WO2024055518A1 - 一种从锂离子电池电解液中回收锂的方法 - Google Patents

一种从锂离子电池电解液中回收锂的方法 Download PDF

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WO2024055518A1
WO2024055518A1 PCT/CN2023/077686 CN2023077686W WO2024055518A1 WO 2024055518 A1 WO2024055518 A1 WO 2024055518A1 CN 2023077686 W CN2023077686 W CN 2023077686W WO 2024055518 A1 WO2024055518 A1 WO 2024055518A1
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lithium
phase
electrolyte
solvent
loaded
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PCT/CN2023/077686
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English (en)
French (fr)
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王娇萍
李长东
阮丁山
李强
周游
谭明亮
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广东邦普循环科技有限公司
湖南邦普循环科技有限公司
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Publication of WO2024055518A1 publication Critical patent/WO2024055518A1/zh

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    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M10/00—Secondary cells; Manufacture thereof
    • H01M10/54—Reclaiming serviceable parts of waste accumulators
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • B09B3/80—Destroying solid waste or transforming solid waste into something useful or harmless involving an extraction step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D15/00—Lithium compounds
    • C01D15/08—Carbonates; Bicarbonates
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B26/00—Obtaining alkali, alkaline earth metals or magnesium
    • C22B26/10—Obtaining alkali metals
    • C22B26/12—Obtaining lithium
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/006—Wet processes
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M10/00—Secondary cells; Manufacture thereof
    • H01M10/05—Accumulators with non-aqueous electrolyte
    • H01M10/052—Li-accumulators
    • H01M10/0525—Rocking-chair batteries, i.e. batteries with lithium insertion or intercalation in both electrodes; Lithium-ion batteries
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B2101/00—Type of solid waste
    • B09B2101/15—Electronic waste
    • B09B2101/16—Batteries
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/50—Reuse, recycling or recovery technologies
    • Y02W30/84—Recycling of batteries or fuel cells

Definitions

  • the invention belongs to the technical field of battery material recycling processing, and specifically relates to a method for recovering lithium from lithium-ion battery electrolyte.
  • Electrolyte is the key material of lithium-ion batteries. It plays a role in conducting ions between the positive and negative electrodes in the battery. It is the guarantee for the normal operation of lithium-ion batteries and the advantages of high voltage and high specific energy.
  • the electrolyte is generally composed of high-purity organic solvents, electrolyte lithium salts (lithium hexafluorophosphate, LiF 6 PO 4 ) and other raw materials. Therefore, a large amount of waste lithium-ion battery electrolyte will be produced after the service life of the lithium-ion battery. Among them, because some lithium ions will migrate into the electrolyte during use of lithium-ion batteries, the lithium content in the electrolyte of waste lithium-ion batteries can reach 7-14g/L.
  • the electrolyte of waste lithium-ion batteries will evaporate in the air. It absorbs water and deteriorates. At the same time, it contains toxic components. If it leaks into the air, it will pollute the environment. If the waste lithium-ion battery electrolyte is not properly treated, it will cause great harm to the environment and human body.
  • the electrolyte in lithium-ion batteries is distributed between the positive and negative electrode sheets and the separator.
  • the electrolyte collected by directly crushing the single battery contains too many impurities, and most of them are Adhesion to the broken material prevents the electrolyte from being collected.
  • most of the carbonates contained in the electrolyte are insoluble in water, because their density is close to that of water, it is difficult to separate into layers after mixing with water. Therefore, good separation effects cannot be achieved, and there are no reports on electrolysis in the current literature. Efficient and convenient collection method of liquid.
  • alkaline solution is currently used directly for treatment. However, ester organic solvents will hydrolyze to varying degrees in alkaline environments, making it impossible to proceed to the next step of recovery.
  • the present invention aims to solve at least one of the technical problems existing in the prior art. To this end, the present invention proposes a method for recovering lithium from lithium-ion battery electrolyte. This solves the problem of difficult layer separation between carbonate and water in the electrolyte.
  • a method for recovering lithium from lithium ion battery electrolyte includes mixing waste electrolyte and an extraction agent and then layering to obtain an upper organic layer with a density not higher than 1.07g/cm 3
  • the lower layer supports the lithium phase with a density of 1.15 ⁇ 1.5g/ cm3 ;
  • the waste electrolyte includes lithium ions and ester organic solvents
  • the extraction agent includes an aqueous solution of salt and a solvent
  • the solvent includes at least one of ethanol and methanol
  • the upper organic phase includes the ester organic solvent
  • the supported lithium phase includes water.
