WO2024066445A1 - 钠离子电池正极材料前驱体及其制备方法、钠离子电池正极材料、钠离子电池和涉电设备 - Google Patents

钠离子电池正极材料前驱体及其制备方法、钠离子电池正极材料、钠离子电池和涉电设备 Download PDF

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WO2024066445A1
WO2024066445A1 PCT/CN2023/098145 CN2023098145W WO2024066445A1 WO 2024066445 A1 WO2024066445 A1 WO 2024066445A1 CN 2023098145 W CN2023098145 W CN 2023098145W WO 2024066445 A1 WO2024066445 A1 WO 2024066445A1
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Prior art keywords
ion battery
positive electrode
electrode material
sodium ion
sodium
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PCT/CN2023/098145
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English (en)
French (fr)
Inventor
訚硕
李唯
张雨英
林艺佳
刘小虎
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CNGR Advanced Material Co Ltd
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CNGR Advanced Material Co Ltd
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Priority to US18/868,598 priority Critical patent/US20250340452A1/en
Priority to EP23869697.5A priority patent/EP4506309A4/en
Priority to MA71486A priority patent/MA71486A1/fr
Priority to KR1020247039214A priority patent/KR20250004864A/ko
Priority to JP2024566900A priority patent/JP7812466B2/ja
Publication of WO2024066445A1 publication Critical patent/WO2024066445A1/zh
Anticipated expiration legal-status Critical
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G53/00—Compounds of nickel
    • C01G53/05—Hydroxides; Oxyhydroxides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G53/00—Compounds of nickel
    • C01G53/40—Complex oxides containing nickel and at least one other metal element
    • C01G53/42—Complex oxides containing nickel and at least one other metal element containing alkali metals, e.g. LiNiO2
    • C01G53/44—Complex oxides containing nickel and at least one other metal element containing alkali metals, e.g. LiNiO2 containing manganese
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G53/00—Compounds of nickel
    • C01G53/40—Complex oxides containing nickel and at least one other metal element
    • C01G53/42—Complex oxides containing nickel and at least one other metal element containing alkali metals, e.g. LiNiO2
    • C01G53/44—Complex oxides containing nickel and at least one other metal element containing alkali metals, e.g. LiNiO2 containing manganese
    • C01G53/50—Complex oxides containing nickel and at least one other metal element containing alkali metals, e.g. LiNiO2 containing manganese of the type (MnO2)n-, e.g. Li(NixMn1-x)O2 or Li(MyNixMn1-x-y)O2
    • C01G53/51—Complex oxides containing nickel and at least one other metal element containing alkali metals, e.g. LiNiO2 containing manganese of the type (MnO2)n-, e.g. Li(NixMn1-x)O2 or Li(MyNixMn1-x-y)O2 containing sodium
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G53/00—Compounds of nickel
    • C01G53/80—Compounds containing nickel, with or without oxygen or hydrogen, and containing one or more other elements
    • C01G53/82—Compounds containing nickel, with or without oxygen or hydrogen, and containing two or more other elements
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G53/00—Compounds of nickel
    • C01G53/80—Compounds containing nickel, with or without oxygen or hydrogen, and containing one or more other elements
    • C01G53/84—Hydroxides
    • 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
    • H01M10/054—Accumulators with insertion or intercalation of metals other than lithium, e.g. with magnesium or aluminium
    • 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
    • H01M4/48—Selection of substances as active materials, active masses, active liquids of inorganic oxides or hydroxides
    • H01M4/50—Selection of substances as active materials, active masses, active liquids of inorganic oxides or hydroxides of manganese
    • H01M4/505—Selection of substances as active materials, active masses, active liquids of inorganic oxides or hydroxides of manganese of mixed oxides or hydroxides containing manganese for inserting or intercalating light metals, e.g. LiMn2O4 or LiMn2OxFy
    • 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
    • H01M4/48—Selection of substances as active materials, active masses, active liquids of inorganic oxides or hydroxides
    • H01M4/52—Selection of substances as active materials, active masses, active liquids of inorganic oxides or hydroxides of nickel, cobalt or iron
    • H01M4/525—Selection of substances as active materials, active masses, active liquids of inorganic oxides or hydroxides of nickel, cobalt or iron of mixed oxides or hydroxides containing iron, cobalt or nickel for inserting or intercalating light metals, e.g. LiNiO2, LiCoO2 or LiCoOxFy
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2002/00—Crystal-structural characteristics
    • C01P2002/70—Crystal-structural characteristics defined by measured X-ray, neutron or electron diffraction data
    • C01P2002/72—Crystal-structural characteristics defined by measured X-ray, neutron or electron diffraction data by d-values or two theta-values, e.g. as X-ray diagram
    • 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
    • C01P2004/30—Particle morphology extending in three dimensions
    • C01P2004/32—Spheres
    • 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
    • C01P2004/61—Micrometer sized, i.e. from 1-100 micrometer
    • 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
    • C01P2006/11—Powder tap density
    • 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
    • C01P2006/12—Surface area
    • 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
    • C—CHEMISTRY; METALLURGY
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    • C01P2006/00—Physical properties of inorganic compounds
    • C01P2006/80—Compositional purity
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/10—Energy storage using batteries

Definitions

  • the present application relates to the field of batteries, and in particular to a sodium ion battery positive electrode material precursor and a preparation method thereof, a sodium ion battery positive electrode material, a sodium ion battery and electrical equipment.
  • the purpose of the present application is to provide a sodium ion battery positive electrode material precursor and a preparation method thereof, a sodium ion battery positive electrode material, a sodium ion battery and electrical-related equipment to solve the above-mentioned problems.
  • a sodium ion battery cathode material precursor the general chemical formula of which is Ni x Mn y Fe 1-xy (OH) 2 , wherein 0.15 ⁇ x ⁇ 0.35, 0.2 ⁇ y ⁇ 0.5;
  • the S element content in the precursor of the sodium ion battery positive electrode material is ⁇ 4000ppm.
  • the precursor further contains Na, and the Na/S mass ratio is ⁇ 1.5.
  • the sodium ion battery cathode material precursor satisfies at least one of the following conditions:
  • the S element content in the precursor of the positive electrode material for a sodium ion battery is 800-3700 ppm, and the Na/S mass ratio is ⁇ 1.18; optionally, the S element content in the precursor of the positive electrode material for a sodium ion battery is 1700-2800 ppm, and the Na/S mass ratio is ⁇ 0.45;
  • the D50 of the sodium ion battery cathode material precursor is 3-14 ⁇ m, preferably 5-10 ⁇ m;
  • the specific surface area of the precursor of the positive electrode material for sodium ion battery is 6-11 m 2 /g, preferably 6-8 m 2 /g;
  • the tap density of the sodium ion battery cathode material precursor is ⁇ 1.7 g/cm 3 , preferably 1.9-2.3 g/cm 3 ;
  • the precursor of the positive electrode material of the sodium ion battery is spherical or quasi-spherical.
  • the present application also provides a method for preparing a precursor of a positive electrode material for a sodium ion battery, comprising:
  • the remaining complexing agent, the remaining precipitant and the mixed salt solution are added to the bottom liquid for co-precipitation reaction, and the solid-liquid separation is performed to obtain a solid, which is then washed with alkali, washed with water and dried to obtain a precursor of the positive electrode material for a sodium ion battery;
  • At least one of the nickel source, the manganese source and the ferrous source comprises sulfate.
  • the method for preparing a precursor of a positive electrode material for a sodium ion battery satisfies at least one of the following conditions:
  • the nickel source includes one or more of nickel sulfate, nickel nitrate, and nickel acetate
  • the manganese source includes one or more of manganese sulfate, manganese nitrate, and manganese acetate
  • the ferrous source includes one or more of ferrous sulfate, ferrous nitrate, and ferrous chloride
  • the concentration of the mixed salt solution is 1.0-2.2 mol/L
  • the precipitating agent includes sodium hydroxide and/or potassium hydroxide, and the complexing agent includes one or more of ammonium bicarbonate, ammonium carbonate, and ammonia water;
  • the complexing agent is used in the form of an aqueous solution with a concentration of 0.3 to 8 mol/L, optionally, a concentration of 0.3 to 2.0 mol/L;
  • the temperature of the water used in preparing the base liquid is 40-60°C, and the temperature is raised so that the temperature of the prepared base liquid is 40-60°C; the pH of the base liquid is 10-12;
  • the flow rate of the mixed salt solution added to the bottom liquid is 2%/h-8%/h of the available volume of the reactor, the flow rate of the precipitant added to the bottom liquid is 0.08%/h-0.32%/h of the available volume of the reactor, and the flow rate of the complexing agent added to the bottom liquid is 0.04%/h-0.16%/h of the available volume of the reactor;
  • the coprecipitation reaction is carried out under stirring conditions at a stirring rate of 300-1000r/min;
  • the end point of the coprecipitation reaction is that the D50 of the sodium ion battery cathode material precursor reaches 3-14 ⁇ m;
  • the end point of water washing i.e. the standard for completion of water washing
  • the conductivity of the washing liquid i.e. the mother liquor obtained by filtration after washing
  • the drying temperature is 120-180°C
  • the time is 10-16h
  • the end point of drying is that the moisture content of the material is less than or equal to 0.6wt%.
