collection of lithium raffinate starts at 0-1 BVs, preferably at 0.5-1 BVs while other elements are retained in the resin until operating capacity is reached. The operating capacity can be predetermined by calculating the resin capacity from the element content of the initial feed. On the other hand, the operating capacity can be detected on-line by visual inspection or with spectroscopic methods such as by UV or other methods known by person skilled in the art. For a typical process solution containing 20-30 g/1 of elements (i.e.
lithium and other elements in total), the lithium raffinate is collected at 0-3 BVs, preferably 0.5-2 BVs.
Temperature during chromatographic separation can be 20-100 C, preferably 25-50 C and intra-column pressure can be from ambient up to 10 bar, preferably between 1-5 bar.
Lithium raffinate comprises lithium salt and a monoprotic salt that is a result of the chromatographic separation. As an optional step, the lithium raffinate can be circulated through the resin bed several times to further increase purity and concentration of lithium in the lithium raffinate. The resulting lithium raffinate can then be processed to lithium products such as lithium carbonate or lithium hydroxide using known hydrometallurgical methods.
Optionally, aqueous monoprotic hydroxide e.g. sodium hydroxide is used to flush out residual lithium from the columns i.e. from the resin loaded with other elements and residual lithium, producing a lithium hydroxide solution. The concentration of the monoprotic hydroxide used in this step is 0.25-2 wt%, preferably 0.5-1 wt%.
One further step (not shown in Figure 1), also optional, is to add monoprotic hydroxide solution to the lithium raffinate and use that hydroxide-raffinate solution for flushing to

7 increase purity and concentration of lithium of the lithium raffinate. The solution leaving the column after flushing contains lithium salt, lithium hydroxide and a monoprotic salt that is a result of the chromatographic separation.
In the second step, the other elements are eluted from the resin with 1-4 BVs of a strong acid solution like 10-25 wt%, preferably 15-20 wt% sulphuric acid or hydrochloric acid solution.
Also other applicable strong acids can be used with the similar concentration.
The resulting eluate contains e.g. nickel, cobalt, manganese and/or aluminium in a form of salts e.g., sulfates or chlorides depending on the strong acid used. The acid solution is fed at a rate of 1-6 BVs/h, preferably 2-4 BVs/h.
The eluate can then be processed into separate products with traditional hydrometallurgical methods such as solvent exchange, precipitation and ion exchange.
The resin bed is washed with 0.5-2 BVs, preferably 1-1.5 BVs, of water to remove residual eluate.
In the final step, the resin is regenerated using a 2-25 wt%, preferably 5-20 wt%, monoprotic hydroxide like sodium or lithium hydroxide solution, which is fed through the resin bed at a rate of 1-6 BVs/h, preferably 2-4 BVs/h. After this step, the resin bed is ready for repeated use.
The number of columns in series can be 1-10, preferably 2-6. Other techniques, such as simulated moving bed, can also be applied for this invention.
Examples In the examples 1-8 below, black mass containing NCM based cathode material was dissolved in sulfuric acid using hydrogen peroxide as a reducing agent to obtain a lithium salt containing solution. The metal composition is presented in Table 1.

8 Table 1. Metal composition of the lithium salt containing solution.
Element mg/kg Co 10 200 Li 2 550 Mn 1 480 Ni 8 850 Example 1 40 ml of Finex CA16G-Na resin with carboxylic acid functionality was loaded into a 25 rum diameter chromatographic column (YMC Eco). Bed height measured to 575 mm. pH
of the lithium salt containing solution was adjusted to 3.5 with sodium hydroxide (NaOH) to obtain a process solution. 700 ml of the process solution was pumped at a rate of 1 BVs/h through the resin bed and then immediately followed by 500 ml of 20 % sulfuric acid (112SO4) and then followed by water until clear solution was collected. Samples were collected at 50 ml intervals. Samples were analysed with MP-AES for metal content, and were presented as relative concentration curve (sample concentration (c) vs. original concentration (co) in the process solution). The curves are shown in Figure 2.
A clear chromatographic separation of lithium is observed as lithium concentration increases to about 1.5x the original. In the area of 0.8 BY to 2 BVs, 80% of lithium is separated from other elements.
Example 2 40 ml of Finex CA16G-Na resin with carboxylic acid functionality was loaded into a 30 xi=
diameter column. Bed height was measured to 80 mm. pH of the lithium containing solution (containing dissolved battery material) was increased to pH 4 with sodium hydroxide. 38 ml of the pH-adjusted process solution was circulated through the resin bed for 3 hours at a rate of 3 BVs/h. The lithium raffinate was collected, the resin bed was washed with 2 BVs of water,

