Lithium chloride manufacturing apparatus and manufacturing method thereof

Abstract

The present invention relates to an apparatus for manufacturing lithium chloride and a method for manufacturing the same, and the apparatus for manufacturing lithium chloride includes: a hopper for supplying a lithium compound and a reducing agent; a selective chlorinator connected to a lower part of the hopper to receive chloride and induce a chlorination reaction; and an extractor connected to the top of the selective chlorinator to extract lithium chloride produced by the chlorination reaction, wherein the amount of residual Li in the lithium compound can be 15 wt% or less.

Description

[Technical Field]

[0001] The present invention relates to a lithium recovery method, and more particularly to an apparatus and method for producing lithium chloride that selectively recovers lithium from lithium compounds. [Background technology]

[0002] A conventional method for extracting lithium from lithium ore involves oxidizing and roasting spodumene, leaching it using sulfuric acid, neutralizing it, refining it, and then evaporating and concentrating it to produce Li2CO3. Specifically, the existing lithium extraction method involves roasting spodumene ore at a specific temperature to transform α-spodumene into β-spodumene, activating the reaction potential of the raw material, pulverizing it through a milling process, and then reacting it with sulfuric acid to produce lithium sulfate.

[0003] After that, it is purified through sulfidizing and carbonation processes to produce lithium carbonate, which allows the intermediate lithium compound of lithium aluminate (LiAlO2) to be used after physical sorting and pre-heat treatment processes from lithium batteries.

[0004] Lithium aluminate is attracting increasing attention as a raw material for materials that can be used in various fields such as cement and insulation. There is growing interest in selectively producing high-purity lithium chloride (LiCl) using lithium aluminate and discharging the remaining oxide, aluminum oxide (Al2O3), as a high-purity dry by-product and using it in various fields. Summary of the Invention [Problem to be solved by the invention]

[0005] The technical problem to be solved by the present invention is to provide a lithium chloride production apparatus for recovering lithium from lithium compounds, which can produce high-purity lithium chloride and produce high-purity dry by-products.

[0006] Another technical problem to be solved by the present invention is to provide a method for producing lithium chloride for lithium recovery having the above-mentioned advantages. [Means for solving the problem]

[0007] According to one embodiment of the present invention, an apparatus for producing lithium chloride includes a hopper for supplying a lithium compound and a reducing agent, a selective chlorinator connected to a lower portion of the hopper to receive chloride and induce a chlorination reaction, and an extractor connected above the selective chlorinator to extract lithium chloride produced by the chlorination reaction, wherein the amount of residual Li in the lithium compound may be 15 wt% or less. In one embodiment, the amount of residual Al in the lithium compound may be 40 wt% or more.

[0008] In one embodiment, the molar ratio of the reducing agent to the lithium compound may be 0.5 to 2.0. In one embodiment, the selective chlorination reactor may further include a collector (cyclone) connected to an upper portion of the selective chlorination reactor to collect by-products other than lithium chloride produced by the chlorination reaction.

[0009] In one embodiment, the lithium compound may be LiAlO2. In one embodiment, the lithium compound may be recovered from waste batteries.

[0010] According to another embodiment of the present invention, a method for producing lithium chloride is a method for selectively extracting Li from a lithium compound, and includes the steps of supplying a lithium compound, a reducing agent, and a chloride to a reactor to perform a chlorination reaction, and extracting lithium chloride (LiCl) through the chlorination reaction, wherein the amount of residual Li in the lithium compound may be 15 wt% or less. In one embodiment, the molar ratio of the reducing agent to the lithium compound may be 0.5 to 2.0.

[0011] In one embodiment, the lithium compound may be LiAlO2. In one embodiment, the method may further include filtering out oxide by-products from the reactor.

[0012] In one embodiment, in the step of extracting lithium chloride (LiCl) through a chlorination reaction, the gasified chloride may be extracted when the temperature of the reactor is 1,500° C. or more. In one embodiment, in the step of extracting lithium chloride (LiCl) through a chlorination reaction, the chloride may be extracted by water leaching when the temperature of the reactor is less than 1,500° C.