  • the flow rates of the remaining complexing agent, the remaining precipitant and the mixed salt solution added to the base solution are controlled in stages.
  • staged control may include:
  • the first flow rate of the mixed salt solution added to the bottom liquid is controlled to be 2%/h-4%/h of the available volume of the reactor, the first flow rate of the precipitant added to the bottom liquid is controlled to be 0.08%/h-0.16%/h of the available volume of the reactor, and the first flow rate of the complexing agent added to the bottom liquid is controlled to be 0.04%/h-0.08%/h of the available volume of the reactor, until the first precipitate D50 is 3-5 ⁇ m;
  • the second flow rate of the mixed salt solution added to the bottom liquid is controlled to be 4%/h-8%/h of the available volume of the reactor.
  • the second flow rate of the precipitant added to the bottom liquid is controlled to be 0.16-0.32%/h of the available volume of the reactor, and the second flow rate of the complexing agent added to the bottom liquid is controlled to be 0.08-0.16%/h of the available volume of the reactor, until the D50 of the sodium ion battery positive electrode material precursor is 6-14 ⁇ m.
  • the available volume of the reactor is the remaining volume of the reactor after the base liquid is added when stirring without splashing liquid.
  • the first flow rate and the second flow rate of each of the above solutions are adjusted according to the D50 size of the target material.
  • the present application also provides a sodium ion battery positive electrode material, which is prepared by reacting a sodium ion battery positive electrode material precursor with a sodium source.
  • the molar ratio of the sum of nickel, manganese and iron in the precursor of the positive electrode material of the sodium ion battery to the sodium in the sodium source is 1:(1.02-1.07);
  • reaction is calcined using programmed temperature:
  • the temperature is raised to 780-880°C at a heating rate of 2-4°C/min and calcined for 10-20 hours.
  • the present application also provides a sodium ion battery, the raw materials of which include a sodium ion battery positive electrode material.
  • the present application also provides an electrical device, including a sodium ion battery.
  • the sodium ion battery positive electrode material precursor provided in the present application is based on nickel manganese iron hydroxide, and the material performance is improved by optimizing the sulfur content and the sodium-sulfur mass ratio; when retaining the trace sulfur impurity content, at the same sulfur content level, the lower the sodium-sulfur ratio, the better the battery capacity, first efficiency and cycle performance; in the range of 2-4.2V, the 0.1C first discharge capacity is >165mAh/g, the 1C discharge capacity is >154mAh/g, and the 50-week cycle capacity retention rate under 1C conditions is >78%, and the charge and discharge rate is fast under high cycle efficiency conditions.
  • the present application provides a method for preparing a positive electrode material precursor for a sodium ion battery.
  • the prepared positive electrode material precursor has good element uniformity, few structural defects, controllable particle size, good sphericity, low sodium content, and moderate sulfur content.
  • the sodium ion battery positive electrode material, sodium ion battery and electrical equipment provided in this application have excellent electrical properties.
  • FIG1 is a scanning electron microscope image of the precursor obtained in Example 1;
  • FIG2 is an XRD diagram of the precursor obtained in Example 1;
  • FIG3 is a graph showing the discharge capacity of some embodiments as a function of sulfur content.
  • Ni x Mn y Fe 1-xy (OH) 2 It is a sodium ion battery cathode material precursor, and its general chemical formula is Ni x Mn y Fe 1-xy (OH) 2 , wherein 0.15 ⁇ x ⁇ 0.35, 0.2 ⁇ y ⁇ 0.5;
  • the S element content in the precursor of the sodium ion battery positive electrode material is ⁇ 4000ppm.
  • the precursor further contains Na, and the Na/S mass ratio is ⁇ 1.5.
  • x may be 0.15, 0.20, 0.25, 0.30, 0.35 or any value between 0.15 and 0.35
  • y may be 0.2, 0.3, 0.4, 0.5 or any value between 0.2 and 0.5.
  • the sodium ion battery cathode material precursor satisfies at least one of the following conditions:
  • the S element content in the precursor of the positive electrode material for a sodium ion battery is 800-3700 ppm, and the Na/S mass ratio is ⁇ 1.18; optionally, the S element content in the precursor of the positive electrode material for a sodium ion battery is 1700-2800 ppm, and the Na/S mass ratio is ⁇ 0.45;
  • the S element content in the sodium ion battery positive electrode material precursor can be 800ppm, 900ppm, 1000ppm, 1100ppm, 1200ppm, 1300ppm, 1400ppm, 1500ppm, 1600ppm, 1700ppm, 1800ppm, 1900ppm, 2000ppm, 2100ppm, 2200ppm, 2300ppm, 2400ppm, 2500ppm, 2600ppm, 2700ppm, 2800ppm, 2900ppm, 3000ppm, 31 00ppm, 3200ppm, 3300ppm, 3400ppm, 3500ppm, 3600ppm, 3700ppm or any value between 800-3700ppm, and the Na/S mass ratio can be 0.10, 0.15, 0.20, 0.25, 0.30, 0.35, 0.40, 0.45, 0.50, 0.55, 0.60, 0.65, 0.70, 0.75, 0.80, 0.85, 0.90, 0.95, 1.00, 1.05, 1.10, 1.15, 1.18 or any value ⁇
  • the D50 of the sodium ion battery cathode material precursor is 3-14 ⁇ m, preferably 5-10 ⁇ m;
  • the D50 of the sodium ion battery cathode material precursor may be 3 ⁇ m, 4 ⁇ m, 5 ⁇ m, 6 ⁇ m, 7 ⁇ m, 8 ⁇ m, 9 ⁇ m, 10 ⁇ m, 11 ⁇ m, 12 ⁇ m, 13 ⁇ m, 14 ⁇ m or any value between 3 and 14 ⁇ m;
  • the specific surface area of the precursor of the positive electrode material for sodium ion battery is 6-11 m 2 /g, preferably 6-8 m 2 /g;
  • the specific surface area of the sodium ion battery cathode material precursor may be 6 m 2 /g, 7 m 2 /g, 8 m 2 /g, 9 m 2 /g, 10 m 2 /g, 11 m 2 /g or any value between 6-11 m 2 /g;
  • the tap density of the sodium ion battery cathode material precursor is ⁇ 1.7 g/cm 3 , preferably 1.9-2.3 g/cm 3 ;
  • the tap density of the sodium ion battery cathode material precursor may be 1.7 g/cm 3 , 1.8 g/cm 3 , 1.9 g/cm 3 , 2.0 g/cm 3 , 2.1 g/cm 3 , 2.2 g/cm 3 , 2.3 g/cm 3 or any value greater than 1.9-2.3 g/cm 3 ;
  • the precursor of the positive electrode material of the sodium ion battery is spherical or quasi-spherical.
  • the present application also provides a method for preparing a precursor of a positive electrode material for a sodium ion battery, comprising:
  • the remaining complexing agent, the remaining precipitant and the mixed salt solution are added to the bottom liquid for co-precipitation reaction, and the solid-liquid separation is performed to obtain a solid, which is then washed with alkali, washed with water and dried to obtain a precursor of the positive electrode material for a sodium ion battery;
  • At least one of the nickel source, the manganese source, and the ferrous source includes a sulfate.