9 and then eluted with 1.5 BVs of 20 wt% sulfuric acid (H2SO4). The samples were analysed with MP-AES (Agilent Technologies) for metal contents and yields were calculated and are presented in Table 2.
Table 2. Metal yields of the solutions in Example 2.
Sample Co Li Mn Ni Lithium raffinate 0 % 60 % 0 % 0 %
Eluate 100% 40% 99% 100%
Total 100% 100% 99% 100%
Chromatographic separation of lithium is clearly demonstrated, which allows recovery of at least 60% of the lithium present in the leach, lithium salt containing, solution.
Example 3 40 ml of Finex CA16G-Na resin with carboxylic acid functionality was loaded into a 30 rum diameter column. Bed height was measured to 80 mm. pH of the leach solution i.e. the lithium salt containing solution was increased to 3.1 with NaOH, and 41 ml of this process solution was passed through the resin bed at a rate of 3 BV/h. The lithium raffinate was collected and analysed with MP-AES.
The resin bed was washed with 2 bed volumes of water, after which the resin bed was flushed with 1 BY of 20 wt% NaOH solution. The flushing solution was collected and analysed with MP-AES. Finally, the resin was eluted with 1.5 BVs of 20 wt% H2SO4 which was collected and analysed with MP-AES. Metals yields were calculated in all samples and are presented in Table 3.
Table 3. Metal yields of the solutions in Example 3.
Sample Co Li Ni Lithium raffinate 0 % 16 % 0 %

10 Lithium hydroxide 0 % 84 % 0 %
solution Eluate 100% 0% 100%
Total 100% 100% 100%
Example 4 40 ml of Finex CA16G-Na resin with carboxylic acid functionality was loaded into a 30 xi=
diameter column. Bed height was measured to 80 mm. pH of a lithium salt containing solution was increased to 3 with NaOH, and 50 ml of the process solution was passed through the resin bed at a rate of 3 BV/h. The lithium raffinate was collected and analysed with MP-AES.
The resin bed was washed with 2 bed volumes of water, after which the resin bed was flushed with 1 BV of 5 wt% NaOH solution. The flushing solution was collected and analysed with MP-AES. Lastly, the resin was eluted with 1.5 BVs of 20 wt% H2SO4 and eluate was collected and analysed with MP-AES.
Metals yields were calculated in all samples and are presented in Table 4.
Table 4. Metal yields of the solutions in Example 4.
Sample Co Li Ni Lithium raffinate 0 % 36 % 0 %
Lithium hydroxide solution 0 % 65 % 0 %
Eluate 79% 0% 100%
Total 79 % 99% 100 %
Example 5 Three columns were each packed with 4300 ml of Finex CA16G-Na resin. pH of the leach solution was adjusted to 4.4 with NaOH. The process solution was pumped through the

