WO2023087800A1 - 一种从废旧磷酸铁锂电池中回收制备正极材料的方法 - Google Patents

一种从废旧磷酸铁锂电池中回收制备正极材料的方法 Download PDF

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WO2023087800A1
WO2023087800A1 PCT/CN2022/111816 CN2022111816W WO2023087800A1 WO 2023087800 A1 WO2023087800 A1 WO 2023087800A1 CN 2022111816 W CN2022111816 W CN 2022111816W WO 2023087800 A1 WO2023087800 A1 WO 2023087800A1
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black powder
positive electrode
solid
iron phosphate
lithium iron
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PCT/CN2022/111816
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English (en)
French (fr)
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余海军
李爱霞
谢英豪
李长东
张学梅
钟应声
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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
宜昌邦普时代新能源有限公司
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Priority to GB2313003.2A priority Critical patent/GB2620690B/en
Priority to US18/260,005 priority patent/US12009492B2/en
Priority to DE112022000199.2T priority patent/DE112022000199T5/de
Priority to ES202390075A priority patent/ES2963369A2/es
Publication of WO2023087800A1 publication Critical patent/WO2023087800A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B25/00—Phosphorus; Compounds thereof
    • C01B25/16—Oxyacids of phosphorus; Salts thereof
    • C01B25/26—Phosphates
    • C01B25/45—Phosphates containing plural metal, or metal and ammonium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B82—NANOTECHNOLOGY
    • B82Y—SPECIFIC USES OR APPLICATIONS OF NANOSTRUCTURES; MEASUREMENT OR ANALYSIS OF NANOSTRUCTURES; MANUFACTURE OR TREATMENT OF NANOSTRUCTURES
    • B82Y30/00—Nanotechnology for materials or surface science, e.g. nanocomposites
    • 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
    • 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
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M4/00—Electrodes
    • H01M4/02—Electrodes composed of, or comprising, active material
    • H01M4/13—Electrodes for accumulators with non-aqueous electrolyte, e.g. for lithium-accumulators; Processes of manufacture thereof
    • H01M4/139—Processes of manufacture
    • H01M4/1397—Processes of manufacture of electrodes based on inorganic compounds other than oxides or hydroxides, e.g. sulfides, selenides, tellurides, halogenides or LiCoFy
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M4/00—Electrodes
    • H01M4/02—Electrodes composed of, or comprising, active material
    • H01M4/36—Selection of substances as active materials, active masses, active liquids
    • H01M4/58—Selection of substances as active materials, active masses, active liquids of inorganic compounds other than oxides or hydroxides, e.g. sulfides, selenides, tellurides, halogenides or LiCoFy; of polyanionic structures, e.g. phosphates, silicates or borates
    • H01M4/5825—Oxygenated metallic salts or polyanionic structures, e.g. borates, phosphates, silicates, olivines
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2004/00—Particle morphology
    • C01P2004/01—Particle morphology depicted by an image
    • C01P2004/03—Particle morphology depicted by an image obtained by SEM
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2004/00—Particle morphology
    • C01P2004/60—Particles characterised by their size
    • C01P2004/64—Nanometer sized, i.e. from 1-100 nanometer
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2006/00—Physical properties of inorganic compounds
    • C01P2006/40—Electric properties
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M4/00—Electrodes
    • H01M4/02—Electrodes composed of, or comprising, active material
    • H01M2004/026—Electrodes composed of, or comprising, active material characterised by the polarity
    • H01M2004/028—Positive electrodes
    • 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, and in particular relates to a method for recycling and preparing positive electrode materials from waste lithium iron phosphate batteries.
  • lithium iron phosphate batteries Although the working voltage platform and capacity density of lithium iron phosphate batteries are inferior to those of transition metal oxide batteries such as nickel cobalt lithium manganese oxide and lithium manganese oxide, their performance in charge and discharge cycle life, safety, thermal stability and The manufacturing cost is superior to the transition metal oxide type battery. Therefore, in the pursuit of long-life, low-cost and easy-to-use batteries, lithium iron phosphate batteries have become the preferred choice for power storage and power batteries. With the development of the lithium iron phosphate battery industry, it can be expected that there will be a large number of replaced waste lithium iron phosphate batteries in the future. Therefore, how to deal with and recycle waste lithium iron phosphate batteries will also become a big problem.
  • transition metal oxide batteries such as nickel cobalt lithium manganese oxide and lithium manganese oxide
  • the recycling of waste lithium iron phosphate batteries generally includes the following steps: first, classify the batteries according to their chemical composition, then physically disassemble them, then perform high-temperature calcination, crushing and sorting, and extract the electrolyte.
  • the waste polyanion battery will be affected by the broken shell, pulverized current collector and separator during the mechanical crushing process, which will change the physical and chemical composition of the positive electrode material to be recycled.
  • the crushing process destroys the internal arrangement of the cathode material crystals; on the other hand, the crushing process mixes copper, aluminum, phosphate, electrolyte, and binder together, which increases the difficulty of the subsequent purification process.
  • the present invention aims to solve at least one of the technical problems in the above-mentioned prior art. For this reason, the present invention proposes a method for recycling and preparing positive electrode materials from waste lithium iron phosphate batteries. While controlling the recycling cost, high-purity positive electrode materials can be recovered, and the batteries prepared again by using the recycled positive electrode materials have good performance. .
  • the invention provides a method for recycling and preparing positive electrode materials from waste lithium iron phosphate batteries.
  • a method for recycling and preparing positive electrode materials from waste lithium iron phosphate batteries comprises the following steps:
  • step (1) the black powder that step (1) obtains is mixed with benzene sulfonate, then reacts in fluidized bed, obtains the black powder that sloughs off carbon, fluorine;
  • step (3) Add acid to the black powder that removes carbon and fluorine described in step (2), and solid-liquid separation obtains solution A and solid A; Liquid separation obtains solution B and solid B;
  • step (3) Mix solid A and solution B obtained in step (3), add at least one of lithium supplement, iron supplement or phosphate to obtain a mixture, then add a reducing agent to the mixture, sinter, and prepare get the positive electrode material.