  • the method for preparing a sodium ion battery positive electrode material precursor satisfies at least one of the following conditions:
  • the nickel source includes one or more of nickel sulfate, nickel nitrate, and nickel acetate
  • the manganese source includes one or more of manganese sulfate, manganese nitrate, and manganese acetate
  • the ferrous source includes one or more of ferrous sulfate, ferrous nitrate, and ferrous chloride
  • the concentration of the mixed salt solution is 1.0-2.2 mol/L
  • the concentration of the mixed salt solution may be 1.0 mol/L, 1.1 mol/L, 1.2 mol/L, 1.3 mol/L, 1.4 mol/L, 1.5 mol/L, 1.6 mol/L, 1.7 mol/L, 1.8 mol/L, 1.9 mol/L, 2.0 mol/L, 2.1 mol/L, 2.2 mol/L or any value between 1.0 and 2.2 mol/L;
  • the precipitating agent includes sodium hydroxide and/or potassium hydroxide, and the complexing agent includes one or more of ammonium bicarbonate, ammonium carbonate, and ammonia water;
  • the complexing agent is used in the form of an aqueous solution with a concentration of 0.3 to 8 mol/L, optionally, a concentration of 0.3 to 2.0 mol/L;
  • the concentration of the complexing agent aqueous solution can be 0.3mol/L, 0.4mol/L, 0.5mol/L, 0.6mol/L, 0.7mol/L, 0.8mol/L, 0.9mol/L, 1.0mol/L, 1.1mol/L, 1.2mol/L, 1.3mol/L, 1.4mol/L, 1.5mol/L, 1.6mol/L, 1.7mol/L, 1.8mol/L, 1.9mol/L, 2.0mol/L, 3.0mol/L, 4.0mol/L, 5.0mol/L, 6.0mol/L, 7.0mol/L, 8.0mol/L or any value between 0.3-8.0mol/L;
  • the temperature of the water used in preparing the base liquid is 40-60°C, and the temperature is raised so that the temperature of the prepared base liquid is 40-60°C; the pH of the base liquid is 10-12;
  • the temperature of the water may be 40°C, 50°C, 60°C or any value between 40-60°C
  • the pH of the base solution may be 10.0, 10.5, 11.0, 11.5, 12.0 or any value between 10-12;
  • the flow rate of the mixed salt solution added to the bottom liquid is 2%/h-8%/h of the available volume of the reactor, the flow rate of the precipitant added to the bottom liquid is 0.08%/h-0.32%/h, and the flow rate of the complexing agent added to the bottom liquid is 0.04%/h-0.16%/h;
  • the flow rate of the mixed salt solution added to the bottom liquid can be 2%/h, 3%/h, 4%/h, 5%/h, 6%/h, 7%/h, 8%/h or any value between 2-8%/h of the available volume of the reactor, and the flow rate of the precipitant added to the bottom liquid can be 0.08%/h, 0.10%/h, 0.15%/h, 0.20%/h, 0.25%/h, 0.30%/h, 0.32%/h or any value between 0.08%/h and 0.32%/h.
  • the flow rate of the complexing agent added to the bottom liquid is 0.04%/h, 0.05%/h, 0.06%/h, 0.07%/h, 0.08%/h, 0.09%/h, 0.10%/h, 0.11%/h, 0.12%/h, 0.13%/h, 0.14%/h, 0.15%/h, 0.16%/h or any value in between;
  • the coprecipitation reaction is carried out under stirring conditions at a stirring rate of 300-1000r/min;
  • the stirring rate may be 300 r/min, 400 r/min, 500 r/min, 600 r/min, 700 r/min, 800 r/min, 900 r/min, 1000 r/min or any value between 300-1000 r/min;
  • the end point of the coprecipitation reaction is that the D50 of the sodium ion battery cathode material precursor reaches 3-14 ⁇ m;
  • the end product D50 of the coprecipitation reaction may be 3 ⁇ m, 4 ⁇ m, 5 ⁇ m, 6 ⁇ m, 7 ⁇ m, 8 ⁇ m, 9 ⁇ m, 10 ⁇ m, 11 ⁇ m, 12 ⁇ m, 13 ⁇ m, 14 ⁇ m or any value between 3 and 14 ⁇ m;
  • the end point of water washing i.e. the standard for completion of water washing
  • the conductivity of the washing liquid i.e. the mother liquor obtained by filtration after washing
  • the drying temperature is 120-180°C
  • the time is 10-16h
  • the end point of drying is that the moisture content of the material is less than or equal to 0.6wt%.
  • the conductivity of the washing liquid at the end point of water washing can be 10 ⁇ S/cm, 20 ⁇ S/cm, 30 ⁇ S/cm, 40 ⁇ S/cm, 49 ⁇ S/cm or any value less than 50 ⁇ S/cm
  • the drying temperature can be 120°C, 130°C, 140°C, 150°C, 160°C, 170°C, 180°C or any value between 120-180°C
  • the time can be 10h, 11h, 12h, 13h, 14h, 15h, 16h or any value between 10-16h
  • the moisture content of the material at the end point of drying can be 0.1wt%, 0.2wt%, 0.3wt%, 0.4wt%, 0.5wt%, 0.6wt% or less than or equal to 0.6wt%.
  • the flow rates of adding the remaining complexing agent, the remaining precipitating agent and the mixed salt solution to the base solution are controlled in stages.
  • the staged control includes:
  • the first flow rate of the mixed salt solution added to the bottom liquid is controlled to be 2%/h-4%/h of the available volume of the reactor, the first flow rate of the precipitant added to the bottom liquid is controlled to be 0.08%/h-0.16%/h of the available volume of the reactor, and the first flow rate of the complexing agent added to the bottom liquid is controlled to be 0.04%/h-0.08%/h of the available volume of the reactor, until the first precipitate D50 is 3-5 ⁇ m;
  • the first flow rate at which the mixed salt solution is added to the bottom liquid can be 2%/h, 3%/h, 4%/h, or any value between 2%/h and 4%/h of the available volume of the reactor;
  • the first flow rate at which the precipitant is added to the bottom liquid can be 0.08%/h, 0.09%/h, 0.10%/h, 0.11%/h, 0.12%/h, 0.13%/h, 0.14%/h, 0.15%/h, 0.16%/h, or any value between 0.08%/h and 0.16%/h of the available volume of the complexing agent reactor;
  • the first flow rate at which the complexing agent is added to the bottom liquid can be 0.04%/h, 0.05%/h, 0.06%/h, 0.07%/h, 0.08%/h, or any value between 0.04%/h and 0.08%/h of the available volume of the precipitant reactor;
  • the second flow rate of the mixed salt solution added to the bottom liquid is controlled to be 4%/h-8%/h of the available volume of the reactor, the second flow rate of the precipitant added to the bottom liquid is controlled to be 0.16%/h-0.32%/h of the available volume of the reactor, and the second flow rate of the complexing agent added to the bottom liquid is controlled to be 0.08%/h-0.16%/h of the available volume of the reactor, until the D50 of the sodium ion battery positive electrode material precursor is 6-14 ⁇ m.
  • the second flow rate at which the mixed salt solution is added to the bottom liquid can be 4%/h, 5%/h, 6%/h, 7%/h, 8%/h or any value between 4%/h and 8%/h of the available volume of the reactor, and the second flow rate at which the precipitant is added to the bottom liquid can be 0.16%/h, 0.18%/h, 0.20%/h, 0.22%/h, 0.24%/h, 0.26%/h, 0.28%/h, 0.30%/h, 0.
  • the second flow rate for controlling the complexing agent to be added to the bottom liquid can be 0.08%/h, 0.09%/h, 0.10%/h, 0.11%/h, 0.12%/h, 0.13%/h, 0.14%/h, 0.15%/h, 0.16%/h or any value between 0.08%/h and 0.16%/h of the available volume of the reactor.
  • the mixed salt flow rate is controlled in stages, which is beneficial to retaining a certain sulfur content in the precursor structure and facilitating obtaining the required sulfur content in the washing stage.
  • the present application also provides a sodium ion battery positive electrode material, which is prepared by reacting a sodium ion battery positive electrode material precursor with a sodium source.
  • the molar ratio of the sum of nickel, manganese and iron in the precursor of the positive electrode material of the sodium ion battery to the sodium in the sodium source is 1: (1.02-1.07);
  • reaction is calcined using programmed temperature:
  • the temperature is raised to 780-880°C at a heating rate of 2-4°C/min and calcined for 10-20 hours.
  • the molar ratio of the sum of nickel, manganese and iron in the precursor of the positive electrode material of the sodium ion battery to the sodium in the sodium source can be 1:1.02, 1:1.03, 1:1.04, 1:1.05, 1:1.06, 1:1.07 or any value between 1:(1.02-1.07);
  • the heating rate can be 2°C/min, 3°C/min, 4°C/min or any value between 2-4°C/min
  • the heating end point can be 780°C, 800°C, 820°C, 840°C, 860°C, 880°C or any value between 780-880°C
  • the calcination time can be 10 hours, 12 hours, 14 hours, 16 hours, 18 hours, 20 hours or any value between 10-20 hours.
  • the present application also provides a sodium ion battery, the raw materials of which include a positive electrode material for a sodium ion battery.
  • the present application also provides an electrical device, including a sodium ion battery.
  • the electrical equipment referred to here may be electric vehicles, power banks, mobile phones and other equipment.
  • This embodiment provides a sodium ion battery positive electrode material precursor, and the preparation method thereof is as follows:
  • Nickel sulfate, manganese sulfate, and ferrous sulfate (molar ratio 1:1:1) were prepared into a 2 mol/L mixed salt solution; 50°C deionized water, 10 mol/L sodium hydroxide solution, and 8 mol/L ammonia water were added to a reactor with a stirring device to prepare a base solution with a pH of 11.5. The temperature of the reactor was raised to 50°C, and ammonia water, sodium hydroxide solution, and mixed salt solution were slowly added at a stirring rate of 600 r/min. The first flow rate of the mixed salt solution added to the base solution was 100% of the available volume of the reactor.