[0013] In one embodiment, the reducing agent may be coke or CO. In one embodiment, in the step of supplying the lithium compound, the reducing agent, and the chloride to the reactor to perform the chlorination reaction, if the chloride is a gas, the flow rate of the chloride may be 100 to 5,000 ml / min.

[0014] In one embodiment, the lithium chloride may be included in a liquid, solid, or gaseous state. In one embodiment, the chloride may include Cl gas or at least one chloride substance selected from CaCl, FeCl, MgCl, NaCl, KCl, CuCl, AlCl, and MnCl. In one embodiment, the crystalline structure of the lithium compound in the chlorination reaction may include, by volume, 40% or more of an α phase, 10 to 50% of a γ phase, and the remaining δ phase.

[0015] In one embodiment, the particle size of the lithium compound may be 10 to 500 μm. In one embodiment, the lithium compound may be recovered from waste batteries.

[0016] In one embodiment, the lithium compound may be obtained through the steps of crushing the waste battery, heat-treating the crushed battery, and magnetic separation. [Effects of the Invention]

[0017] The method for recovering lithium from a lithium compound according to one embodiment of the present invention provides a lithium recovery method that can produce high-purity lithium chloride from ore without pre-treatment and produce a high-purity dry by-product by dry-processing lithium chloride (LiCl) from the lithium compound, compared to the existing wet process system using sulfuric acid. [Brief explanation of the drawings]

[0018] [Figure 1] 1 illustrates an apparatus for producing lithium chloride, according to one embodiment of the present invention. [Figure 2] 1 shows a process diagram of the selective chlorination reaction of Li in LiAlO with Cl injection according to one embodiment of the present invention. [Figure 3] 1 shows a process diagram of the selective chlorination reaction of Li with the introduction of FeCl in LiAlO according to one embodiment of the present invention. DETAILED DESCRIPTION OF THE INVENTION

[0019] Terms such as first, second, and third are used to describe various parts, components, regions, layers, and / or sections, but are not limited to these. These terms are used to distinguish one part, component, region, layer, or section from another part, component, region, layer, or section. Therefore, a first part, component, region, layer, or section described below may be referred to as a second part, component, region, layer, or section without departing from the scope of the present invention.

[0020] The terminology used herein is merely for the purpose of referring to particular embodiments and is not intended to limit the present invention. As used herein, the singular form includes the plural form unless the context clearly dictates otherwise. As used in the specification, the meaning of "comprising" embodies certain properties, regions, integers, steps, operations, elements, and / or components, and does not exclude the presence or addition of other properties, regions, integers, steps, operations, elements, and / or components.

[0021] When a part is referred to as being "on" another part, it can mean that it is directly on top of the other part, or there can be other parts between them. In contrast, when a part is referred to as being "directly on" another part, there are no other parts between them.

[0022] Unless otherwise defined, all terms, including technical and scientific terms, used herein have the same meaning as commonly understood by a person of ordinary skill in the art to which this invention belongs. Terms defined in commonly used dictionaries are additionally interpreted as having a meaning consistent with the relevant technical literature and the presently disclosed content, and unless defined, are not interpreted as having an ideal or very formal meaning. Furthermore, unless otherwise specified, % means % by weight, and 1 ppm is 0.0001% by weight.

[0023] DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS The present invention will now be described in detail with reference to exemplary embodiments thereof, so that those skilled in the art will be able to easily understand and practice the present invention. However, the present invention may be embodied in many different forms and is not limited to the embodiments set forth herein.

[0024] FIG. 1 shows an apparatus for producing lithium chloride according to one embodiment of the present invention.

[0025] Referring to FIG. 1, the lithium chloride production apparatus is for selectively recovering lithium from lithium compounds and includes a hopper, a selective chlorinator, and an extractor.