  • the density of the water phase is increased by preparing an aqueous solution of salt, and after mixing in proportion with at least one of ethanol and methanol, the lithium in the waste electrolyte is extracted, and after standing for a period of time, the liquid is separated into layers. , realizes the separation of the ester organic solvent in the organic phase of the waste electrolyte and the loaded lithium phase, and solves the problem of difficult layer separation after the ester organic solvent in the electrolyte is mixed with water.
  • the ester organic solvent includes at least one of dimethyl carbonate and ethyl methyl carbonate.
  • the mass concentration of the aqueous salt solution is 5% to 25%.
  • the volume ratio of the waste electrolyte, the aqueous salt solution and the solvent is 1 ⁇ 3:1 ⁇ 3:1 ⁇ 3.
  • the volume ratio of the waste electrolyte, the aqueous salt solution and the organic solvent is 1:1:1, 2:1:1, 2:2:1, 2:1:2,1; 3:3, 3:1:1, 3:2:1, 3:3:1 or 3:1:3.
  • the density of the upper organic phase is not higher than 1.07g/cm 3 and the density of the lower lithium-loaded phase is about 1.15 to 1.5g/cm 3 , which can realize the stratification of the upper organic phase and the lower lithium-loaded phase.
  • the stratification time is 0.5 to 3 hours.
  • the layering method includes standing.
  • the aqueous salt solution includes at least one of a sulfate salt aqueous solution and a chloride salt aqueous solution.
  • the solute of the aqueous sulfate solution includes at least one of potassium sulfate and sodium sulfate.
  • the solute of the aqueous chloride salt solution includes at least one of sodium chloride and potassium chloride.
  • the mixing temperature is 15-100°C.
  • the mixing time is 5 to 30 minutes.
  • the mixing is performed by stirring, and the stirring speed of the stirring is 60 to 400 r/min.
  • the method for recovering lithium further includes distilling the upper organic phase.
  • the rectification includes batch rectification.
  • the temperature of the intermittent rectification is 60-120°C
  • the pressure of the intermittent rectification is 10kPa ⁇ 50kPa
  • the intermittent distillation time is 10 ⁇ 30min.
  • the method for recovering lithium further includes removing impurities from the lower layer loaded with lithium to obtain a liquid phase product.
  • the impurity removal includes distillation.
  • the temperature of the distillation is 15°C to 100°C
  • the vacuum degree of the distillation is 10kPa to 70kPa
  • the distillation time is 10 to 45 minutes.
  • the distillation collects the distillation residue and fraction; the recovery method of the fraction includes condensation.
  • the condensation temperature is 20-25°C.
  • the method for recovering lithium further includes using the fraction as a solvent for extraction.
  • the method for recovering lithium further includes mixing the distillation residue and an aqueous carbonate solution.
  • the mass concentration of the carbonate is 1% to 15%.
  • the added amount of the carbonate is based on the molar ratio of Li + :CO 3 2- , which is 2:1.2-1.4.
  • the mixing time of the liquid phase product and the aqueous carbonate solution is 20 to 30 minutes.
  • the solid and liquid are separated, and the solid phase product and the filtrate are collected respectively.
  • the filtrate is a press filtrate.
  • the method further includes adding acid to the filtrate.
  • the pH value of the filtrate after acid addition is 0.5-1.
  • the purpose of adding acid is to remove carbonate in the filtrate.
  • the pH of the filtrate after acid addition is adjusted to 6-7 to obtain the salt solution as part of the extraction agent.
  • the aqueous solution of the salt obtained above can be recycled as part of the extraction agent.
  • the lower layer loaded lithium phase further includes concentration before impurity removal, and the concentration includes the following steps:
  • step S2 After collecting the secondary lithium-loaded phase, replenish the solvent, use it as an extraction agent again, and repeat the operation of step S1 until the lithium content in the obtained liquid phase is 16-20 g/L.
  • the lithium content in the supported lithium phase can be increased.
  • the aqueous solution of solvent or salt is mixed with the waste electrolyte, there will be a small amount of A certain amount of solvent volatilizes, and at the same time, a small amount of solvent enters the upper organic phase (lithium removal electrolyte phase) during layering. Therefore, a certain amount of solvent needs to be supplemented, and there is no need to supplement the aqueous salt solution.
  • step S1 the waste electrolyte is added in a volume ratio of 1:1 to the lower layer loaded lithium phase.
  • step S1 the volume of the lower layer supporting lithium phase is marked as V 1
  • step S2 the volume of the secondary supporting lithium phase is marked as V 2
  • step S2 The amount of solvent added is V 2 -V 1 .