  • the first flow rate of sodium hydroxide solution added to the bottom liquid is 2%/h of the available volume of the reactor, the first flow rate of ammonia water added to the bottom liquid is 0.08%/h of the available volume of the reactor, and the first flow rate of ammonia water added to the bottom liquid is 0.04%/h of the available volume of the reactor, until the first precipitate D50 is 3.0 ⁇ m, and then the second flow rate of the mixed salt solution is increased to 4%/h of the available volume of the reactor, and the second flow rates of the ammonia solution and the sodium hydroxide solution are synchronously adjusted to 0.12%/h and 0.20%/h of the available volume of the reactor, respectively, until the D50 of the sodium ion battery positive electrode material precursor is 10.0 ⁇ m.
  • the above-mentioned sodium ion battery positive electrode material precursor precipitate is centrifuged and washed, and alkaline washed multiple times with 0.5 mol/L sodium hydroxide solution, and then washed multiple times with 70°C deionized water.
  • the conductivity of the mother liquor obtained by filtration after washing is less than 50 ⁇ S/cm, the washing is considered to be completed, the same below.
  • the solid matter after centrifugal washing was dispersed, placed in a forced air oven, and dried and dehydrated at 120° C. for 12 h. The end point of drying was when the moisture content of the material was 0.4 wt %. The solid matter was taken out and sealed for storage.
  • the obtained dried material is subjected to sieving, demagnetization and other treatments to obtain a precursor of a positive electrode material for a sodium ion battery, the molecular formula of which is Ni 0.33 Mn 0.33 Fe 0.34 (OH) 2 .
  • Figure 1 is a scanning electron microscope image of the obtained sodium ion battery positive electrode material precursor.
  • Figure 1 shows that the prepared sodium ion battery positive electrode material precursor is a spherical structure with good sphericity and a narrow particle size distribution.
  • Figure 2 is an XRD graph of the obtained sodium ion battery positive electrode material precursor. The XRD in Figure 2 shows that the sodium ion battery positive electrode material precursor corresponds to ⁇ -type hydroxide.
  • This embodiment 1 also provides a sodium ion battery positive electrode material, and the preparation method thereof is as follows:
  • the reaction stages are the same as in Example 1, and a nickel-iron-manganese ternary precipitate is obtained.
  • the above-mentioned sodium ion battery positive electrode material precursor precipitate was centrifuged and washed, and was alkaline washed multiple times with 0.5 mol/L sodium hydroxide solution, and then washed multiple times with 70°C deionized water.
  • the number of alkaline washing and water washing, washing time, amount of alkali solution and water used for washing were adjusted so that the contents of Na impurities and S impurities were at different levels. The specific values are shown in Table 1.
  • Nickel sulfate, manganese sulfate, and ferrous sulfate (molar ratio 2:4:4) were prepared into a 2 mol/L mixed salt solution; deionized water at 40°C, 10 mol/L sodium hydroxide solution, and 8 mol/L ammonia water were added to a reactor with a stirring device to prepare a base solution with a pH of 11.5. The temperature in the reactor was raised to 40°C, and ammonia water, sodium hydroxide solution, and mixed salt solution were slowly added at a stirring rate of 1000 r/min.
  • the first flow rate of the mixed solution salt added to the base solution was 4%/h of the available volume of the reactor, and the first flow rate of the sodium hydroxide solution added to the base solution was 0.16%/h of the available volume of the reactor.
  • the first flow rate of adding ammonia water into the bottom liquid is 0.08%/h of the available volume of the reactor, until the first precipitate D50 grows to 5.0 ⁇ m, and then the second flow rate of the mixed salt solution is increased to 8%/h of the available volume of the reactor, and the second flow rates of the ammonia solution and the sodium hydroxide solution are synchronously adjusted to 0.12%/h and 0.20%/h of the available volume of the reactor, respectively, until the sodium ion battery positive electrode material precursor D50 grows to 8.0 ⁇ m. When the precursor D50 reaches 8.0 ⁇ m, the feeding is stopped.
  • the above-mentioned sodium ion battery positive electrode material precursor precipitate was centrifugally washed, alkaline washed multiple times with 0.5 mol/L sodium hydroxide solution, and then washed multiple times with 70°C deionized water.
  • the number of alkaline washing and water washing, washing time, amount of alkali solution and water used for washing were adjusted so that the contents of Na impurities and S impurities were at different levels. The specific values are shown in Table 1.
  • the subsequent drying treatment, sintering into positive electrode material and battery manufacturing steps are the same as those in Example 1.
  • the molecular formula of the obtained sodium ion battery positive electrode material precursor is Ni 0.2 Mn 0.4 Fe 0.4 (OH) 2 .
  • Nickel sulfate, manganese sulfate, and ferrous sulfate (molar ratio 2:4:4) are prepared into a 2 mol/L mixed salt solution; deionized water at 40°C, 10 mol/L sodium hydroxide solution, and 8 mol/L ammonia water are added to a reactor with a stirring device to prepare a base solution with a pH of 11.5. The temperature in the reactor is raised to 40°C, and ammonia water, sodium hydroxide solution, and mixed salt solution are slowly added at a stirring rate of 1000 r/min.
  • the first flow rate of the mixed salt solution added to the base solution is 8%/h of the available volume of the reactor, the first flow rate of the sodium hydroxide solution added to the base solution is 0.32%/h of the available volume of the reactor, and the first flow rate of the ammonia water added to the base solution is 0.16%/h of the available volume of the reactor, until the sodium ion battery positive electrode material precursor D50 grows to 8.0 ⁇ m, and the feeding is stopped.
  • the subsequent drying treatment, sintering into positive electrode material and battery manufacturing steps are the same as those in Example 16.
  • the molecular formula of the obtained sodium ion battery positive electrode material precursor is Ni 0.2 Mn 0.4 Fe 0.4 (OH) 2 .
  • FIG3 is a graph showing the discharge capacity of some embodiments as a function of sulfur content.
  • the increase in S content can improve the battery capacity and rate performance, but after the S content increases to a certain value, the battery capacity and rate performance decrease again.
  • the preferred S: 800-3700ppm, Na/S ⁇ 1.18, 0.1C first discharge capacity can be ⁇ 163mAh/g, 50-week cycle capacity retention rate ⁇ 77.83%; the most preferred S: 1700-2800ppm, Na/S ⁇ 0.45, 0.1C first discharge capacity can be ⁇ 166mAh/g, 50-week cycle retention rate ⁇ 78.2%; from Comparative Example 1, it can be seen that when S>4000ppm, all performances are significantly reduced; from Comparative Examples 2-3, it can be seen that when Na/S>1.5, all performances are also significantly reduced.
  • the same characteristics are also found in Examples 16-17 and Comparative Example 4 of Ni 0.2 Mn 0.4 Fe 0.4 (OH) 2. Therefore, the presence of trace amounts of non-sodium sulfate within a specific range plays a key role in improving the performance of the material, and the lower the sodium-sulfur ratio, the better the performance of the material.
  • Comparing Example 16 with Comparative Example 5 when only the feed flow rate is changed to a large flow rate throughout the process, while the washing method and other methods remain unchanged, the sulfur content of the precursor decreases, and the sodium-sulfur ratio is higher, resulting in a decrease in performance. Therefore, the mixed salt flow rate is controlled in stages, which is conducive to retaining a certain sulfur content in the precursor structure, and it is easier to obtain a precursor material with a sulfur content and a sodium-sulfur ratio within the above-mentioned specific range.
  • the present application provides a sodium ion battery positive electrode material precursor and a preparation method thereof, a sodium ion battery positive electrode material, a sodium ion battery and electrical equipment, and relates to the field of batteries.
  • the sodium ion battery positive electrode material precursor has a general chemical formula of Ni x Mn y Fe 1-xy (OH) 2 , wherein 0.15 ⁇ x ⁇ 0.35, 0.2 ⁇ y ⁇ 0.5; the S element content in the sodium ion battery positive electrode material precursor is ⁇ 4000ppm, and the Na/S mass ratio is ⁇ 1.5.
  • the sodium ion battery positive electrode material precursor provided in the present application has good element uniformity of the prepared positive electrode material, few structural defects, controllable particle size, good sphericity, high energy density, and while retaining a trace amount of sulfur impurities, at the same level of sulfur content, the lower the sodium-sulfur ratio, the better the battery capacity, first efficiency and cycle performance.
  • the sodium ion battery cathode material precursor and preparation method thereof, sodium ion battery cathode material, sodium ion battery and electrical equipment of the present application are reproducible and can be used in a variety of industrial applications.
  • the sodium ion battery cathode material precursor and preparation method thereof, sodium ion battery cathode material, sodium ion battery and electrical equipment of the present application can be used in the battery field.