[0026] The hopper may be a component for supplying a lithium compound and a reducing agent. The lithium compound may be recovered from waste batteries, for example, end-of-life waste batteries obtained from electric devices that use lithium ion batteries, such as electric vehicles. Specifically, the recovered materials may include process scrap generated during battery recycling, such as end-of-life waste batteries, cathode material scrap, and bi-cell scrap.

[0027] In one embodiment, the lithium compound may be obtained by crushing waste batteries, heat-treating the crushed waste batteries, and magnetically separating the heat-treated material. The lithium compound may be a residue remaining in the magnetic separation step. As a non-limiting example, the waste batteries may be crushed using a device such as a crusher.

[0028] The step of heat-treating the waste batteries may be a step of performing a reduction reaction on the waste batteries that have been pulverized. The temperature range of the heat-treating step may include any temperature condition that can cause a reduction reaction on the waste batteries. The step of magnetically separating the heat-treated materials may be a step of separating magnetic materials, such as NCM alloys, using magnetic force. The residue remaining after separating the magnetic materials may be a non-magnetic material, such as an oxide, or the lithium compound of the present invention.

[0029] The lithium compound may be a compound containing lithium. Specifically, the lithium compound may include compounds such as LiAlO2, spodumene, and black mass recovered from waste batteries. More specifically, it may be LiAlO2. The lithium compound may be a source material and an object for selectively recovering lithium.

[0030] In one embodiment, the lithium compound may have an average particle size of 10 to 500 μm, specifically, 30 to 100 μm.

[0031] If the average particle size is outside the upper limit, the efficiency of the chlorination reaction may decrease, and if the average particle size is outside the lower limit, the recovery rate may decrease due to the powder scattering phenomenon during the chlorination reaction.

[0032] The reducing agent may be a carbon-based reducing agent. The reducing agent may be a material that promotes the reduction of the lithium compound. The reducing agent may be, for example, coke or CO.

[0033] The reducing agent may serve to increase the reaction rate between the lithium compound and a chloride, which will be described later. In one embodiment, the reducing agent may have an average particle size of 10 to 500 μm. Specifically, the average particle size may be 30 to 200 μm.

[0034] If the average particle size is outside the upper limit, the chlorination reaction may not proceed smoothly, and if the average particle size is outside the lower limit, the chlorination reaction may not proceed smoothly due to slugging.

[0035] In one embodiment, the lithium compound and the reducing agent may be mixed in a predetermined ratio. The molar ratio of the reducing agent to the lithium compound may be 0.5 to 2.0. Specifically, the molar ratio may be 0.6 to 1.2.

[0036] If the molar ratio is outside the upper limit, there are problems of reduced economic efficiency and contamination with other impurities, and if the molar ratio is outside the lower limit, there is a problem of the reaction not proceeding smoothly.

[0037] The selective chlorinator is connected to the bottom of the hopper to receive chlorides for chlorination reaction. The chlorides may be solid or gaseous, such as Cl2 gas or at least one chloride substance selected from the group consisting of CaCl2, FeCl3, MgCl2, NaCl, KCl, CuCl2, AlCl3, and MnCl2.

[0038] In one embodiment, when the chloride is a gas, the flow rate of the chloride may vary depending on the scale of the application device, and may be, for example, 100 to 5,000 ml / min, specifically, 200 to 500 ml / min.

[0039] When the flow rate of the chloride is within the above range, the chlorination reaction can proceed satisfactorily. When the flow rate of the chloride is outside the above range, elution may occur, resulting in poor results in the chlorination reaction.

[0040] In one embodiment, the chlorination reaction may be carried out at a pressure in the range of 0.1 to 1.5 atm. Specifically, the pressure may be in the range of 0.3 to 1.3 atm. Only when the pressure is in this range can the chlorination reaction be achieved.

[0041] In one embodiment, the chlorination reaction step may be carried out for 5 minutes to 2 hours. When the chlorination reaction is carried out for the above time, the lithium element remaining in the chloride may be efficiently extracted.