  • the lithium concentration in the lithium-loaded phase will gradually become enriched, which is conducive to the precipitation of lithium ions.
  • the present invention realizes the enrichment of lithium in the lithium-loaded phase by supplementing the waste electrolyte and solvent before impurity removal in the lithium-loaded phase, which is beneficial to the recovery of lithium.
  • the waste electrolyte, salt water and ethanol are mixed evenly according to the above adding amounts, and the lithium in the electrolyte is extracted.
  • the liquids are separated into layers to obtain an upper organic phase and a lower lithium-loaded phase.
  • the lithium-loaded phase Carry out low-temperature distillation to collect the solvent ethanol in the extraction agent, which can be used for recycling extraction.
  • An aqueous solution of salt in the extractant is obtained, which can be recycled as an extractant.
  • the upper organic phase is subjected to batch distillation to obtain dimethyl carbonate and ethyl methyl carbonate.
  • Figure 1 is a process flow diagram of a method for recovering lithium in Embodiment 2 of the present invention.
  • Figure 2 is a process flow diagram of a method for recovering lithium in Embodiment 1 of the present invention.
  • This embodiment discloses a method for recovering lithium from lithium ion battery electrolyte.
  • the content of each component is as follows, in terms of weight percentage: 30% dimethyl carbonate, 33% ethylene carbonate Ester, 32% ethyl methyl carbonate; lithium 9g/L.
  • step S3 After adding 100mL ethanol and 1L electrolyte to the lithium-loaded phase in the lower layer, repeat step S1.
  • the lithium concentration in the lithium-loaded phase continues to increase.
  • the lithium content of the lithium-loaded phase (secondary lithium-loaded phase) in the final system is 20g/ L;
  • step S5 Add hydrochloric acid to the filtrate in step S4 to adjust the pH to 1 to remove CO 3 2- , then add sodium hydroxide to adjust the pH to 7 to obtain an aqueous solution of the salt in the extraction agent. Realize the recycling of salt aqueous solution.
  • Figure 2 is a process flow diagram of a method for recovering lithium in Embodiment 1 of the present invention.
  • step S1 the lithium content in the lithium removal electrolyte phase in the upper layer is 0.01g/L. After the lithium carbonate is precipitated in the lower layer, the extraction rate of lithium in this part is 99%.
  • the extraction rate is calculated as (lithium content in the electrolyte - lithium content in the upper lithium-removing electrolyte phase after layering in step S1)/lithium content in the electrolyte.
  • step S2 the recovery rate of dimethyl carbonate was 80%, and the recovery rate of ethyl methyl carbonate was 75%.
  • This embodiment discloses a method for recovering lithium from lithium ion battery electrolyte.
  • the content of each component is as follows, in terms of weight percentage: 30% dimethyl carbonate, 33% ethylene carbonate Ester, 32% ethyl methyl carbonate; lithium 9g/L.
  • step S4 Add hydrochloric acid to the filtrate in step S3 to adjust the pH to 1 to remove carbonate, then add sodium hydroxide to adjust the pH to 7 to obtain an aqueous solution of the salt in the extraction agent.
  • step S1 the lithium content in the lithium removal electrolyte phase in the upper layer is 0.01g/L, and lithium carbonate precipitate is obtained in the lower layer.
  • the extraction rate of this part of lithium is 99%.
  • step S2 the recovery rate of dimethyl carbonate was 85%, and the recovery rate of ethyl methyl carbonate was 75%.
  • Figure 1 is a process flow diagram of a method for recovering lithium in Embodiment 2 of the present invention.
  • This embodiment discloses a method for recovering lithium from lithium ion battery electrolyte.
  • the content of each component is as follows, in terms of weight percentage: 30% dimethyl carbonate, 33% ethylene carbonate Ester, 32% methyl ethyl carbonate; lithium 9g/L, the specific steps are:
  • step S5 Add hydrochloric acid to the filtrate in step S4 to adjust the pH to 1 to remove carbonate, then add sodium hydroxide to adjust the pH to 7 to obtain an aqueous solution of the salt in the extraction agent.
  • step S1 the lithium content in the lithium removal electrolyte phase in the upper layer is 0.01g/L. After the lithium carbonate is precipitated in the lower layer, the extraction rate of this part of lithium is 99%.
  • step S2 the recovery rate of dimethyl carbonate was 80%, and the recovery rate of ethyl methyl carbonate was 70%.
  • This comparative example discloses a method for recovering lithium from lithium ion battery electrolyte.
  • the difference between this comparative example and Example 1 is that ethanol in step S1 of Example 1 is not added in this comparative example.