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Abstract

本申请提供一种钠离子电池正极材料前驱体及其制备方法、钠离子电池正极材料、钠离子电池和涉电设备，涉及电池领域。钠离子电池正极材料前驱体，其化学通式为NixMnyFe1-x-y(OH)2，其中，0.15≤x≤0.35，0.2≤y≤0.5；所述钠离子电池正极材料前驱体中S元素含量≤4000ppm，且Na/S质量比≤1.5。本申请提供的钠离子电池正极材料前驱体，制备所得正极材料元素均匀性很好，结构缺陷少，粒度可控，球形度好，能量密度高，在保留微量硫杂质含量下，在同水平硫含量下，钠硫比越低，电池容量、首效和循环性能越好。

Description

钠离子电池正极材料前驱体及其制备方法、钠离子电池正极材料、钠离子电池和涉电设备
相关申请的交叉引用
本申请要求于2022年09月28日提交中国国家知识产权局的申请号为202211188250.3、名称为“钠离子电池正极材料前驱体及其制备方法、钠离子电池正极材料、钠离子电池和涉电设备”的中国专利申请的优先权，其全部内容通过引用结合在本申请中。
技术领域
本申请涉及电池领域，尤其涉及一种钠离子电池正极材料前驱体及其制备方法、钠离子电池正极材料、钠离子电池和涉电设备。
背景技术
锂资源缺乏和高成本的问题使得锂离子电池在大规模储能领域的应用受到制约。资源丰富、成本较低的钠离子电池有望在此领域替代锂离子电池，而正极材料是制约钠离子电池发展的决定性因素。层状过渡金属氧化物是一类容量较高，稳定性较好的钠离子电池正极材料，且拥有与锂离子电池类似的体系和工作原理，因此受到研究者广泛关注。但该类材料的商业化仍然受到低能量密度和相对较差的循环寿命等问题的阻碍。
如何解决上述钠离子电池相关的问题，合成一种高能量密度、容量高、循环寿命长的正极材料，便成为本领域所要研究解决的问题。
发明内容
本申请的目的在于提供一种钠离子电池正极材料前驱体及其制备方法、钠离子电池正极材料、钠离子电池和涉电设备，以解决上述问题。
为实现以上目的，本申请采用以下技术方案：
一种钠离子电池正极材料前驱体，其化学通式为NixMnyFe1-x-y(OH)2，其中，0.15≤x≤0.35，0.2≤y≤0.5；
钠离子电池正极材料前驱体中S元素含量≤4000ppm。
可选地，前驱体中还含有Na，且Na/S质量比≤1.5。
可选地，钠离子电池正极材料前驱体满足以下条件中的至少一个：
A.钠离子电池正极材料前驱体中S元素含量为800-3700ppm，且Na/S质量比≤1.18；可选地，钠离子电池正极材料前驱体中S元素含量为1700-2800ppm，且Na/S质量比≤0.45；
B.钠离子电池正极材料前驱体的D50为3-14μm，优选为5-10μm；
C.钠离子电池正极材料前驱体的比表面积为6-11m2/g，优选为6-8m2/g；
D.钠离子电池正极材料前驱体的振实密度为≥1.7g/cm3，优选为1.9-2.3g/cm3；
E.钠离子电池正极材料前驱体呈球形，或类球形。
本申请还提供一种的钠离子电池正极材料前驱体的制备方法，包括：
将包括镍源、锰源、亚铁源、水在内的原料混合得到混合盐溶液，将包括水、部分络合剂和部分沉淀剂在内的物料混合得到底液；
将剩余的络合剂、剩余的沉淀剂和混合盐溶液加入到底液中进行共沉淀反应，固液分离得到固体物，然后进行碱洗、水洗、干燥，得到钠离子电池正极材料前驱体；
其中，镍源、锰源和亚铁源中的至少一者包括硫酸盐。
可选地，钠离子电池正极材料前驱体的制备方法，满足以下条件中的至少一个：
a.镍源包括硫酸镍、硝酸镍、乙酸镍中的一种或多种，锰源包括硫酸锰、硝酸锰、乙酸锰中的一种或多种，亚铁源包括硫酸亚铁、硝酸亚铁、氯化亚铁中的一种或多种；
b.混合盐溶液的浓度为1.0-2.2mol/L；
c.沉淀剂包括氢氧化钠和/或氢氧化钾，络合剂包括碳酸氢铵、碳酸铵、氨水中的一种或多种；
d.络合剂以水溶液形式使用，浓度为0.3～8mol/L，可选地，浓度为0.3-2.0mol/L；
e.制备底液时使用的水的温度为40-60℃，并且升温使得制备得到的底液的温度为40-60℃；底液的pH为10-12；
f.混合盐溶液加入到底液中的流速为反应釜可用容积的2％/h-8％/h，沉淀剂加入到底液中的流速为反应釜可用容积的0.08％/h-0.32％/h，络合剂加入到底液中的流速为反应釜可用容积的0.04％/h-0.16％/h；
g.共沉淀反应在搅拌条件下进行，搅拌速率为300-1000r/min；
h.共沉淀反应的终点为所述钠离子电池正极材料前驱体D50达到3-14μm；
i.水洗的终点(即水洗完成的标准)为洗涤液(即洗涤后过滤得到的母液)的电导率小于50μS/cm，干燥的温度为120-180℃，时间为10-16h，干燥的终点为物料水分含量小于等于0.6wt％。
可选地，对剩余的络合剂、剩余的沉淀剂和混合盐溶液加入底液的流速进行分阶段控制。
可选地，分阶段控制可以包括：
第一阶段时，控制混合盐溶液加入到底液中的第一流速为反应釜可用容积的2％/h-4％/h，控制沉淀剂加入到底液中的第一流速为反应釜可用容积的0.08％/h-0.16％/h，控制络合剂加入到底液中的第一流速为反应釜可用容积的0.04％/h-0.08％/h，直至得到第一沉淀D50为3-5μm；
第二阶段时，控制混合盐溶液加入到底液中的第二流速为反应釜可用容积的4％/h-8％/h， 控制沉淀剂加入到底液中的第二流速为反应釜可用容积的0.16-0.32％/h，控制络合剂加入到底液中的第二流速为反应釜可用容积的0.08-0.16％/h，直至钠离子电池正极材料前驱体D50为6-14μm。
反应釜可用容积为在搅拌不溅出液体时，加入底液后反应釜剩余的体积。
上述各溶液的第一流速、第二流速根据目标物料的D50大小进行调整。
本申请还提供一种钠离子电池正极材料，使用的钠离子电池正极材料前驱体和钠源反应制得。
可选地，钠离子电池正极材料前驱体中镍锰铁之和与钠源中钠的摩尔比为1：(1.02-1.07)；
可选地，反应采用程序升温进行煅烧：
以2-4℃/min的升温速率升至780-880℃进行煅烧10-20小时。
本申请还提供一种钠离子电池，其原料包括钠离子电池正极材料。
本申请还提供一种涉电设备，包括钠离子电池。
与相关技术相比，本申请的有益效果至少包括：
本申请提供的钠离子电池正极材料前驱体，以镍锰铁氢氧化物为基础，通过优化硫元素含量以及钠硫质量比，实现材料性能的提升；保留微量硫杂质含量时，在同等硫含量水平下，钠硫比越低，则电池容量、首效和循环性能越好；在2-4.2V范围内，0.1C首次放电容量>165mAh/g，1C放电容量>154mAh/g，1C条件下50周循环容量保持率>78％，在高循环效率条件下，充放电速率快。
具体的：钠离子电池正极材料前驱体中特定范围内的微量非钠硫酸盐存在于颗粒表面时，可抑制材料充放电过程产生的晶格裂纹；其溶解在电解液中时，有助于金属阳离子的扩散，降低DCR(直流阻抗)，且随着硫含量增加，可提高电池容量，并改善循环和倍率性能；但硫酸根含量过高会增加正极材料中的缺陷，从而降低结晶性，并且由于硫酸钠无法提升容量性能，所以硫含量越高，初始充放电容量越低，且烧结过程中硫酸盐的挥发会损坏设备；此外，前驱体中高钠含量(硫酸钠或氢氧化钠)会降低前驱体的结晶度，对电池性能有不利影响，所以在同等硫水平下，钠硫比越低，电池容量、首效和循环性能越好，成本低廉。
本申请提供的钠离子电池正极材料前驱体的制备方法，制备所得正极材料前驱体元素均匀性很好，结构缺陷少，粒度可控，球形度好；且钠含量低，硫含量适中。
本申请提供的钠离子电池正极材料、钠离子电池和涉电设备，电性能优异。
附图说明
为了更清楚地说明本申请实施例的技术方案，下面将对实施例中所需要使用的附图作 简单地介绍，应当理解，以下附图仅示出了本申请的某些实施例，因此不应被看作是对本申请范围的限定。
图1为实施例1得到的前驱体的扫描电镜图；
图2为实施例1得到的前驱体的XRD图；
图3为部分实施例放电容量随硫含量变化趋势图。
具体实施方式
为一种钠离子电池正极材料前驱体，其化学通式为NixMnyFe1-x-y(OH)2，其中，0.15≤x≤0.35，0.2≤y≤0.5；