  • the discharge process is to place the waste lithium iron phosphate battery in a metal salt solution and discharge for 0.1-10d.
  • the metal salt is selected from one or more of sodium chloride, sodium sulfate, sodium phosphate, magnesium chloride, magnesium sulfate, lithium sulfate or lithium chloride.
  • the mass concentration of the metal salt is 0.1-20w%.
  • the drying process is to place the waste lithium iron phosphate battery in a sintering furnace, a kiln kiln, a muffle furnace, an electric furnace or an oven at 15-150°C, Dry 1-120h. It is also possible to place the waste lithium iron phosphate battery under solar radiation.
  • the crushing process is to shear the waste lithium iron phosphate battery 1-10 times to obtain a crushing block.
  • the area ratio of the broken pieces to the waste lithium iron phosphate battery is greater than 5%; further preferably, the area ratio of the broken pieces to the waste lithium iron phosphate battery is greater than 10%.
  • the peeling process is to place the broken pieces in the peeling liquid, heat once to separate the solid and the separating liquid; then heat the separating liquid twice to remove the peeling liquid. liquid to obtain black powder.
  • the solids are aluminum and copper foils which, after separation, are recycled.
  • the stripping solution includes polyhydric alcohol and phosphate ester.
  • the waste lithium iron phosphate pole pieces are broken smaller, and the corresponding electrode materials contain more aluminum-copper debris or aluminum-copper powder, which is not conducive to later removal , so that the content of aluminum and copper in the final positive electrode material is high, which affects its performance.
  • the inventors have found that by controlling the size of the broken pieces after shearing and using a stripping solution comprising polyols and phosphoric acid esters for stripping treatment, the stripping solution hardly produces aluminum-copper debris, which can reduce the amount of aluminum-copper in the final positive electrode material. content, and the stripping fluid can be recycled.
  • the polyhydric alcohol is selected from at least one of ethylene glycol, propylene glycol, glycerol, isopropanol, butanol, 1,2-butanediol or 1,3 butanediol.
  • the phosphoric acid ester is selected from at least one of phosphoric acid monoester, phosphoric acid diester, phosphoric acid triester, triethyl phosphate or trimethyl phosphate.
  • the volume ratio of the polyol to the phosphate is 1:(0.1-1); further preferably, the volume ratio of the polyol to the phosphate is 1:(0.3-0.8).
  • the temperature of the primary heating is 130-210°C, and the time of the primary heating is 0.5-10h; further preferably, the temperature of the primary heating is 160-210°C, and the time of the primary heating is 1 -8h.
  • the temperature of the secondary heating is 210-300° C., and the time of the secondary heating is 2-12 hours.
  • the benzenesulfonate is at least one selected from sodium p-toluenesulfonate, sodium toluenesulfonate, sodium benzenesulfonate or zinc benzenesulfonate.
  • Pyrolysis of benzenesulfonate produces sulfur dioxide and water, which can promote the heating of the separator (polyethylene, polypropylene), electrolyte (LiClO 4 , LiPF 6 , carbonate), and binder (polyvinylidene fluoride) in the black powder. solution, which is beneficial to remove fluorine and decarburization.
  • the added amount of the benzenesulfonate is 0.1-5w% of the black powder; more preferably, the added amount of the benzenesulfonate is 0.1-3w% of the black powder.
  • the temperature of the reaction is 300-850°C, and the reaction time is 1-360min; more preferably, in step (2), the temperature of the reaction is 400-750°C , The reaction time is 30-240min.
  • the gas in the fluidized bed includes at least one of oxygen, carbon dioxide or nitrogen.
  • the mass percentage of carbon in the black powder from which carbon and fluorine have been removed is less than 2%.
  • a heating furnace is used to pyrolyze the black powder, and the heat released by the heating furnace is transmitted from the surface of the black powder to the interior, not only part of the heat cannot be transferred in, but heat loss is easily generated, and the interior requires a long heating time.
  • the heating furnace cannot fully pyrolyze the separator (polyethylene, polypropylene), electrolyte (LiClO 4 , LiPF 6 , carbonate), binder (polyvinylidene fluoride) and other substances in the black powder.
  • the present invention adopts the method of fluidized bed pyrolysis, cooperates with the use of benzenesulfonate, the black powder layer is heated at a uniform temperature, can avoid local overheating, is easy to flow between equipment, has large transport capacity, and is suitable for large-scale pyrolysis .
  • the sulfur dioxide and water produced by the thermal decomposition of benzenesulfonate promote the thermal decomposition of the separator (polyethylene, polypropylene), electrolyte (LiClO 4 , LiPF 6 , carbonate), and binder (polyvinylidene fluoride) in the black powder.
  • the combined use of the two can make the pyrolysis of fluorine and carbon substances in the black powder more thorough, which is beneficial to the removal of carbon and fluorine in the black powder.
  • the acid is at least one selected from phosphoric acid, formic acid, lactic acid, citric acid, oxalic acid or acetic acid.
  • the molar concentration of the acid is 0.01-6 mol/L.
  • the alkali is selected from calcium hydroxide and/or magnesium hydroxide.
  • step (3) the solid A is iron phosphate, the solution A is a solution containing lithium hydroxide, the solution B is a lithium hydroxide solution, and the solid B is aluminum hydroxide and copper hydroxide.
  • the lithium supplement agent is selected from at least one of lithium carbonate, lithium oxalate or lithium phosphate.
  • the iron supplement is at least one selected from ferric hydroxide, ferric phosphate, ferric oxalate, ferrous oxalate, ferric citrate or ferrous citrate.
  • the phosphate is selected from at least one of ammonium phosphate, ammonium hydrogen phosphate, sodium phosphate, ferrous phosphate, ferric phosphate or phosphoric acid.