  • the remaining conditions are the same as those of Example 1. same.
  • This comparative example discloses a method for recovering lithium from lithium ion battery electrolyte.
  • the difference between this comparative example and Example 1 is that the 15% sodium chloride brine in step S1 of Example 1 is not added in this comparative example.
  • the remaining conditions are the same as in Example 1.
  • the lithium-loaded phase and the lithium-removing electrolyte phase cannot be collected according to the above steps. Under the combined action of the solution and ethanol, the ethanol extracts the lithium in the electrolyte.
  • the brine mainly plays a stratification role. Without the brine, the densities of the upper organic phase and the lower lithium-loaded phase are similar, and stratification cannot be achieved, so the load cannot be collected. Lithium phase and lithium-removing electrolyte phase.
  • This comparative example discloses a method for recovering lithium from lithium ion battery electrolyte.
  • the difference between this comparative example and Example 1 is that the density of the upper organic phase in this comparative example is 1.1g/cm 3 , and the remaining conditions and implementation Same as Example 1.
  • This comparative example discloses a method for recovering lithium from lithium ion battery electrolyte.
  • the difference between this comparative example and Example 1 is that in this comparative example, the density of the lower layer loaded lithium phase is 1.0g/cm 3 , and the remaining conditions are the same as those in Example 1. Same as Example 1.
  • This comparative example discloses a method for recovering lithium from lithium ion battery electrolyte.
  • the difference between this comparative example and Example 1 is that in this comparative example, the density of the lower layer loaded lithium phase is 1.6g/cm 3 , and the remaining conditions are the same as those in Example 1. Same as Example 1.