11 columns in series at a rate of 1.6 BVs/h, and samples were taken at 1 liter intervals after each column. All samples were analysed with MP-AES.
161g of NaOH was dissolved in 20 1 of lithium raffmate and the columns were flushed at a rate of 1.6 BVs/h using this mixture (optional step, not shown in Figure 1).
Samples were taken at 1 liter intervals and analysed with MP-AES. As the last step, the columns were eluted with 1.5 BVs of 20 wt% H2SO4 at a rate of 4 BV/h. The results are presented in Table 5.
Table 5. Metal yields of solutions in Example 5.
1. column Co Li Mn Ni Lithium raffinate 36 % 68 % 37 % 34 %
Lithium hydroxide 2 % 19 % 2 % 1 %
solution Eluate 53 % 9 % 45 % 51 %
2. column Co Li Mn Ni Lithium raffinate 3 % 43 % 3 % 3 %
Lithium hydroxide solution 0 % 36 % 1 % 1 %
Eluate 36% 9% 38% 33%
3. column Co Li Mn Ni Lithium raffinate 0 % 16 % 0 % 0 %
Lithium hydroxide solution 0 % 44 % 0 % 0 %
Eluate 5% 18% 7% 4%
Example 6 Three columns were packed each with 4300 ml of Finex CA16G-Na resin and pH of the dissolved black mass was increased to 4 with NaOH. The process solution was pumped through the columns in series at a rate of 2 BV/h, and samples were taken at 1 liter intervals after each column. All samples were analysed with MP-AES. Columns were washed with 1 BY of water and as the last step, the columns were eluted with 1.5 BVs of 20 wt% H2SO4.
Breakthrough curves are shown in Figure 3.

12 The chromatographic effect is evident when the column length increases, as lithium is moving faster through the columns and breaking through earlier than nickel, cobalt and manganese.
Consequently, this allows for collection lithium fraction free from other metals.
Example 7 Six columns were packed each with 4300 ml of Finex CA16G-Na resin and pH of lithium salt containing solution was increased to 4 with NaOH. The process solution was pumped through the columns in series at a rate of 4 BV/h, and samples were taken at 1 liter intervals after each column. All samples were analyzed with MP-AES. Columns were washed with 1 BV
of water and as the last step, the columns were eluted with 1.5 BVs of 20 wt% H2SO4.
Breakthrough curves are shown in Figure 4.
Based on these results, it can be concluded that the other elements, e.g.
nickel, cobalt and manganese bind harder to the resin allowing lithium to exit the column earlier resulting in lithium fraction free from other metals coming at the end of the last column.
Example 8 A black mass containing NCM cathode material was dissolved in hydrochloric acid and filtered. Filtrate pH was increased to 4.2 with NaOH to create a process solution. 50 ml process solution was passed through 40 ml of Finex CA16G-Na resin at a rate of 2 BVs/h. 50 ml of lithium raffinate was collected and resin was eluted with 1 BY of 10 % HC1.
Table 6. Metal yields of the solutions in Example 8.
Sample Co Li Mn Ni Raffinate 15 % 75 % 16 % 15 %
Eluate 75 % 21 % 75 % 76 %
Total 90 % 95 % 91 % 90 %

Claims

1. A method for recovering and purifying lithium from a lithium containing material comprising the steps of a) passing a process solution containing lithium salt and other elements through an acid cation exchange resin, which process solution has a pH of 3-5.5 and is passed through the acid cation exchange resin at a rate of 0.5-6 BVs/h in a chromatographic separation, b) collecting a lithium raffinate at 0-1 BVs while the other elements are retained in the cation exchange resin until operating capacity is reached, c) optionally flushing out residual lithium as lithium hydroxide with a monoprotic hydroxide, d) eluting the other elements from the acid cation exchange resin with 1-4 BVs of a strong acid solution to obtain an eluate, which strong acid solution is fed at a rate of 1-6 BVs/h, e) washing the acid cation exchange resin with 0.5-2 BVs of water to remove residual eluate, and f) regenerating the acid cation exchange resin with the 2-25 wt% monoprotic hydroxide solution, which is fed through the acid cation exchange resin at a rate of 1-6 BVs/h.

2. The method for recovering and purifying lithium according to claim 1, wherein the lithium containing material is a lithium ion battery material.

3. The method for recovering and purifying lithium according to any one of claim 1 or 2, wherein the lithium salt is lithium sulphate.

4. The method for recovering and purifying lithium according to any one of claims 1-3, wherein the monoprotic hydroxide is sodium hydroxide.

5. The method for recovering and purifying lithium according to any one of claims 1-4, wherein the strong acid is sulphuric acid.

6. The method for recovering and purifying lithium according to any one of claims 1-5, wherein the acid cation exchange resin is a weak acid cation having carboxylic acids as functional group.