钠离子电池正极材料前驱体中S元素含量≤4000ppm。
可选地，前驱体中还含有Na，且Na/S质量比≤1.5。
可选的，x可以为0.15、0.20、0.25、0.30、0.35或者0.15-0.35之间的任一值，y可以为0.2、0.3、0.4、0.5或者0.2-0.5之间的任一值。
在一个可选的实施方式中，钠离子电池正极材料前驱体满足以下条件中的至少一个：
A.钠离子电池正极材料前驱体中S元素含量为800-3700ppm，且Na/S质量比≤1.18；可选地，钠离子电池正极材料前驱体中S元素含量为1700-2800ppm，且Na/S质量比≤0.45；
可选的，钠离子电池正极材料前驱体中S元素含量可以为800ppm、900ppm、1000ppm、1100ppm、1200ppm、1300ppm、1400ppm、1500ppm、1600ppm、1700ppm、1800ppm、1900ppm、2000ppm、2100ppm、2200ppm、2300ppm、2400ppm、2500ppm、2600ppm、2700ppm、2800ppm、2900ppm、3000ppm、3100ppm、3200ppm、3300ppm、3400ppm、3500ppm、3600ppm、3700ppm或者800-3700ppm之间的任一值，且Na/S质量比可以为0.10、0.15、0.20、0.25、0.30、0.35、0.40、0.45、0.50、0.55、0.60、0.65、0.70、0.75、0.80、0.85、0.90、0.95、1.00、1.05、1.10、1.15、1.18或者≤1.18的任一值；
B.钠离子电池正极材料前驱体的D50为3-14μm，优选为5-10μm；
可选的，钠离子电池正极材料前驱体的D50可以为3μm、4μm、5μm、6μm、7μm、8μm、9μm、10μm、11μm、12μm、13μm、14μm或者3-14μm之间的任一值；
C.钠离子电池正极材料前驱体的比表面积为6-11m2/g，优选为6-8m2/g；
可选的，钠离子电池正极材料前驱体的比表面积可以为6m2/g、7m2/g、8m2/g、9m2/g、10m2/g、11m2/g或者6-11m2/g之间的任一值；
D.钠离子电池正极材料前驱体的振实密度为≥1.7g/cm3，优选为1.9-2.3g/cm3；
可选的，钠离子电池正极材料前驱体的振实密度可以为1.7g/cm3、1.8g/cm3、1.9g/cm3、2.0g/cm3、2.1g/cm3、2.2g/cm3、2.3g/cm3或者大于1.9-2.3g/cm3之间的任一值；
E.钠离子电池正极材料前驱体呈球形，或类球形。
本申请还提供一种的钠离子电池正极材料前驱体的制备方法，包括：
将包括镍源、锰源、亚铁源、水在内的原料混合得到混合盐溶液，将包括水、部分络合剂和部分沉淀剂在内的物料混合得到底液；
将剩余的络合剂、剩余的沉淀剂和混合盐溶液加入到底液中进行共沉淀反应，固液分离得到固体物，然后进行碱洗、水洗、干燥，得到钠离子电池正极材料前驱体；
镍源、锰源和亚铁源中的至少一者包括硫酸盐。
在一个可选的实施方式中，钠离子电池正极材料前驱体的制备方法，满足以下条件中的至少一个：
a.镍源包括硫酸镍、硝酸镍、乙酸镍中的一种或多种，锰源包括硫酸锰、硝酸锰、乙酸锰中的一种或多种，亚铁源包括硫酸亚铁、硝酸亚铁、氯化亚铁中的一种或多种；
b.混合盐溶液的浓度为1.0-2.2mol/L；
可选的，混合盐溶液的浓度可以为1.0mol/L、1.1mol/L、1.2mol/L、1.3mol/L、1.4mol/L、1.5mol/L、1.6mol/L、1.7mol/L、1.8mol/L、1.9mol/L、2.0mol/L、2.1mol/L、2.2mol/L或者1.0-2.2mol/L之间的任一值；
c.沉淀剂包括氢氧化钠和/或氢氧化钾，络合剂包括碳酸氢铵、碳酸铵、氨水中的一种或多种；
d.络合剂以水溶液形式使用，浓度为0.3～8mol/L，可选地，浓度为0.3-2.0mol/L；
可选的，络合剂水溶液的浓度可以为0.3mol/L、0.4mol/L、0.5mol/L、0.6mol/L、0.7mol/L、0.8mol/L、0.9mol/L、1.0mol/L、1.1mol/L、1.2mol/L、1.3mol/L、1.4mol/L、1.5mol/L、1.6mol/L、1.7mol/L、1.8mol/L、1.9mol/L、2.0mol/L、3.0mol/L、4.0mol/L、5.0mol/L、6.0mol/L、7.0mol/L、8.0mol/L或者0.3-8.0mol/L之间的任一值；
e.制备底液时使用的水的温度为40-60℃，并且升温使得制备得到的底液的温度为40-60℃；底液的pH为10-12；
可选的，水的温度可以为40℃、50℃、60℃或者40-60℃之间的任一值，底液的pH可以为10.0、10.5、11.0、11.5、12.0或者10-12之间的任一值；
f.混合盐溶液加入到底液中的流速为反应釜可用容积的2％/h-8％/h，沉淀剂加入到底液中的流速为0.08％/h-0.32％/h，络合剂加入到底液中的流速为0.04％/h-0.16％/h；
可选的，混合盐溶液加入底液的流速可以为反应釜可用容积的2％/h、3％/h、4％/h、5％/h、6％/h、7％/h、8％/h或者2-8％/h之间的任一值，沉淀剂加入底液的流速可以为反应釜可用容积的0.08％/h、0.10％/h、0.15％/h、0.20％/h、0.25％/h、0.30％/h、0.32％/h或者0.08％/h-0.32％/h之间的任一值，络合剂加入底液的流速为反应釜可用容积的0.04％/h、0.05％/h、0.06％/h、0.07％/h、0.08％/h、0.09％/h、0.10％/h、0.11％/h、0.12％/h、0.13％/h、0.14％/h、0.15％/h、 0.16％/h或者之间的任一值；
g.共沉淀反应在搅拌条件下进行，搅拌速率为300-1000r/min；
可选的，搅拌速率可以为300r/min、400r/min、500r/min、600r/min、700r/min、800r/min、900r/min、1000r/min或者300-1000r/min之间的任一值；
h.共沉淀反应的终点为所述钠离子电池正极材料前驱体D50达到3-14μm；
可选的，共沉淀反应的终点产物D50可以为3μm、4μm、5μm、6μm、7μm、8μm、9μm、10μm、11μm、12μm、13μm、14μm或者3-14μm之间的任一值；
i.水洗的终点(即水洗完成的标准)为洗涤液(即洗涤后过滤得到的母液)的电导率小于50μS/cm，干燥的温度为120-180℃，时间为10-16h，干燥的终点为物料水分含量小于等于0.6wt％。
可选的，水洗的终点的洗涤液电导率可以为10μS/cm、20μS/cm、30μS/cm、40μS/cm、49μS/cm或者小于50μS/cm的任一值，干燥的温度可以为120℃、130℃、140℃、150℃、160℃、170℃、180℃或者120-180℃之间的任一值，时间可以为10h、11h、12h、13h、14h、15h、16h或者10-16h之间的任一值，干燥的终点物料水分含量可以为0.1wt％、0.2wt％、0.3wt％、0.4wt％、0.5wt％、0.6wt％或者小于等于0.6wt％。
在一个可选的实施方式中，对剩余的络合剂、剩余的沉淀剂和混合盐溶液加入底液的流速进行分阶段控制。
在一个可选的实施方式中，分阶段控制包括：
第一阶段时，控制混合盐溶液加入到底液中的第一流速为反应釜可用容积的2％/h-4％/h，控制沉淀剂加入到底液中的第一流速为反应釜可用容积的0.08％/h-0.16％/h，控制络合剂加入到底液中的第一流速为反应釜可用容积的0.04％/h-0.08％/h，直至得到第一沉淀D50为3-5μm；
可选的，混合盐溶液加入到底液中的第一流速可以为反应釜可用容积的2％/h、3％/h、4％/h或者2％/h-4％/h之间的任一值；沉淀剂加入到底液的第一流速可以为络合剂反应釜可用容积的0.08％/h、0.09％/h、0.10％/h、0.11％/h、0.12％/h、0.13％/h、0.14％/h、0.15％/h、0.16％/h或者0.08％/h-0.16％/h之间的任一值；络合剂加入到底液的第一流速可以为沉淀剂反应釜可用容积的0.04％/h、0.05％/h、0.06％/h、0.07％/h、0.08％/h或者0.04％/h-0.08％/h之间的任一值；