  • the molar ratio of lithium:iron:phosphate in the mixture is (0.1-20):(0.1-20):(0.1-20).
  • the reducing agent is selected from at least one of glucose, fructose or starch.
  • the added amount of the reducing agent accounts for 1-25w% of the mixture.
  • the method proposed by the present invention to recycle and prepare positive electrode materials from waste lithium iron phosphate batteries can recycle to obtain pure High positive electrode material, the battery prepared again by using the recycled positive electrode material has good performance.
  • the recovery method provided by the present invention can not only effectively reduce the content of aluminum, copper, carbon, and fluorine in the black powder, but also only need to make up iron or lithium when regenerating the positive electrode material, and it can be reduced by carbon heat.
  • Fig. 1 is the process flow diagram among the embodiment 1;
  • Fig. 2 is the SEM picture of the lithium iron phosphate cathode material that embodiment 1 makes;
  • FIG. 3 is a diagram of the discharge cycle performance of a button battery assembled using the lithium iron phosphate cathode material provided in Comparative Example 1 and Example 4.
  • FIG. 3 is a diagram of the discharge cycle performance of a button battery assembled using the lithium iron phosphate cathode material provided in Comparative Example 1 and Example 4.
  • the raw materials, reagents or devices used in the following examples can be obtained from conventional commercial channels, or can be obtained by existing known methods.
  • Battery pre-treatment Place 38.3kg of recovered waste lithium iron phosphate batteries in tap water containing 1.7% sodium chloride (mass concentration), discharge for 4 days, and then dry the internal electrolyte of the battery under solar radiation. Then cut the battery 3 times to obtain broken pieces, so that the ratio of the area of the broken pieces (pole pieces) to the area of the battery is about 30%. Put the broken pieces in the stripping solution (the volume ratio of glycerol and triethyl phosphate is 1:0.5), and be submerged by the stripping solution.
  • the heating equipment is heated to 170°C, kept warm for 2h 20min, stirred, sieved and separated to obtain solid and separated
  • the solid is aluminum and copper foil, which are recovered; continue to heat the separation liquid containing the flake active substance, keep it warm at 225°C for 3h 30min, and recover the stripping liquid, separate the flake active substance, and grind the flake active substance , Demagnetization obtains 9.2kg black powder.
  • a method for reclaiming and preparing positive electrode materials from waste lithium iron phosphate batteries comprising the following steps:
  • Battery pre-treatment Put 23.4kg of recovered waste lithium iron phosphate batteries in tap water containing 1.7% sodium chloride (mass concentration), discharge for 4 days, and then dry the electrolyte inside the battery under solar radiation. Then cut the battery three times to obtain broken pieces, so that the ratio of the area of the broken pieces to the area of the battery is about 30%.
  • step (2) Decarburization, fluorine: add 20.0g sodium p-toluenesulfonate to the black powder obtained in step (1), mix; open the heater and pump of the fluidized bed, heat, pump air, and mix the black powder Pump to the combustion chamber for reaction, control the heating temperature of the combustion chamber to about 550°C, burn, cool down, and recycle to obtain 4.6kg of decarburized and fluorine black powder.
  • a method for reclaiming and preparing positive electrode materials from waste lithium iron phosphate batteries comprising the following steps:
  • Battery pre-treatment Place 50.2kg of recovered waste lithium iron phosphate batteries in tap water containing 1.7% sodium chloride (mass concentration), discharge for 4 days, and then dry the electrolyte inside the battery under solar radiation. Then cut the battery 3 times to obtain broken pieces, so that the ratio of the area of the broken pieces to the area of the battery is about 30%.
  • step (2) Decarburization, fluorine: Add 32.0g sodium p-toluenesulfonate to the black powder obtained in step (1), mix; open the heater and pump of the fluidized bed, heat, pump air, and mix the black powder Pump to the combustion chamber for reaction, control the heating temperature of the combustion chamber to about 570°C, burn, cool down, and recover 9.3kg of decarburized and fluorine black powder.
  • a method for reclaiming and preparing positive electrode materials from waste lithium iron phosphate batteries comprising the following steps:
  • Battery pre-treatment Place 46.5kg of recovered waste lithium iron phosphate batteries in tap water containing 1.7% sodium chloride (mass concentration), discharge for 4 days, and then dry the internal electrolyte of the battery under solar radiation. Then cut the battery three times to obtain broken pieces, so that the ratio of the area of the broken pieces to the area of the battery is about 20%.
  • step (2) Decarburization, fluorine: Add 32.0g sodium p-toluenesulfonate to the black powder obtained in step (1), mix; open the heater and pump of the fluidized bed, heat, pump air, and mix the black powder Pump it to the combustion chamber for reaction, control the heating temperature of the combustion chamber to about 560°C, burn, cool down, and recover 8.9kg of decarburized and fluorine black powder.
  • a method for reclaiming and preparing positive electrode materials from waste lithium iron phosphate batteries comprising the following steps:
  • Battery pre-treatment Put 42.7kg of recovered waste lithium iron phosphate batteries in tap water containing 1.7% sodium chloride (mass concentration), discharge for 4 days, and then dry the internal electrolyte of the battery under solar radiation. Then cut the battery three times to obtain broken pieces, so that the ratio of the area of the broken pieces to the area of the battery is about 30%.
  • the stripping solution (volume ratio of glycerol to triethyl phosphate is 1:0.6), covered by the stripping solution, heat up the heating equipment to 180°C, keep warm for 2h 40min, stir, and sieve to separate the solid and separate Liquid, the solid is aluminum, copper foil, for recycling; continue to heat the separation liquid containing the flake-shaped active substance at 244°C until it no longer changes, and recover the stripping liquid to separate the flake-shaped active substance, which is ground and removed Magnetically obtained 9.4kg black powder.