  • step S1 the lithium content in the lithium removal electrolyte phase in the upper layer is 0.12g/L. After the lithium carbonate is precipitated in the lower layer, the extraction rate of this part of lithium is 98%.
  • step S2 the recovery rate of dimethyl carbonate was 80%, and the recovery rate of ethyl methyl carbonate was 70%.

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Abstract

本发明公开了一种从锂离子电池电解液中回收锂的方法，包括将废电解液和萃取剂混合后分层，得到密度不高于1.07g/cm3的上层有机相和密度为1.15～1.5g/cm3的下层负载锂相；所述废电解液包括锂离子和酯类有机溶剂；所述萃取剂包括盐的水溶液和溶剂；所述溶剂包括乙醇和甲醇中的至少一种；所述上层有机相包括所述酯类有机溶剂；所述负载锂相包括水。本发明的回收锂的方法，解决了电解液中碳酸酯与水混合后难分层分离的问题。

Description

一种从锂离子电池电解液中回收锂的方法 技术领域
本发明属于电池材料循环利用处理技术领域，具体涉及一种从锂离子电池电解液中回收锂的方法。
背景技术
电解液是锂离子电池的关键材料，在电池中正负极之间起到传导离子的作用，是锂离子电池正常工作，并获得高电压、高比能等优点的保证。电解液一般由高纯度的有机溶剂、电解质锂盐(六氟磷酸锂，LiF6PO4)等原料组成，因此在锂离子电池使用寿命结束后将会产生大量的废锂离子电池电解液。其中，因为锂离子电池在使用过程中部分锂离子会迁移到电解液中，使废锂离子电池电解液中的锂含量可达7～14g/L，同时废锂离子电池电解液在空气中会吸水变质，同时其含有有毒成分，泄露在空气中会对环境造成污染，废锂离子电池电解液若得不到合理的处理，对环境和人体会造成极大危害。
目前锂离子电解液回收最大的问题是：1、锂离子电池中电解液分布在正负极片和隔膜之间，直接破碎单体电池收集到的电解液含有过多的杂质，且大部分都粘附在破碎料上，无法收集电解液。电解液中含有的碳酸酯，虽大部分不溶于水，但由于其密度与水接近，与水混合后很难分层分离，故无法达到好的分离效果，且目前的文献报道中没有对电解液高效便捷的收集方法。2、关于锂的回收目前是直接采用碱液处理，但是酯类有机溶剂在碱性环境下会出现不同程度的水解，无法进行下一步回收处理。
因此，开发一种从锂离子电池电解液中回收锂的方法，能够解决废锂离子电池电解液中酯类有机溶剂与水混合后难分离的问题是目前的当务之急。
发明内容
本发明旨在至少解决现有技术中存在的技术问题之一。为此，本发明提出一种从锂离子电池电解液中回收锂的方法。解决了电解液中碳酸酯与水混合后难分层分离的问题。
根据本发明的第一方面实施例的一种从锂离子电池电解液中回收锂的方法，包括将废电解液和萃取剂混合后分层，得到密度不高于1.07g/cm3的上层有机相和密度为1.15～1.5g/cm3的下层负载锂相；
所述废电解液包括锂离子和酯类有机溶剂；
所述萃取剂包括盐的水溶液和溶剂；
所述溶剂包括乙醇和甲醇中的至少一种；
所述上层有机相包括所述酯类有机溶剂；
所述负载锂相包括水。
根据本发明实施例的一种从锂离子电池电解液中回收锂的方法，至少具有以下有益效果：
本发明通过配制盐的水溶液将水相的密度增大，并协同乙醇和甲醇中的至少一种按比例混合后，将废电解液中的锂萃取出来，静置一段时间后，分层分液，实现了废电解液有机相中的酯类有机溶剂与负载锂相分离，解决了电解液中酯类有机溶剂与水混合后难分层分离的问题。
根据本发明的一些实施例，所述酯类有机溶剂包括碳酸二甲酯和碳酸甲乙酯中的至少一种。
根据本发明的一些实施例，所述盐的水溶液的质量浓度为5～25％。
根据本发明的一些实施例，按体积比，所述废电解液、所述盐的水溶液和所述溶剂的体积比为1～3:1～3:1～3。
根据本发明的一些实施例，按体积比，所述废电解液、所述盐的水溶液和所述有机溶剂的体积比为1:1:1，2:1:1，2:2:1，2:1:2，1；3:3，3:1:1，3:2:1，3:3:1或3:1:3。
上述体积比下，上层有机相的密度不高于1.07g/cm3，下层负载锂相的密度约为1.15～1.5g/cm3，能够实现上层有机相和下层负载锂相的分层。