第二阶段时，控制混合盐溶液加入到底液中的第二流速为反应釜可用容积的4％/h-8％/h，控制沉淀剂加入到底液中的第二流速为反应釜可用容积的0.16％/h-0.32％/h，控制络合剂加入到底液中的第二流速为反应釜可用容积的0.08％/h-0.16％/h，直至钠离子电池正极材料前驱体D50为6-14μm。
可选的，混合盐溶液加入到底液中的第二流速可以为反应釜可用容积的4％/h、5％/h、6％/h、7％/h、8％/h或者4％/h-8％/h之间的任一值，控制沉淀剂加入到底液中的第二流速可以为0.16％/h、0.18％/h、0.20％/h、0.22％/h、0.24％/h、0.26％/h、0.28％/h、0.30％/h、0.32％/h反应釜可用容积的或者0.16％/h-0.32％/h之间的任一值，控制络合剂加入到底液中的第二流速可以为反应釜可用容积的0.08％/h、0.09％/h、0.10％/h、0.11％/h、0.12％/h、0.13％/h、0.14％/h、0.15％/h、0.16％/h或者0.08％/h-0.16％/h之间的任一值。
混合盐流速采用分阶段控制，有利于前驱体结构内保留一定的硫含量，便于在洗涤阶段得到需要的硫含量。
本申请还提供一种钠离子电池正极材料，使用的钠离子电池正极材料前驱体和钠源反应制得。
在一个可选的实施方式中，钠离子电池正极材料前驱体中镍锰铁之和与钠源中钠的摩尔比为1：(1.02-1.07)；
在一个可选的实施方式中，反应采用程序升温进行煅烧：
以2-4℃/min的升温速率升至780-880℃进行煅烧10-20小时。
可选的，钠离子电池正极材料前驱体中镍锰铁之和与钠源中钠的摩尔比可以为1：1.02、1：1.03、1：1.04、1：1.05、1：1.06、1：1.07或者1：(1.02-1.07)之间的任一值；升温速率可以为2℃/min、3℃/min、4℃/min或者2-4℃/min之间的任一值，升温终点可以为780℃、800℃、820℃、840℃、860℃、880℃或者780-880℃之间的任一值，煅烧时间可以为10小时、12小时、14小时、16小时、18小时、20小时或者10-20小时之间的任一值。本申请还提供一种钠离子电池，其原料包括钠离子电池正极材料。
本申请还提供一种涉电设备，包括钠离子电池。
需要说明的是，此处所指的涉电设备可以是电动车、充电宝、手机等设备。
下面将结合具体实施例对本申请的实施方案进行详细描述，但是本领域技术人员将会理解，下列实施例仅用于说明本申请，而不应视为限制本申请的范围。实施例中未注明具体条件者，按照常规条件或制造商建议的条件进行。所用试剂或仪器未注明生产厂商者，均为可以通过市售购买获得的常规产品。
实施例1
本实施例提供一种钠离子电池正极材料前驱体，其制备方法如下：
将硫酸镍、硫酸锰、硫酸亚铁(摩尔比1:1:1)配制成2mol/L的混合盐溶液；在带搅拌装置的反应釜中加入50℃的去离子水、10mol/L的氢氧化钠溶液和8mol/L的氨水混合制备得到pH为11.5的底液。将反应釜温度升至50℃，在600r/min的搅拌速率下，缓慢加入氨水、氢氧化钠溶液、混合盐溶液，混合盐溶液加入到底液中的第一流速为反应釜可用容积 的2％/h，氢氧化钠溶液加入到底液中的第一流速为反应釜可用容积的0.08％/h，氨水加入到底液中的第一流速为反应釜可用容积的0.04％/h，直至得到第一沉淀D50为3.0μm，然后将混合盐溶液的第二流速增加到反应釜可用容积的4％/h，同步调节氨水溶液和氢氧化钠溶液的第二流速分别为反应釜可用容积的0.12％/h、0.20％/h，直至钠离子电池正极材料前驱体D50为10.0μm。
对上述钠离子电池正极材料前驱体沉淀物进行离心、洗涤，用0.5mol/L的氢氧化钠溶液进行多次碱洗，然后用70℃去离子水进行多次水洗，当水洗后过滤得到的母液电导率小于50μS/cm，即可认为完成洗涤，下同。
将离心洗涤后的固体物分散开，放入鼓风式烘箱中，在120℃条件下烘干脱水12h，干燥的终点为物料水分含量为0.4wt％，取出密封保存。
将得到的干燥料通过过筛、除磁等处理，得到钠离子电池正极材料前驱体，分子式为Ni0.33Mn0.33Fe0.34(OH)2。
图1为所得钠离子电池正极材料前驱体的扫描电镜图。图1显示制备的钠离子电池正极材料前驱体为球形度良好的球状结构，粒度分布较窄。图2为所得钠离子电池正极材料前驱体的XRD图。图2的XRD显示钠离子电池正极材料前驱体对应于α型氢氧化物。
本实施例1还提供一种钠离子电池正极材料，其制备方法如下：
将得到的前驱体和碳酸钠按照元素摩尔比(Ni+Mn+Fe):Na＝1:1.05进行混合后在马弗炉内以3℃/min的升温速率，升到830℃进行煅烧15小时，冷却后过筛，再将其组装成电池，在2-4.2V间测试其电池性能。
实施例2-15及对比例1-3
反应阶段与实施例1相同，得到镍铁锰三元沉淀物。
对上述钠离子电池正极材料前驱体沉淀物进行离心、洗涤，用0.5mol/L的氢氧化钠溶液进行多次碱洗，然后用70℃去离子水进行多次水洗，调整碱洗和水洗的洗涤次数、洗涤时长及洗涤用碱液量和用水量，使其Na杂质和S杂质含量分处于不同水平，其具体值如表1所示。
后续烘干处理、烧结成正极材料及制成电池步骤与实施例1相同。
实施例16-17及对比例4
将硫酸镍、硫酸锰、硫酸亚铁(摩尔比2:4:4)配制成2mol/L的混合盐溶液；在带搅拌装置的反应釜中加入40℃的去离子水、10mol/L的氢氧化钠溶液和8mol/L的氨水混合制备得到pH为11.5的底液。将反应釜内温度升至40℃，在1000r/min的搅拌速率下，缓慢加入氨水、氢氧化钠溶液、混合盐溶液，混合溶液盐的加入到底液中的第一流速为反应釜可用容积的4％/h，氢氧化钠溶液的加入到底液中的第一流速为反应釜可用容积的0.16％/h， 氨水的加入到底液中的第一流速为反应釜可用容积的0.08％/h，直至得到第一沉淀D50长大到5.0μm，然后将混合盐溶液的第二流速增加到反应釜可用容积的8％/h，同步调节氨水溶液和氢氧化钠溶液的第二流速分别为反应釜可用容积的0.12％/h、0.20％/h，直至钠离子电池正极材料前驱体D50长大到8.0μm，当前驱体D50达到8.0μm的情况下停止进料。
对上述钠离子电池正极材料前驱体沉淀物进行离心洗涤，用0.5mol/L的氢氧化钠溶液进行多次碱洗，然后用70℃去离子水进行多次水洗，调整碱洗和水洗的洗涤次数、洗涤时长及洗涤用碱液量和用水量，使其Na杂质和S杂质含量分处于不同水平，其具体值如表1所示。
后续烘干处理、烧结成正极材料及制成电池步骤与实施例1相同。所得钠离子电池正极材料前驱体的分子式为Ni0.2Mn0.4Fe0.4(OH)2。
对比例5
将硫酸镍、硫酸锰、硫酸亚铁(摩尔比2:4:4)配制成2mol/L的混合盐溶液；在带搅拌装置的反应釜中加入40℃的去离子水、10mol/L的氢氧化钠溶液和8mol/L的氨水混合制备得到pH为11.5的底液。将反应釜内温度升至40℃，在1000r/min的搅拌速率下，缓慢加入氨水、氢氧化钠溶液、混合盐溶液，混合盐溶液的加入到底液中的第一流速为反应釜可用容积的8％/h，氢氧化钠溶液的加入到底液中的第一流速为反应釜可用容积的0.32％/h，氨水的加入到底液中的第一流速为反应釜可用容积的0.16％/h，直至钠离子电池正极材料前驱体D50长大到8.0μm的情况下停止进料。
对上述沉淀物进行离心洗涤，洗涤方法与实施例16一致，其Na杂质和S杂质含量如表1所示。
后续烘干处理、烧结成正极材料及制成电池步骤与实施例16相同。所得钠离子电池正极材料前驱体的分子式为Ni0.2Mn0.4Fe0.4(OH)2。
表1实施例及对比例相关数据


由表1分别从实施例1～2、实施例3～5、实施例6～8、实施例9～12、实施例13～15可以看出，当S≤4000ppm，同水平硫含量下，钠硫比越低材料的性能越好。