  • step (2) Decarburization and fluorine: add 35.0g sodium p-toluenesulfonate to the black powder obtained in step (1), mix; open the heater and pump of the fluidized bed, heat, pump air, and mix the black powder Pump to the combustion chamber for reaction, control the heating temperature of the combustion chamber to about 570°C, burn, cool down, and recover to obtain 7.4kg of decarburized and fluorine black powder.
  • step (2) decarburization and fluorine treatment uses a conventional heating tube for decarburization and fluorine.
  • the black powder is sent to a tube furnace and heated at 510°C for 8 hours for decarburization and fluorine. All the other steps are the same as in Example 1.
  • step (2) no sodium p-toluenesulfonate is added, and only a fluidized bed is used for decarburization and fluorine. All the other steps are the same as in Example 1.
  • the assembly of the lithium-ion button cell is carried out in a glove box full of neon gas, with the prepared electrode sheet as the positive electrode, 1.0mol/LiPF 6 (the solvent is ethylene carbonate) as the electrolyte, and the shell, shrapnel, gasket, negative electrode (metal lithium sheet), 0.25mL electrolyte, diaphragm (polypropylene film), positive electrode (electrode sheet), and shell are assembled in sequence, and the coin cell is packaged.
  • the prepared electrode sheet as the positive electrode
  • 1.0mol/LiPF 6 the solvent is ethylene carbonate
  • the shell shrapnel, gasket, negative electrode (metal lithium sheet), 0.25mL electrolyte, diaphragm (polypropylene film), positive electrode (electrode sheet), and shell are assembled in sequence, and the coin cell is packaged.
  • test the charge and discharge performance of the assembled battery Then on the constant current charge and discharge test equipment, test the charge and discharge performance of the assembled battery. Test conditions: the voltage range is 2.0-3.5V, the test rate is 0.5C (152mAh ⁇ g -1 ), and the results of 30 cycles at 0.5C rate are shown in Table 2.
  • FIG. 3 is a diagram of the discharge cycle performance of a button battery assembled using the lithium iron phosphate cathode material provided in Comparative Example 1 and Example 4.
  • FIG. 3 the abscissa is the number of cycles, and the ordinate is the discharge capacity.
  • the 30-time discharge capacity of the button battery of Comparative Example 1 is 154.3-156.2mAh g -1