根据本发明的一些实施例，所述分层的时间为0.5～3h。所述分层的方法包括静置。
根据本发明的一些实施例，所述盐的水溶液包括硫酸盐的水溶液和氯化盐的水溶液中的至少一种。
根据本发明的一些实施例，所述硫酸盐的水溶液的溶质包括硫酸钾和硫酸钠中的至少一种。
根据本发明的一些实施例，所述氯化盐的水溶液的溶质包括氯化钠和氯化钾中的至少一种。
根据本发明的一些实施例，所述混合的温度为15～100℃。
根据本发明的一些实施例，所述混合的时间为5～30min。
根据本发明的一些实施例，所述混合借助搅拌实施，所述搅拌的搅拌速度为60～400r/min。
根据本发明的一些实施例，所述回收锂的方法还包括将所述上层有机相精馏。
根据本发明的一些实施例，所述精馏包括间歇精馏。
根据本发明的一些实施例，所述间歇精馏的温度为60～120℃，所述间歇精馏的压强为 10kPa～50kPa，所述间歇精馏的时间为10～30min。
在上述精馏条件下，能够实现碳酸二甲酯和碳酸甲乙酯的回收。
根据本发明的一些实施例，所述回收锂的方法还包括将所述下层负载锂相除杂得到液相产物。
根据本发明的一些实施例，所述除杂包括蒸馏。
根据本发明的一些实施例，所述蒸馏的温度为15℃～100℃，所述蒸馏的真空度为10kPa～70kPa，所述蒸馏的时间为10～45min。
所述蒸馏收取蒸馏残液和馏分；所述馏分的回收方法包括冷凝。
根据本发明的一些实施例，所述冷凝的温度为20～25℃。
根据本发明的一些实施例，所述回收锂的方法还包括以所述馏分作为萃取剂的溶剂。
根据本发明的一些实施例，所述回收锂的方法还包括将所述蒸馏残液和碳酸盐的水溶液混合。
根据本发明的一些实施例，所述碳酸盐的质量浓度为1％～15％。
根据本发明的一些实施例，所述碳酸盐的加入量为按照摩尔比，Li+：CO3 2-为2：1.2～1.4。
根据本发明的一些实施例，所述液相产物和碳酸盐的水溶液混合的时间为20～30min。
根据本发明的一些实施例，所述液相产物和所述碳酸盐的水溶液混合后，固液分离，分别收集固相产物和滤液。
根据本发明的一些实施例，所述滤液为压滤液。
根据本发明的一些实施例，收集所述滤液后还包括向所述滤液中加入酸。
根据本发明的一些实施例，所述加酸后的滤液的pH值0.5～1。
上述加酸的目的是除去滤液中的碳酸根。
根据本发明的一些实施例，还包括将所述加酸后的滤液的pH调节至6～7，得到所述盐溶液，作为萃取剂的一部分。
上述得到盐的水溶液可作为萃取剂的一部分循环使用。
根据本发明的一些优选地实施例，所述下层负载锂相除杂前还包括浓缩，所述浓缩包括以下步骤：
S1、向所述下层负载锂相中补充所述溶剂后作为所述萃取剂，对废电解液进行萃取，得到上层有机相和二次负载锂相；
S2、收集所述二次负载锂相后，补充所述溶剂，再次作为萃取剂，重复步骤S1的操作，至所得液相中的锂的含量为16～20g/L。
由此，可提升所述负载锂相中锂的含量。溶剂、盐的水溶液与废电解液混合时，会有少 量溶剂挥发，同时分层时也有少量溶剂进入到上层有机相(除锂电解液相)中，因此需要补充一定量的溶剂，不需要补充盐的水溶液。
根据本发明的一些优选地实施例，步骤S1中，按体积比，加入废电解液：下层负载锂相为1：1。
根据本发明的一些优选地实施例，步骤S1中，所述下层负载锂相的体积记为V1，步骤S2中，所述二次负载锂相的体积记为V2，步骤S2中所述溶剂的加入量为V2-V1。
分出的负载锂相，补充加入溶剂和废电解液后，负载锂相中的锂浓度会逐渐富集，有利于锂离子的沉淀。本发明通过在负载锂相除杂前补充加入废电解液和溶剂实现了富集负载锂相中的锂，有利于锂的回收。
本发明中废电解液与盐水和乙醇按上述加入量混合均匀，将电解液中的锂萃取出来，静置一段时间后，分层分液，得到上层有机相和下层负载锂相，负载锂相进行低温蒸馏，收集得到萃取剂中的溶剂乙醇，可进行循环萃取使用，蒸馏残液中加入碳酸盐，进行搅拌混合，过滤得到碳酸锂和滤液，滤液中加入强酸除去碳酸根后再调节pH得到萃取剂中的盐的水溶液，可作为萃取剂循环使用，上层有机相进行间歇式精馏得到碳酸二甲酯和碳酸甲乙酯。
附图说明
本发明的上述和/或附加的方面和优点从结合下面附图对实施例的描述中将变得明显和容易理解，其中：
图1是本发明实施例2中回收锂的方法的工艺流程图。
图2是本发明实施例1中回收锂的方法的工艺流程图。
具体实施方式
下面详细描述本发明的实施例，所述实施例的示例在附图中示出，其中自始至终相同或类似的标号表示相同或类似的元件或具有相同或类似功能的元件。下面通过参考附图描述的实施例是示例性的，仅用于解释本发明，而不能理解为对本发明的限制。
实施例1
本实施例公开了一种从锂离子电池电解液中回收锂的方法，其中，废旧三元锂电池中，各组分含量如下，按重量百分比计：30％碳酸二甲酯、33％碳酸乙烯酯、32％碳酸甲乙酯；锂9g/L。