图3为部分实施例放电容量随硫含量变化趋势图。由图3可知，对于Ni0.33Mn0.33Fe0.34(OH)2，当钠含量水平相当时，S含量增加可提高电池容量和倍率性能，但是S含量增加到一定值后，电池容量和倍率性能又下降。其中优选S:800～3700ppm，Na/S≤1.18，0.1C首次放电容量可以≥163mAh/g，50周循环容量保持率≥77.83％；最优选S:1700～2800ppm，Na/S≤0.45，0.1C首次放电容量可以≥166mAh/g，50周循环保持率≥78.2％；由对比例1可知，S＞4000ppm时，各性能均明显下降；由对比例2～3可知，Na/S＞1.5时，各性能也均明显下降。关于Ni0.2Mn0.4Fe0.4(OH)2的实施例16-17、对比例4也是同样的特点。因此特定范围内的微量非钠硫酸盐存在对材料的性能提高起到关键作用，且钠硫比越低材料的性能越好。
对比实施例16和对比例5，当只改变进料流量为全程采用大流量，而洗涤方法与其他均不变时，前驱体的硫含量下降，且钠硫比更高，导致了性能下降。因此混合盐流速采用分阶段控制，有利于前驱体结构内保留一定的硫含量，更易于获得上述特定范围内的硫含量及钠硫比的前驱体材料。
最后应说明的是：以上各实施例仅用以说明本申请的技术方案，而非对其限制；尽管参照前述各实施例对本申请进行了详细的说明，本领域的普通技术人员应当理解：其依然可以对前述各实施例所记载的技术方案进行修改，或者对其中部分或者全部技术特征进行等同替换；而这些修改或者替换，并不使相应技术方案的本质脱离本申请各实施例技术方案的范围。
此外，本领域的技术人员能够理解，尽管在此的一些实施例包括其它实施例中所包括的某些特征而不是其它特征，但是不同实施例的特征的组合意味着处于本申请的范围之内并且形成不同的实施例。例如，在上面的权利要求书中，所要求保护的实施例的任意之一都可以以任意的组合方式来使用。公开于该背景技术部分的信息仅仅旨在加深对本申请的总体背景技术的理解，而不应当被视为承认或以任何形式暗示该信息构成已为本领域技术人员所公知的现有技术。
工业实用性
本申请提供了一种钠离子电池正极材料前驱体及其制备方法、钠离子电池正极材料、钠离子电池和涉电设备，涉及电池领域。钠离子电池正极材料前驱体，其化学通式为NixMnyFe1-x-y(OH)2，其中，0.15≤x≤0.35，0.2≤y≤0.5；所述钠离子电池正极材料前驱体中S元素含量≤4000ppm，且Na/S质量比≤1.5。本申请提供的钠离子电池正极材料前驱体，制备所得正极材料元素均匀性很好，结构缺陷少，粒度可控，球形度好，能量密度高，在保留微量硫杂质含量下，在同水平硫含量下，钠硫比越低，电池容量、首效和循环性能越好。
此外，可以理解的是，本申请的钠离子电池正极材料前驱体及其制备方法、钠离子电池正极材料、钠离子电池和涉电设备是可以重现的，并且可以用在多种工业应用中。例如，本申请的钠离子电池正极材料前驱体及其制备方法、钠离子电池正极材料、钠离子电池和涉电设备可以用于电池领域。

Claims (10)

  1. 一种钠离子电池正极材料前驱体，其中，所述钠离子电池正极材料前驱体的化学通式为NixMnyFe1-x-y(OH)2，其中，0.15≤x≤0.35，0.2≤y≤0.5；
    所述钠离子电池正极材料前驱体中S元素含量≤4000ppm。
  2. 根据权利要求1所述的钠离子电池正极材料前驱体，其中，所述前驱体中还含有Na，且Na/S质量比≤1.5。
  3. 根据权利要求2所述的钠离子电池正极材料前驱体，其中，满足以下条件中的至少一个：
    A.所述钠离子电池正极材料前驱体中S元素含量为800-3700ppm，且Na/S质量比≤1.18；可选地，所述钠离子电池正极材料前驱体中S元素含量为1700-2800ppm，且Na/S质量比≤0.45；
    B.所述钠离子电池正极材料前驱体的D50为3-14μm，优选为5-10μm；
    C.所述钠离子电池正极材料前驱体的比表面积为6-11m2/g，优选为6-8m2/g；
    D.所述钠离子电池正极材料前驱体的振实密度为≥1.7g/cm3，优选为1.9-2.3g/cm3；
    E.所述钠离子电池正极材料前驱体呈球形，或类球形。
  4. 一种用于根据权利要求1至3中的任一项所述的钠离子电池正极材料前驱体的制备方法，其中，所述方法包括：
    将包括镍源、锰源、亚铁源、水在内的原料混合得到混合盐溶液，将包括水、部分络合剂和部分沉淀剂在内的物料混合得到底液；
    将剩余的所述络合剂、剩余的所述沉淀剂和所述混合盐溶液加入到所述底液中进行共沉淀反应，固液分离得到固体物，然后进行碱洗、水洗、干燥，得到所述钠离子电池正极材料前驱体；
    所述镍源、所述锰源和所述亚铁源中的至少一者包括硫酸盐。
  5. 根据权利要求4所述的钠离子电池正极材料前驱体的制备方法，其中，满足以下条件中的至少一个：
    a.所述镍源包括硫酸镍、硝酸镍、乙酸镍中的一种或多种，所述锰源包括硫酸锰、硝酸锰、乙酸锰中的一种或多种，所述亚铁源包括硫酸亚铁、硝酸亚铁、氯化亚铁中的一种或多种；
    b.所述混合盐溶液的浓度为1.0-2.2mol/L；
    c.所述沉淀剂包括氢氧化钠和/或氢氧化钾，所述络合剂包括碳酸氢铵、碳酸铵、氨水中的一种或多种；
    d.所述络合剂以水溶液形式使用，浓度为0.3～8mol/L，可选地，浓度为0.3-2.0mol/L；
    e.制备所述底液时使用的水的温度为40-60℃，所述底液的pH为10-12；
    f.所述混合盐溶液加入到所述底液中的流速为反应釜可用容积的2％/h-8％/h，所述沉淀剂加入到所述底液中的流速为所述反应釜可用容积的0.08％/h-0.32％/h，所述络合剂加入到所述底液中的流速为所述反应釜可用容积的0.04％/h-0.16％/h；
    g.所述共沉淀反应在搅拌条件下进行，搅拌速率为300-1000r/min；
    h.所述共沉淀反应的终点为所述钠离子电池正极材料前驱体D50达到3-14μm；
    i.所述水洗完成的标准为洗涤后过滤得到的母液的电导率小于50μS/cm，所述干燥的温度为120-180℃，时间为10-16h，所述干燥的终点为物料水分含量小于等于0.6wt％。
  6. 根据权利要求4或5所述的钠离子电池正极材料前驱体的制备方法，其中，对剩余的所述络合剂、剩余的所述沉淀剂和所述混合盐溶液加入所述底液的流速进行分阶段控制。
  7. 根据权利要求6所述的钠离子电池正极材料前驱体的制备方法，其中，所述分阶段控制包括：
    第一阶段时，控制所述混合盐溶液加入到所述底液中的第一流速为反应釜可用容积的2％/h-4％/h，控制所述沉淀剂加入到所述底液中的第一流速为反应釜可用容积的0.08％/h-0.16％/h，控制所述络合剂加入到所述底液中的第一流速为反应釜可用容积的0.04％/h-0.08％/h，直至得到第一沉淀D50为3-5μm；
    第二阶段时，控制所述混合盐溶液加入到所述底液中的第二流速为所述反应釜可用容积的4％/h-8％/h，控制所述沉淀剂加入到所述底液中的第二流速为所述反应釜可用容积的0.16-0.32％/h，控制所述络合剂加入到所述底液中的第二流速为所述反应釜可用容积的0.08-0.16％/h，直至所述的钠离子电池正极材料前驱体D50为6-14μm。
  8. 一种钠离子电池正极材料，其中，所述钠离子电池正极材料使用根据权利要求1至3中任一项所述的钠离子电池正极材料前驱体和钠源反应制得；
    可选地，所述钠离子电池正极材料前驱体中镍锰铁之和与所述钠源中钠的摩尔比为1：(1.02-1.07)；
    可选地，所述反应采用程序升温进行煅烧：
    以2-4℃/min的升温速率升至780-880℃进行煅烧10-20小时。
  9. 一种钠离子电池，其中，所述钠离子电池的原料包括根据权利要求8所述的钠离子电池正极材料。
  10. 一种涉电设备，其中，所述涉电设备包括根据权利要求9所述的钠离子电池。
PCT/CN2023/098145 2022-09-28 2023-06-02 钠离子电池正极材料前驱体及其制备方法、钠离子电池正极材料、钠离子电池和涉电设备 Ceased WO2024066445A1 (zh)

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