  • the 30-time discharge capacity of the button battery of Example 4 is 155.6-156.4mAh g -1
  • the lithium iron phosphate provided by Example 4 The cycle stability of the cathode material is better.

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Abstract

一种从废旧磷酸铁锂电池中回收制备正极材料的方法。该方法包括以下步骤：将废旧磷酸铁锂电池放电、破碎、剥离，得到黑粉；然后将黑粉与苯磺酸盐混合，于流化床中反应；再加入酸、碱去杂，最后加入补锂剂、补铁剂或磷酸盐，以及还原剂，经烧结制得。该方法通过对破碎、剥离、脱碳氟以及除杂过程的控制和优化，在控制回收成本的同时，能够回收得到纯度高的正极材料，利用回收的正极材料再次制备的电池具有良好性能。该方法不仅能够有效减少黑粉中的铝、铜、碳、氟的含量，且在再生正极材料时，只需要补足铁或锂，经碳热还原即可。

Description

一种从废旧磷酸铁锂电池中回收制备正极材料的方法 技术领域
本发明属于电池材料回收技术领域，具体涉及一种从废旧磷酸铁锂电池中回收制备正极材料的方法。
背景技术
虽然，磷酸铁锂电池的工作电压平台、能力密度逊色于同类型的镍钴锰酸锂、锰酸锂等过渡金属氧化物型电池，但其在充放电循环寿命、安全性、热稳定性和制造成本上均优于过渡金属氧化物型电池。因此，在追求长寿命、低成本和易使用的电池诉求下，磷酸铁锂电池成为了电力储能及动力电池的优先选择。随着磷酸铁锂电池产业的发展，可以预期的是，未来将面对大量更替下来的废旧磷酸铁锂电池。因此如何处理和回收废旧磷酸铁锂电池也将成为一大难题。
目前，废旧磷酸铁锂电池的回收处理一般包括以下步骤：首先是按照电池化学成分对其行分类，然后进行物理拆卸，再进行高温煅烧和破碎分选，以及电解液提取。该回收处理方法仍然存在一些问题，例如废旧聚阴离子型电池会在机械破碎过程中，受到破碎外壳、粉碎集流体和隔膜的影响，使待回收的正极材料的物理、化学成分发生变化。一方面，破碎过程破坏了正极材料晶体内部排列；另一方面，破碎过程使铜铝、磷酸根与电解液、粘结剂混合在一起，增加了后续提纯工艺的难度。尤其是铝铜箔的破碎，使其相互混合，无法采用机械分离过程将其精确分离出来。从而使得回收成本高，回收的正极材料纯度低，再次制备的电池无法满足性能要求，这也一定程度上限制了磷酸铁锂电池的工业应用和推广。
因此，亟需提供一种从废旧磷酸铁锂电池中回收制备正极材料的方法，在控制回收成本的同时，能够回收得到纯度高的正极材料，利用回收的正极材料再次制备的电池具有良好性能。
发明内容
本发明旨在至少解决上述现有技术中存在的技术问题之一。为此，本发明提出一种从废旧磷酸铁锂电池中回收制备正极材料的方法，在控制回收成本的同时，能够回收得到纯度高 的正极材料，利用回收的正极材料再次制备的电池具有良好性能。
本发明提供了一种从废旧磷酸铁锂电池中回收制备正极材料的方法。
具体的，一种从废旧磷酸铁锂电池中回收制备正极材料的方法，包括以下步骤：
(1)将废旧磷酸铁锂电池放电，干燥所述废旧磷酸铁锂电池内部的电解液，然后破碎得破碎块，再将所述破碎块剥离，得到黑粉；
(2)将步骤(1)得到的黑粉与苯磺酸盐混合，然后于流化床中反应，得到脱去碳、氟的黑粉；
(3)向步骤(2)中所述脱去碳、氟的黑粉中加入酸，固液分离得到溶液A和固体A；然后向所述溶液A中加入碱至沉淀不再生成为止，固液分离得到溶液B和固体B；
(4)将步骤(3)得到的固体A和溶液B混合，加入补锂剂、补铁剂或磷酸盐中的至少一种，得到混合物，然后向所述混合物中加入还原剂，烧结，制得正极材料。
优选的，在步骤(1)中，所述放电的过程为将所述废旧磷酸铁锂电池置于金属盐的溶液中，放电0.1-10d。
优选的，所述金属盐选自氯化钠、硫酸钠、磷酸钠、氯化镁、硫酸镁、硫酸锂或氯化锂中的一种或多种。
优选的，在所述金属盐的溶液中，所述金属盐的质量浓度分别为0.1-20w％。
优选的，在步骤(1)中，所述干燥的过程为将所述废旧磷酸铁锂电池置于烧结炉、锟道窑炉、马弗炉、电炉或烘箱中，于15-150℃下，干燥1-120h。也可以是将所述废旧磷酸铁锂电池置于太阳辐射下。
优选的，在步骤(1)中，所述破碎的过程为将所述废旧磷酸铁锂电池剪切1-10次，得到破碎快。
优选的，所述破碎块与所述废旧磷酸铁锂电池的面积比大于5％；进一步优选的，所述破碎块与所述废旧磷酸铁锂电池的面积比大于10％。
优选的，在步骤(1)中，所述剥离的过程为将所述破碎块置于剥离液中，一次加热，分离得固体和分离液；然后将所述分离液进行二次加热，去除剥离液，得到黑粉。所述固体为铝和铜箔，分离之后，进行回收。
优选的，所述剥离液包括多元醇和磷酸酯。
废旧磷酸铁锂电池在破碎过程中，随着剪切次数的增多，废旧磷酸铁锂极片被破碎的越小，相应的电极材料中铝铜碎屑或铝铜粉更多，不利于后期去除，使最终制备的正极材料中铝铜含量高，影响其性能。发明人发现，通过控制剪切后破碎块的大小，配合使用包含多元醇和磷酸酯的剥离液进行剥离处理，剥离液几乎不产生的铝铜碎屑，能够降低最终制备的正极材料中的铝铜含量，且剥离液能够循环使用。
优选的，所述多元醇选自乙二醇、丙二醇、丙三醇、异丙醇、丁醇、1，2-丁二醇或1，3丁二醇中的至少一种。
优选的，所述磷酸酯选自磷酸一酯、磷酸二酯、磷酸三酯、磷酸三乙酯或磷酸三甲酯中的至少一种。
优选的，所述多元醇与所述磷酸酯的体积比为1：(0.1-1)；进一步优选的，所述多元醇与所述磷酸酯的体积比为1：(0.3-0.8)。
优选的，所述一次加热的温度为130-210℃，所述一次加热的时间为0.5-10h；进一步优选的，所述一次加热的温度为160-210℃，所述一次加热的时间为1-8h。