具体步骤为：
S1、取废旧三元锂电池，放完电后扎孔收集2000ml的电解液(废旧锂离子电解液)，加 入1000ml质量浓度为15％的氯化钠盐水，再加入1000ml乙醇(乙醇质量浓度为100％)混合，混合的温度为50℃，搅拌速度为400r/min，洗涤15min，静置0.5h后分层，此时，上层有机相密度为0.9g/cm3，下层负载锂相的密度为1.15g/cm3，分液收集到下层负载锂相和上层的除锂电解液相；
S2、将除锂后的上层除锂电解液相进行间歇式精馏得到碳酸二甲酯和碳酸甲乙酯，间歇精馏的条件为80℃，30kPa，精馏20min；
S3、下层负载锂相补充100mL乙醇后和1L电解液，重复步骤S1，负载锂相中的锂浓度不断增加，最终体系中的负载锂相(二次负载锂相)的锂的含量为20g/L；
S4、在旋转蒸发器中80℃，30kPa，蒸20min将负载锂相中的乙醇蒸发出来，于20℃，冷凝收集萃取剂中的溶剂乙醇，测试蒸发乙醇后的残留液中的锂的含量，按照摩尔比，Li+/CO3 2-为2/1.2加入10％的碳酸钠溶液，搅拌反应20min后进行压滤，得到碳酸锂沉淀和滤液；
S5、将步骤S4中滤液加入盐酸调pH至1除去CO3 2-，再加氢氧化钠调节pH至7后得到萃取剂中的盐的水溶液。实现盐的水溶液的循环利用。
图2是本发明实施例1中回收锂的方法的工艺流程图。
通过icp元素测试，步骤S1中，上层的除锂电解液相中锂含量为0.01g/L，下层得到碳酸锂沉淀后，此部分锂的提取率为99％，计算方法为：(9-0.01)/9＝99％。
提取率计算方法为(电解液中锂的含量-步骤S1中进行分层后的上层除锂电解液相中的锂含量)/电解液中锂的含量。
采用GCMS气质联用进行定性和定量分析测试，步骤S2中，碳酸二甲酯的回收率为80％，碳酸甲乙酯的回收率为75％。
实施例2
本实施例公开了一种从锂离子电池电解液中回收锂的方法，其中，废旧三元锂电池中，各组分含量如下，按重量百分比计：30％碳酸二甲酯、33％碳酸乙烯酯、32％碳酸甲乙酯；锂9g/L。
具体步骤为：
S1、取废旧三元锂电池，放完电后扎孔收集2000ml的电解液，加入1000ml质量浓度为5％的氯化钠盐水，再加入1000ml乙醇混合，混合的温度为50℃，搅拌速度为400r/min，洗涤15min，静置0.5h后分层，分液收集到下层负载锂相和上层的除锂电解液相；
S2、将除锂后的上层除锂电解液相进行间歇式精馏得到碳酸二甲酯和碳酸甲乙酯，间歇精馏的条件为80℃，30kPa，精馏20min；
S3、在旋转蒸发器中将负载锂相中的乙醇蒸发出来，真空度为30kPa，温度为60℃反应40min，25℃冷凝收集萃取剂中的溶剂乙醇，测试蒸发乙醇后的残留液中的锂的含量，按照摩尔比，Li+/CO3 2-为2/1.2加入5％的碳酸钠溶液，搅拌反应20min后进行压滤，得到碳酸锂沉淀和滤液；
S4、将步骤S3中滤液加入盐酸调pH至1除去碳酸根，再加氢氧化钠调节pH至7后得到萃取剂中的盐的水溶液。
通过icp元素测试，步骤S1中，上层的除锂电解液相中锂含量为0.01g/L，下层得到碳酸锂沉淀，此部分锂的提取率为99％。
采用GCMS气质联用进行定性和定量分析测试，步骤S2中，碳酸二甲酯的回收率为85％，碳酸甲乙酯的回收率为75％。
图1是本发明实施例2中回收锂的方法的工艺流程图。
实施例3
本实施例公开了一种从锂离子电池电解液中回收锂的方法，其中，废旧三元锂电池中，各组分含量如下，按重量百分比计：30％碳酸二甲酯、33％碳酸乙烯酯、32％碳酸甲乙酯；锂9g/L，具体步骤为：
S1、取废旧三元锂电池，放完电后扎孔收集1000ml的电解液，加入1000ml实施例1步骤S5中的盐的水溶液，再加入实施例1步骤S4中冷凝回收的乙醇1000ml混合，混合的温度为80℃，搅拌速度为400r/min，洗涤15min，静置0.5h后分层，此时，上层有机相密度为0.9g/cm3，下层负载锂相的密度为1.3g/cm3，分液收集到下层负载锂相和上层的除锂电解液相；
S2、将除锂后的上层除锂电解液相进行间歇式精馏得到碳酸二甲酯和碳酸甲乙酯，间歇精馏的条件为80℃，30kPa，精馏20min；
S3、下层负载锂相补充一定体积的乙醇和电解液后，多次循环洗后，负载锂相中的锂浓度不断增加，进行后续的乙醇回收和提锂；
S4、在旋转蒸发器中将负载锂相中的乙醇蒸发出来，真空度为30kPa，温度为60℃反应40min，于20℃，冷凝收集萃取剂中的溶剂乙醇，测试蒸发乙醇后的残留液中的锂的含量，按照摩尔比，Li+/CO3 2-为2/1.2加入10％的碳酸钠溶液，搅拌反应20min后进行压滤，得到碳酸锂沉淀和滤液；