[0042] In one embodiment, the chlorination reaction may satisfy the following reaction formula 1 and reaction formula 2 depending on the type of reducing agent. [Reaction Scheme 1] 2LiAlO2+C+Cl2(g)=2LiCl+Al2O3+CO(g) [Reaction Scheme 2] 2LiAlO2+CO(g)+Cl2(g)=2LiCl+Al2O3+CO2(g)

[0043] According to Reactions 1 and 2, when the reducing agent is C such as coke or carbon monoxide (CO) gas, it can react with the lithium compound LiAlO2 to produce lithium chloride and aluminum oxide as a by-product.

[0044] The extractor is connected to the selective chlorination reactor to extract lithium chloride produced by the chlorination reaction. The extractor can extract lithium chloride produced by the reaction of a lithium compound with a chloride, as shown in Reaction Scheme 1 or 2.

[0045] In one embodiment, the extracted lithium chloride may be in liquid, solid, or gaseous form. Specifically, if the chloride is gaseous, it may be extracted in gaseous form, e.g., lithium chloride gas.

[0046] In one embodiment, when the chloride is in a liquid or solid state, the chloride may be extracted in a liquid state. Specifically, the method for extracting the chloride in a liquid state may include, but is not limited to, various methods, such as a water leaching method, to extract lithium chloride.

[0047] In one embodiment, the chlorination reaction can be carried out at a temperature range of 300 to 1,600° C. In another embodiment, the chlorination reaction can be carried out at a temperature range of 1,500° C. or higher. When carried out in this temperature range, the produced chloride, for example, lithium chloride, can be recovered in a gaseous state.

[0048] In another embodiment, the chlorination reaction can be carried out at a temperature range of less than 1,500° C. When carried out at this temperature range, the chloride produced, e.g., lithium chloride, can be recovered in liquid or solid form.

[0049] In one embodiment, the selective chlorinator may further include a cyclone connected to the top of the selective chlorinator to collect by-products other than the lithium chloride produced by the chlorination reaction. In addition to the lithium chloride, the chlorination reaction may also produce by-products such as metal oxides. For example, the metal oxide may be Al2O3. The by-products are discharged through the collector and can be used as raw materials in various fields, such as cement or insulation materials.

[0050] In one embodiment, when the chlorination reaction is carried out at a temperature of 1,500° C. or higher, it may include a step of sublimating the gaseous chloride. The sublimation step may cool the gaseous chloride to 10 to 700° C., specifically 20 to 550° C., more specifically 20 to 300° C. When cooled to this temperature, the gaseous chloride is converted to a solid state, which may facilitate collection.

[0051] In one embodiment, when the chlorination reaction is carried out at a temperature range of less than 1,500°C, the liquid or solid chloride may be subjected to water leaching without a separate sublimation process. When the chlorination reaction is carried out at this temperature range, there is an advantage that separate temperature control is not required.

[0052] In one embodiment, the amount of residual Li in the lithium compound may be 15 wt% or less. Specifically, the amount of residual Li may be 11.3 wt% or less. The amount of residual Li in the lithium compound specifically refers to the amount of Li in the unreacted material generated after the initial raw material lithium compound undergoes a chlorination reaction. When the amount of residual Li is low as in the above-mentioned range, it can be confirmed that a considerable amount of lithium in the raw material lithium compound is converted to lithium chloride through the chlorination reaction. When the amount of residual Li is outside the above-mentioned range, the amount of lithium chloride is relatively low, resulting in a problem of a poor lithium chloride production yield.

[0053] In one embodiment, the amount of residual Al in the lithium compound may be 40 wt% or more. Specifically, the amount of Al may be 70 wt% or more. More specifically, the amount of residual Al may be 72.0 wt% or less. The amount of residual Al in the lithium compound specifically refers to the content of Al in unreacted materials generated after the initial lithium compound (raw material) undergoes a chlorination reaction. By including a high content of residual Al within the above-described range, a significant amount of lithium in the lithium compound (raw material) is converted to lithium chloride through the chlorination reaction, and Al is formed as a separate oxide and discharged, thereby producing high-purity lithium chloride. If the content of residual Al is outside the above-described range, aluminum may react with lithium and chlorine to form impurities, thereby reducing the production yield of lithium chloride.