优选的，所述二次加热的温度为210-300℃，所述二次加热的时间为2-12h。
优选的，在步骤(2)中，所述苯磺酸盐选自对甲苯磺酸钠、甲苯磺酸钠、苯磺酸钠或苯磺酸锌中的至少一种。苯磺酸盐高温分解，产生二氧化硫、水，能够促进所述黑粉中隔膜(聚乙烯、聚丙烯)、电解液(LiClO 4、LiPF 6、碳酸酯)、黏结剂(聚偏氟乙烯)热解，利于脱去氟、脱碳。
优选的，在步骤(2)中，所述苯磺酸盐加入量为黑粉0.1-5w％；进一步优选的，所述苯磺酸盐加入量为黑粉0.1-3w％。
优选的，在步骤(2)中，所述反应的温度为300-850℃，反应的时间为1-360min；进一步优选的，在步骤(2)中，所述反应的温度为400-750℃，反应的时间为30-240min。
优选的，所述流化床中的气体包括氧气、二氧化碳或氮气中的至少一种。
优选的，步骤(2)中，所述脱去碳、氟的黑粉中碳的质量百分数小于2％。
在传统的方法中，热解黑粉采用加热炉，加热炉释放的热量由黑粉表面传到内部，不仅部分热量无法传递进去，极易产生热的损耗，而且内部需要较长的加热时间，加热炉无法充分热解黑粉中的隔膜(聚乙烯、聚丙烯)、电解液(LiClO 4、LiPF 6、碳酸酯)、黏结剂(聚 偏氟乙烯)等物质。本发明采用流化床热解的方式，配合苯磺酸盐的使用，黑粉层受热的温度均匀，能避免了局部过热，易于在设备之间流动，输送能力大，适合于大规模热解。而苯磺酸盐受热分解生成的二氧化硫、水，促进黑粉中隔膜(聚乙烯、聚丙烯)、电解液(LiClO 4、LiPF 6、碳酸酯)、黏结剂(聚偏氟乙烯)热解。两者配合使用，使黑粉中含氟、碳物质的热解更彻底，有利于脱去黑粉中的碳、氟。
优选的，在步骤(3)中，所述酸选自磷酸、甲酸、乳酸、柠檬酸、草酸或乙酸中的至少一种。
优选的，在步骤(3)中，所述酸的摩尔浓度为0.01-6mol/L。
优选的，在步骤(3)中，所述碱选自氢氧化钙和/或氢氧化镁。
在步骤(3)中，所述固体A为磷酸铁，所述溶液A为含杂氢氧化锂溶液，所述溶液B为氢氧化锂溶液，所述固体B为氢氧化铝、氢氧化铜。
优选的，在步骤(4)中，所述补锂剂选自碳酸锂、草酸锂或磷酸锂中的至少一种。
优选的，在步骤(4)中，所述补铁剂选自氢氧化铁、磷酸铁、草酸铁、草酸亚铁、柠檬酸铁或柠檬酸亚铁中的至少一种。
优选的，在步骤(4)中，所述磷酸盐选自磷酸铵、磷酸氢铵、磷酸钠、磷酸亚铁、磷酸铁或磷酸中的至少一种。
优选的，在步骤(4)中，所述混合物中锂：铁：磷酸根的摩尔比为(0.1-20)：(0.1-20)：(0.1-20)。
优选的，在步骤(4)中，还原剂选自葡萄糖、果糖或淀粉中的至少一种。
优选的，在步骤(4)中，所述还原剂加入量占所述混合物的1-25w％。
相对于现有技术，本发明的有益效果如下：
(1)本发明提出的从废旧磷酸铁锂电池中回收制备正极材料的方法，通过对破碎、剥离、脱碳氟以及除杂过程的控制和优化，在控制回收成本的同时，能够回收得到纯度高的正极材料，利用回收的正极材料再次制备的电池具有良好性能。
(2)本发明提供的回收方法，不仅能够有效减少黑粉中的铝、铜、碳、氟的含量，且在再生正极材料时，只需要补足铁或锂，经碳热还原即可。
附图说明
图1为实施例1中的工艺流程图；
图2为实施例1制得的磷酸铁锂正极材料的SEM图；
图3为利用对比例1、实施例4提供的磷酸铁锂正极材料组装的扣式电池的放电循环性能图。
具体实施方式
为了让本领域技术人员更加清楚明白本发明所述技术方案，现列举以下实施例进行说明。需要指出的是，以下实施例对本发明要求的保护范围不构成限制作用。
以下实施例中所用的原料、试剂或装置如无特殊说明，均可从常规商业途径得到，或者可以通过现有已知方法得到。
实施例1
一种从废旧磷酸铁锂电池中回收制备正极材料的方法，其工艺流程图见图1，包括以下步骤：
(1)电池前处理：将回收的38.3kg废旧磷酸铁锂电池置于含1.7％氯化钠(质量浓度)的自来水中，放电4d，然后置于太阳辐射下干燥电池内部电解液。再将电池剪切3次得破碎块，使破碎块(极片)的面积与电池的面积之比约为30％。将破碎块置于剥离液(丙三醇与磷酸三乙酯体积比为1：0.5)中，被剥离液覆没，加热设备升温至170℃，保温2h 20min，搅拌，过筛分离得到固体和分离液，固体为铝、铜箔，进行回收；将含片状活性物质的分离液继续加热，于225℃下保温3h 30min，并回收剥离液，分离出片状活性物质，片状活性物质经研磨、除磁得到9.2kg黑粉。
(2)脱碳、氟：向步骤(1)得到的黑粉中加入25.0g对甲苯磺酸钠，混合；开启流化床的加热器、泵机，加热，泵送空气，并将黑粉泵送至燃烧室进行反应，控制燃烧室加热温度约560℃，燃烧，降温，回收得到9.17kg脱碳、氟的黑粉。
(3)除杂：取1.0kg脱碳、氟的黑粉，用1mol/L磷酸酸洗，固液分离得固体A和溶液A，固体A加水洗涤，备用；向溶液A中加2.6g氢氧化钙，搅拌，调pH至沉淀不再增加，再固液分离得固体B和溶液B，溶液B为含氢氧化锂溶液。
(4)再生正极材料：将固体A和溶液B，混合蒸发除水，测定蒸发后固体中铁、锂、磷酸根摩尔比(mol)＝6.134：6.063：6.181，加0.048mol草酸亚铁、0.060mol碳酸锂(铁、锂、 磷酸根摩尔比(mol)＝6.182：6.181：6.183)，再加90g葡萄糖混合，球磨，于氖气环境下，加热至570℃，烧结8h 35min，降温，得到再生的磷酸铁锂正极材料。图2为磷酸铁锂正极材料的SEM图，图2中再生得到的磷酸铁锂正极材料大小在50nm左右，仅个别在50-150nm左右，颗粒大小均匀，粒径集中度高。
实施例2
一种从废旧磷酸铁锂电池中回收制备正极材料的方法，包括以下步骤：