S5、将步骤S4中滤液加入盐酸调pH至1除去碳酸根，再加氢氧化钠调节pH至7后得到萃取剂中的盐的水溶液。
通过icp元素测试，步骤S1中，上层的除锂电解液相中锂含量为0.01g/L，下层得到碳酸锂沉淀后,此部分锂的提取率为99％。
采用GCMS气质联用进行定性和定量分析测试，步骤S2中，碳酸二甲酯的回收率为80％，碳酸甲乙酯的回收率为70％。
对比例1
本对比例公开了一种从锂离子电池电解液中回收锂的方法，本对比例和实施例1的区别在于，本对比例中没有加入实施例1步骤S1的乙醇，其余条件和实施例1相同。
按照上述步骤没有得到碳酸锂沉淀。盐的水溶液和乙醇共同作用下，将电解液进行分层并将锂萃取出来，缺少乙醇后无法萃取锂，因此无法在后续步骤中形成碳酸锂的沉淀。
对比例2
本对比例公开了一种从锂离子电池电解液中回收锂的方法，本对比例和实施例1的区别在于，本对比例中没有加入实施例1步骤S1的15％的氯化钠盐水，其余条件和实施例1相同。
按照上述步骤无法收集到负载锂相和除锂电解液相。溶液和乙醇共同作用下，乙醇将电解液中的锂萃取出来，盐水主要起到分层作用，缺少盐水后上层有机相和下层负载锂相的密度相近，无法实现分层，因而无法收集到负载锂相和除锂电解液相。
对比例3
本对比例公开了一种从锂离子电池电解液中回收锂的方法，本对比例和实施例1的区别在于，本对比例中上层有机相的密度为1.1g/cm3，其余条件和实施例1相同。
该条件下，上层有机相和下层负载锂相的密度相近，无法实现分层，因而无法收集到负载锂相和除锂电解液相。
对比例4
本对比例公开了一种从锂离子电池电解液中回收锂的方法，本对比例和实施例1的区别在于，本对比例中下层负载锂相的密度为1.0g/cm3，其余条件和实施例1相同。
该条件下，上层有机相和下层负载锂相的密度相近，无法实现分层，因而无法收集到负载锂相和除锂电解液相。
对比例5
本对比例公开了一种从锂离子电池电解液中回收锂的方法，本对比例和实施例1的区别在于，本对比例中下层负载锂相的密度为1.6g/cm3，其余条件和实施例1相同。
通过icp元素测试，步骤S1中，上层的除锂电解液相中锂含量为0.12g/L，下层得到碳酸锂沉淀后，此部分锂的提取率为98％。
采用GCMS气质联用进行定性和定量分析测试，步骤S2中，碳酸二甲酯的回收率为80％，碳酸甲乙酯的回收率为70％。
该条件下，盐水溶液的用量过大，造成不必要的浪费，增加了后续处理盐水溶液的难度。 其除锂效果和实施例相比出现了下降。
上面结合附图对本发明实施例作了详细说明，但本发明不限于上述实施例，在所属技术领域普通技术人员所具备的知识范围内，还可以在不脱离本发明宗旨的前提下作出各种变化。

Claims (10)

  1. 一种从锂离子电池电解液中回收锂的方法，其特征在于，包括将废电解液和萃取剂混合后分层，得到密度不高于1.07g/cm3的上层有机相和密度为1.15～1.5g/cm3的下层负载锂相；
    所述废电解液包括锂离子和酯类有机溶剂；
    所述萃取剂包括盐的水溶液和溶剂；
    所述溶剂包括乙醇和甲醇中的至少一种；
    所述上层有机相包括所述酯类有机溶剂；
    所述负载锂相包括水。
  2. 根据权利要求1所述的方法，其特征在于，所述盐的水溶液的质量浓度为5～25％；优选地，按体积比，所述废电解液、所述盐的水溶液和所述溶剂的体积比为1～3:1～3:1～3。
  3. 根据权利要求1所述的方法，其特征在于，所述混合的温度为15～100℃。
  4. 根据权利要求1所述的方法，其特征在于，所述混合的时间为5～30min。
  5. 根据权利要求1所述的方法，其特征在于，所述回收锂的方法还包括将所述上层有机相精馏。
  6. 根据权利要求1所述的方法，其特征在于，所述回收锂的方法还包括将所述下层负载锂相除杂得到液相产物；优选地，所述除杂包括蒸馏。
  7. 根据权利要求6所述的方法，其特征在于，所述蒸馏的温度为15℃～100℃，所述蒸馏的真空度为10kPa～70kPa，所述蒸馏的时间为10～45min。
  8. 根据权利要求6所述的方法，其特征在于，所述回收锂的方法还包括将所述液相产物和碳酸盐的水溶液混合。
  9. 根据权利要求8所述的方法，其特征在于，所述碳酸盐的质量浓度为1％～15％。
  10. 根据权利要求6所述的方法，其特征在于，所述下层负载锂相除杂前还包括加入废电解液和所述溶剂混合后分层，得到上层有机相和下层负载锂相，收集下层负载锂相后重复加入废电解液和所述溶剂至下层负载锂相中的锂的含量为16～20g/L。
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