[0054] In one embodiment, the crystalline structure of the lithium compound in the chlorination reaction may include, by volume, 40% or more of an α phase, 10 to 50% of a γ phase, and the remaining δ phase. The α, γ, and δ phases may be crystalline structures that develop depending on the temperature applied to the lithium compound.

[0055] The α, γ, and δ phases satisfying the above ranges have the advantage of facilitating the chlorination reaction, whereas the α, γ, and δ phases falling outside the above ranges have the problem of reduced reaction efficiency and chlorination rate.

[0056] According to another embodiment of the present invention, a method for producing lithium chloride is a method for selectively extracting Li from a lithium compound, and may include the steps of supplying a lithium compound, a reducing agent, and a chloride to a reactor to perform a chlorination reaction, and extracting lithium chloride (LiCl) through the chlorination reaction. Specifically, for a detailed description of the lithium compound, the reducing agent, and the chloride, please refer to FIG. 1.

[0057] The step of supplying a lithium compound, a reducing agent, and a chloride to a reactor and carrying out a chlorination reaction can be carried out in the selective chlorination reactor, which is a reactor, by supplying the lithium compound and the reducing agent from a hopper and the chloride from the bottom of the selective chlorination reactor. For a detailed description of the chlorination reaction, please refer to FIG. 1 to the extent that it is not inconsistent.

[0058] The step of extracting lithium chloride (LiCl) through the chlorination reaction may be a step of extracting lithium chloride in a gaseous, liquid, or solid state. When the lithium chloride is in a gaseous form, it may be extracted using an extractor. In the extractor, the lithium chloride in a gaseous form may additionally undergo a sublimation step, the details of which may be found above.

[0059] In another embodiment, when the lithium chloride is in a liquid or solid state, the lithium chloride can be extracted by a leaching method such as water leaching without a separate sublimation step, and the details thereof may be found in the above description.

[0060] In one embodiment, the method for producing lithium chloride may further include filtering out by-product oxides from the reactor. The by-product may be a metal oxide, for example, AlO. For a detailed description of this, please refer to the above description. [Example]

[0061] Specific examples of the present invention will be described below. However, the following examples are merely specific embodiments of the present invention, and the present invention is not limited to the following examples.

[0062] Experimental example Lithium compound LiAlO2 and a reducing agent were put into a hopper and fed to a selective chlorinator, and then chlorine gas was added at the bottom of the chlorinator to carry out a chlorination reaction for 30 minutes.

[0063] Specifically, the chlorination reaction is as shown in the following reaction formula 1 when the reducing agent is C, and as shown in the following reaction formula 2 when the reducing agent is CO gas. [Reaction Scheme 1] 2LiAlO2+C+Cl2(g)=2LiCl+Al2O3+CO(g) [Reaction Scheme 2] 2LiAlO2+CO(g)+Cl2(g)=2LiCl+Al2O3+CO2(g)

[0064] Specifically, the lithium compound and the reducing agent were mixed in a hopper and then injected into the top of the chlorination reactor. The particle size of the LiAlO2 was 75 μm, and the particle size of the reducing agent was 150 μm. Lithium chloride (LiCl) gas was then produced.

[0065] The lithium chloride gas was cooled to 25°C in a condenser to produce solid LiCl. Another product, Al2O3, was discharged as a by-product through a cyclone.

[0066] <Experimental Example 1> In the experimental example, coke was used as the reducing agent, the molar ratio of the lithium compound to the reducing agent was 1:0.7, FeCl3 was added for the chlorination reaction, the flow rate was 250 ml / min, and the reaction temperature was controlled to 1,100°C.

[0067] <Experimental Example 2> In the experimental example, coke was used as the reducing agent, the molar ratio of the lithium compound to the reducing agent was 1:0.7, FeCl3 was added for the chlorination reaction, the flow rate was 250 ml / min, and the reaction temperature was controlled to 900°C.