(1)电池前处理：将回收的23.4kg废旧磷酸铁锂电池置于含1.7％氯化钠(质量浓度)的自来水中，放电4d，然后置于太阳辐射下干燥电池内部电解液。再将电池剪切3次得破碎块，使破碎块的面积与电池的面积之比约为30％。将破碎块置于剥离液(丙三醇与磷酸三乙酯体积比为1：0.5)中，被剥离液覆没，加热设备升温至160℃，保温2h 20min，搅拌，过筛分离得到固体和分离液，固体为铝、铜箔，进行回收；将含片状活性物质的分离液继续加热，于215℃下保温4h 25min，并回收剥离液，分离出片状活性物质，片状活性物质经研磨、除磁得到5.8kg黑粉。
(2)脱碳、氟：向步骤(1)得到的黑粉中加入20.0g对甲苯磺酸钠，混合；开启流化床的加热器、泵机，加热，泵送空气，并将黑粉泵送至燃烧室进行反应，控制燃烧室加热温度约550℃，燃烧，降温，回收得到4.6kg脱碳、氟的黑粉。
(3)除杂：取1.0kg脱碳、氟的黑粉，用1mol/L磷酸酸洗，固液分离得固体A和溶液A，固体A加水洗涤，备用；向溶液A中加2.6g氢氧化钙，搅拌，调pH至沉淀不再增加，再固液分离得固体B和溶液B，溶液B为含氢氧化锂溶液。
(4)再生正极材料：将固体A和溶液B，混合蒸发除水，测定蒸发后固体中铁、锂、磷酸根摩尔比(mol)＝6.110：6.037：6.174，加0.064mol草酸亚铁、0.137mol碳酸锂(铁、锂、磷酸根摩尔比(mol)＝6.174：6.174：6.174)，再加85g葡萄糖混合，球磨，于氖气环境下，加热至570℃，烧结8h 35min，降温，得到再生的磷酸铁锂正极材料。
实施例3
一种从废旧磷酸铁锂电池中回收制备正极材料的方法，包括以下步骤：
(1)电池前处理：将回收的50.2kg废旧磷酸铁锂电池置于含1.7％氯化钠(质量浓度)的自来水中，放电4d，然后置于太阳辐射下干燥电池内部电解液。再将电池剪切3次得破碎 块，使破碎块的面积与电池的面积之比约为30％。将破碎块置于剥离液(丙三醇与磷酸三乙酯体积比为1：0.6)中，被剥离液覆没，加热设备升温至180℃，保温2h 20min，搅拌，过筛分离得到固体和分离液，固体为铝、铜箔，进行回收；将含片状活性物质的分离液继续加热，于238℃下保温4h 47min，并回收剥离液，分离出片状活性物质，片状活性物质经研磨、除磁得到11.8kg黑粉。
(2)脱碳、氟：向步骤(1)得到的黑粉中加入32.0g对甲苯磺酸钠，混合；开启流化床的加热器、泵机，加热，泵送空气，并将黑粉泵送至燃烧室进行反应，控制燃烧室加热温度约570℃，燃烧，降温，回收得到9.3kg脱碳、氟的黑粉。
(3)除杂：取1.0kg脱碳、氟的黑粉，用1mol/L磷酸酸洗，固液分离得固体A和溶液A，固体A加水洗涤，备用；向溶液A中加2.6g氢氧化钙，搅拌，调pH至沉淀不再增加，再固液分离得固体B和溶液B，溶液B为含氢氧化锂溶液。
(4)再生正极材料：将固体A和溶液B，混合蒸发除水，测定蒸发后固体中铁、锂、磷酸根摩尔比(mol)＝6.142：6.068：6.217，加0.067mol草酸亚铁、0.143mol碳酸锂(铁、锂、磷酸根摩尔比(mol)6.209：6.211：6.217)，再加90g葡萄糖混合，球磨，于氖气环境下，加热至570℃，烧结8h 35min，降温，得到再生的磷酸铁锂正极材料。
实施例4
一种从废旧磷酸铁锂电池中回收制备正极材料的方法，包括以下步骤：
(1)电池前处理：将回收的46.5kg废旧磷酸铁锂电池置于含1.7％氯化钠(质量浓度)的自来水中，放电4d，然后置于太阳辐射下干燥电池内部电解液。再将电池剪切3次得破碎块，使破碎块的面积与电池的面积之比约为20％。将破碎块置于剥离液(丙三醇与磷酸三乙酯体积比为1：0.6)中，被剥离液覆没，加热设备升温至180℃，保温2h 50min，搅拌，过筛分离得到固体和分离液，固体为铝、铜箔，进行回收；将含片状活性物质的分离液继续加热，于212℃下保温5h 26min，并回收剥离液，分离出片状活性物质，片状活性物质经研磨、除磁得到11.3kg黑粉。
(2)脱碳、氟：向步骤(1)得到的黑粉中加入32.0g对甲苯磺酸钠，混合；开启流化床的加热器、泵机，加热，泵送空气，并将黑粉泵送至燃烧室进行反应，控制燃烧室加热温度约560℃，燃烧，降温，回收得到8.9kg脱碳、氟的黑粉。
(3)除杂：取1.0kg脱碳、氟的黑粉，用1mol/L磷酸酸洗，固液分离得固体A和溶液A，固体A加水洗涤，备用；向溶液A中加2.7g氢氧化钙，搅拌，调pH至沉淀不再增加，再固液分离得固体B和溶液B，溶液B为含氢氧化锂溶液。
(4)再生正极材料：将固体A和溶液B，混合蒸发除水，测定蒸发后固体中铁、锂、磷酸根摩尔比(mol)＝6.131：6.063：6.196，加0.065mol草酸亚铁、0.134mol碳酸锂(铁、锂、磷酸根摩尔比(mol)＝6.196：6.197：6.196)，再加75g葡萄糖混合，球磨，于氖气环境下，加热至570℃，烧结8h 31min，降温，得到再生的磷酸铁锂正极材料。
实施例5
一种从废旧磷酸铁锂电池中回收制备正极材料的方法，包括以下步骤：
(1)电池前处理：将回收的42.7kg废旧磷酸铁锂电池置于含1.7％氯化钠(质量浓度)的自来水中，放电4d，然后置于太阳辐射下干燥电池内部电解液。再将电池剪切3次得破碎块，使破碎块的面积与电池的面积之比约为30％。将破碎块置于剥离液(丙三醇与磷酸三乙酯体积比为1：0.6)中，被剥离液覆没，加热设备升温至180℃，保温2h 40min，搅拌，过筛分离得到固体和分离液，固体为铝、铜箔，进行回收；将含片状活性物质的分离液继续加热244℃至不再变化，并回收剥离液，分离出片状活性物质，片状活性物质经研磨、除磁得到9.4kg黑粉。
(2)脱碳、氟：向步骤(1)得到的黑粉中加入35.0g对甲苯磺酸钠，混合；开启流化床的加热器、泵机，加热，泵送空气，并将黑粉泵送至燃烧室进行反应，控制燃烧室加热温度约570℃，燃烧，降温，回收得到7.4kg脱碳、氟的黑粉。