[0068] <Experimental Example 3> In the experimental example, coke was used as the reducing agent, the molar ratio of the lithium compound to the reducing agent was 1:0.7, FeCl3 was added for the chlorination reaction, the flow rate was 250 ml / min, and the reaction temperature was controlled to 700°C.

[0069] <Experimental Example 4> In the experimental example, coke was used as the reducing agent, the molar ratio of the lithium compound to the reducing agent was 1:0.7, FeCl3 was added for the chlorination reaction, the flow rate was 250 ml / min, and the reaction temperature was controlled to 500°C.

[0070] <Experimental Example 5> In the experimental example, coke was used as the reducing agent, the molar ratio of the lithium compound to the reducing agent was 1:0.7, the flow rate of the chlorine gas was 300 ml / min, and the reaction temperature was controlled at 900°C.

[0071] <Experimental Example 6> In the experimental example, coke was used as the reducing agent, the molar ratio of the lithium compound to the reducing agent was 1:0.7, the flow rate of the chlorine gas was 300 ml / min, and the reaction temperature was controlled at 1,000°C.

[0072] <Experimental Example 7> In the experimental example, coke was used as the reducing agent, the molar ratio of the lithium compound to the reducing agent was 1:0.7, the flow rate of the chlorine gas was 300 ml / min, and the reaction temperature was controlled at 700°C.

[0073] <Experimental Example 8> In the above experimental example, CO gas was used as a reducing agent, the flow rate of chlorine gas and CO gas was 1:1, the flow rate of the chlorine gas was 150 ml / min, and the reaction temperature was controlled at 900°C.

[0074] <Experimental Example 9> In the experimental example, CO gas was used as the reducing agent, the molar ratio of the lithium compound to the reducing agent was 1:1, the flow rate of chlorine gas to CO gas was 1:1, the flow rate of the chlorine gas was 150 ml / min, and the reaction temperature was controlled to 900°C.

[0075] Table 1 below shows the specific conditions and amounts of residual elements in the above-mentioned experimental examples. The amounts of residual elements in the lithium compound are listed as the weight percent of the remaining lithium and aluminum relative to the initial lithium compound raw material.

[0076] [Table 1]

[0077] From Table 1, it can be seen that in Experimental Examples 1 to 9, the amount of residual elements in the lithium compound was 15 wt% or less and 70 wt% or more of Al relative to the initial lithium compound raw material. This confirmed that lithium chloride was properly formed and high-purity lithium chloride was provided. In contrast, in Experimental Example 10, the amount of unreacted Li remaining was 22.7 wt%, confirming a difference in effect compared to Experimental Examples 1 to 9. It was also confirmed that aluminum was chlorinated and mixed with lithium chloride. This confirmed the difficulty of producing high-purity lithium chloride.

[0078] FIG. 2 shows a process diagram of the selective chlorination reaction of Li when Cl is introduced into LiAlO in accordance with one embodiment of the present invention.

[0079] Figure 2 shows the reaction equilibrium diagram when C and Cl2 are added together with LiAlO2. The reaction equilibrium diagram shows that when the above materials are added together, LiCl is produced by the reaction. However, when implementing the process, the amount of Cl2 gas must be properly adjusted to produce LiCl. If too much Cl2 gas is added, AlCl3 reacts with the gas, resulting in the formation of chlorides.

[0080] When LiCl is gasified at temperatures above 1,400°C, specifically, if the process conditions are controlled to above 1,400°C, LiCl can be collected in the form of chloride fumes and recovered by collecting the LiCl in a condenser. If the process conditions are controlled to temperatures below 1,400°C, LiCl can be collected in solid form and recovered by water leaching.

[0081] FIG. 3 shows a process diagram of the selective chlorination reaction of Li when FeCl3 is introduced into LiAlO2 according to one embodiment of the present invention.

[0082] Referring to FIG. 3, it can be seen that the amount of FeCl3 can be controlled compared to Cl gas, and LiCl can be selectively produced.