(3)除杂：取1.0kg脱碳、氟的黑粉，用1mol/L磷酸酸洗，固液分离得固体A和溶液A，固体A加水洗涤，备用；向溶液A中加2.7g氢氧化钙，搅拌，调pH至沉淀不再增加，再固液分离得固体B和溶液B，溶液B为含氢氧化锂溶液。
(4)再生正极材料：将固体A和溶液B，混合蒸发除水，测定蒸发后固体中铁、锂、磷酸根摩尔比(mol)＝6.158：6.104：6.214，加0.048mol草酸亚铁、0.060mol碳酸锂(铁、锂、磷酸根摩尔比(mol)＝6.163：6.161：6.214)，再加80g葡萄糖混合，球磨，于氖气环境下，加热至570℃，烧结8h 31min，降温，得到再生的磷酸铁锂正极材料。
对比例1
对比例1与实施例1的区别在于：步骤(2)脱碳、氟处理采用常规加热管进行脱碳、氟。黑粉送至管式炉中，510℃下加热8h，进行脱碳、氟。其余步骤同实施例1。
对比例2
对比例2与实施例1的区别在于：步骤(2)未加对甲苯磺酸钠，仅用流化床进行脱碳、氟。其余步骤同实施例1。
产品效果测试
(1)测试各实施例和对比例中黑粉脱碳、氟前后碳氟的含量。测试结果见表1。
表1实施例和对比例黑粉脱碳、氟前后碳氟的含量
Figure PCTCN2022111816-appb-000001
由表1可知，实施例中黑粉脱碳、氟后碳氟的含量明显低于对比例，采用流化床并配合加苯磺酸盐进行脱碳氟处理，能够有效去除碳氟。
(2)分别取实施例1-5和对比例1-2制备的磷酸铁锂正极材料，组装扣式电池。具体组装过程如下：
将磷酸铁锂正极材料、乙炔黑、聚偏氟乙烯(PVDF)按8：1：1的质量比进行称重，并混合、搅拌、研磨，加入一定量的N-甲基吡咯烷酮(NMP)溶液作为溶剂，搅拌后得到浆料。 将浆料均匀地涂覆在洁净的铝箔上，然后放置在70℃加热管中保温6h，将其冲压成直径约为15mm的电极片。锂离子扣式电池的组装在充满氖气的手套箱中进行，以制备的电极片为正极，1.0mol/LiPF 6(溶剂为碳酸乙烯酯)为电解液，按外壳、弹片、垫片、负极(金属锂片)、0.25mL电解液、隔膜(聚丙烯膜)、正极(电极片)、外壳顺序组装，封装扣式电池。
然后在恒流充放电测试设备上，测试组装的电池的充放电性能。测试条件：电压范围为2.0-3.5V，测试倍率为0.5C(152mAh·g -1)，0.5C倍率下循环30次的结果，见表2。
表2
组别 首次(mAh·g -1) 第30次(mAh·g -1)
实施例1 156.4 155.6
实施例2 156.8 155.6
实施例3 156.7 156.1
实施例4 156.9 155.7
实施例5 156.5 155.7
对比例1 156.2 154.3
对比例2 155.8 154.6
由表2可知，利用实施例提供的磷酸铁锂正极材料组装的扣式电池，循环30次的比容量均达到156mAh·g -1及以上，具有优异的电性能，明显优于对比例。图3为利用对比例1、实施例4提供的磷酸铁锂正极材料组装的扣式电池的放电循环性能图。在图3中，横坐标为循环次数，纵坐标为放电容量。对比例1的扣式电池30次放电容量在154.3-156.2mAh·g -1，实施例4的扣式电池30次放电容量在155.6-156.4mAh·g -1，实施例4提供的磷酸铁锂正极材料的循环稳定性更优。

Claims (10)

  1. 一种从废旧磷酸铁锂电池中回收制备正极材料的方法，其特征在于，包括以下步骤：
    (1)将废旧磷酸铁锂电池放电，干燥所述废旧磷酸铁锂电池内部的电解液，然后破碎得破碎块，再将所述破碎块剥离，得到黑粉；
    (2)将步骤(1)得到的黑粉与苯磺酸盐混合，然后于流化床中反应，得到脱去碳、氟的黑粉；
    (3)向步骤(2)中所述脱去碳、氟的黑粉中加入酸，固液分离得到溶液A和固体A；然后向所述溶液A中加入碱至沉淀不再生成为止，固液分离得到溶液B和固体B；
    (4)将步骤(3)得到的固体A和溶液B混合，加入补锂剂、补铁剂或磷酸盐中的至少一种，得到混合物，然后向所述混合物中加入还原剂，烧结，制得正极材料。
  2. 根据权利要求1所述的方法，其特征在于，在步骤(1)中，所述破碎块与所述废旧磷酸铁锂电池的面积比大于5％。
  3. 根据权利要求1所述的方法，其特征在于，在步骤(1)中，所述剥离的过程为将所述破碎块置于剥离液中，一次加热，分离得固体和分离液；然后将所述分离液进行二次加热，去除剥离液，得到黑粉。
  4. 根据权利要求3所述的方法，其特征在于，所述剥离液包括多元醇和磷酸酯。
  5. 根据权利要求4所述的方法，其特征在于，所述多元醇选自乙二醇、丙二醇、丙三醇、异丙醇、丁醇、1，2-丁二醇或1，3丁二醇中的至少一种；所述磷酸酯选自磷酸一酯、磷酸二酯、磷酸三酯、磷酸三乙酯或磷酸三甲酯中的至少一种。
  6. 根据权利要求4或5所述的方法，其特征在于，所述多元醇与所述磷酸酯的体积比为1：(0.1-1)。
  7. 根据权利要求3所述的方法，其特征在于，所述一次加热的温度为130-210℃，所述一次加热的时间为0.5-10h；所述二次加热的温度为210-300℃，所述二次加热的时间为2-12h。
  8. 根据权利要求1所述的方法，其特征在于，在步骤(2)中，所述苯磺酸盐加入量为黑粉0.1-5w％。
  9. 根据权利要求8所述的方法，其特征在于，在步骤(2)中，所述苯磺酸盐选自对甲 苯磺酸钠、甲苯磺酸钠、苯磺酸钠或苯磺酸锌中的至少一种。
  10. 根据权利要求1所述的方法，其特征在于，在步骤(2)中，所述反应的温度为300-850℃，反应的时间为1-360min。
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