[0083] The present invention is not limited to the above-described embodiments and / or examples, but can be manufactured in various different forms, and a person skilled in the art to which the present invention pertains should understand that the present invention can be embodied in other specific forms without changing the technical spirit or essential characteristics of the present invention. Therefore, it should be understood that the above-described embodiments and / or examples are illustrative in all respects and are not limiting.

Claims

1. a hopper for supplying lithium compounds and reducing agents; A selective chlorinator connected to the bottom of the hopper to receive chloride and induce a chlorination reaction; and an extractor connected to the selective chlorination unit for extracting lithium chloride produced by the chlorination reaction, The amount of residual Li in the lithium compound is 15 wt % or less.

2. 2. The apparatus for producing lithium chloride according to claim 1, wherein the amount of residual Al in the lithium compound is 40 wt % or more in weight %.

3. 2. The apparatus for producing lithium chloride according to claim 1, wherein the reducing agent is supplied at a molar ratio of 0.5 to 2.0 relative to the lithium compound.

4. 2. The apparatus for producing lithium chloride according to claim 1, further comprising a collector connected to an upper portion of the selective chlorinator to collect by-products other than lithium chloride produced by the chlorination reaction.

5. 2. The apparatus for producing lithium chloride according to claim 1, wherein the lithium compound includes a compound containing lithium.

6. 2. The apparatus for producing lithium chloride according to claim 1, wherein the lithium compound is recovered from waste batteries.

7. A method for selectively extracting Li with a lithium compound, comprising: supplying a lithium compound, a reducing agent, and a chloride to a reactor to carry out a chlorination reaction; extracting lithium chloride (LiCl) from the chlorination reaction; The method for producing lithium chloride, wherein the amount of residual Li in the lithium compound satisfies 15 wt % or less in weight %.

8. 8. The method for producing lithium chloride according to claim 7, wherein the reducing agent is supplied at a molar ratio of 0.5 to 2.0 relative to the lithium compound.

9. 8. The method for producing lithium chloride according to claim 7, wherein the lithium compound includes a compound containing lithium.

10. 8. The method for producing lithium chloride according to claim 7, further comprising the step of separating by-product oxides from the reactor.

11. The step of extracting lithium chloride (LiCl) by the chlorination reaction includes:

8. The method for producing lithium chloride according to claim 7, wherein the gasified chloride is extracted when the temperature of the reactor is 1,500°C or higher.

12. The step of extracting lithium chloride (LiCl) by the chlorination reaction includes:

8. The method for producing lithium chloride according to claim 7, wherein the chloride is extracted by water leaching when the temperature of the reactor is less than 1,500°C.

13. 8. The method for producing lithium chloride according to claim 7, wherein the reducing agent is coke or CO.

14. A step of supplying a lithium compound, a reducing agent, and a chloride to a reactor to carry out a chlorination reaction, 8. The method for producing lithium chloride according to claim 7, wherein when the chloride is a gas, the flow rate of the chloride is 100 to 5,000 ml / min.

15. 8. The method for producing lithium chloride according to claim 7, wherein the lithium chloride is contained in a liquid, solid, or gaseous state.

16. The chloride is Cl ２ gas or CaCl ２ , FeCl ３ , MgCl ２ , NaCl, KCl, CuCl ２ , AlCl ３ , and MnCl ２ 8. The method for producing lithium chloride according to claim 7, wherein the chloride substance is at least one of

17. 8. The method for producing lithium chloride according to claim 7, wherein in the chlorination reaction, the crystal structure of the lithium compound includes a γ phase.

18. 8. The method for producing lithium chloride according to claim 7, wherein the particle size of the lithium compound is 10 to 500 μm.

19. 8. The method for producing lithium chloride according to claim 7, wherein the lithium compound is recovered from waste batteries.

20. The lithium compound is crushing the waste batteries; heat treating the pulverized heat treatment; and 8. The method for producing lithium chloride according to claim 7, wherein the lithium chloride is obtained through a step of magnetic separation.

Images