CN220502683U - Reaction device for graphite negative electrode material of battery - Google Patents
Reaction device for graphite negative electrode material of battery Download PDFInfo
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- CN220502683U CN220502683U CN202321737038.8U CN202321737038U CN220502683U CN 220502683 U CN220502683 U CN 220502683U CN 202321737038 U CN202321737038 U CN 202321737038U CN 220502683 U CN220502683 U CN 220502683U
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 67
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 31
- 229910002804 graphite Inorganic materials 0.000 title abstract description 26
- 239000010439 graphite Substances 0.000 title abstract description 26
- 239000007773 negative electrode material Substances 0.000 title description 8
- 238000010438 heat treatment Methods 0.000 claims abstract description 179
- 239000011248 coating agent Substances 0.000 claims abstract description 109
- 238000000576 coating method Methods 0.000 claims abstract description 109
- 238000005469 granulation Methods 0.000 claims abstract description 80
- 230000003179 granulation Effects 0.000 claims abstract description 80
- 239000000463 material Substances 0.000 claims abstract description 76
- 238000003763 carbonization Methods 0.000 claims abstract description 62
- 238000001816 cooling Methods 0.000 claims description 72
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 31
- 238000005253 cladding Methods 0.000 claims description 31
- 239000003546 flue gas Substances 0.000 claims description 31
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 20
- 238000002485 combustion reaction Methods 0.000 claims description 17
- 239000003345 natural gas Substances 0.000 claims description 10
- 238000009826 distribution Methods 0.000 claims description 4
- 239000007789 gas Substances 0.000 claims description 4
- 238000004321 preservation Methods 0.000 claims description 3
- 239000010405 anode material Substances 0.000 abstract description 14
- 238000000034 method Methods 0.000 abstract description 8
- 230000005465 channeling Effects 0.000 abstract description 4
- 238000005192 partition Methods 0.000 abstract description 2
- 238000007599 discharging Methods 0.000 description 25
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 18
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 14
- 239000000047 product Substances 0.000 description 13
- 238000005507 spraying Methods 0.000 description 13
- 238000007789 sealing Methods 0.000 description 11
- 239000010426 asphalt Substances 0.000 description 9
- 238000010000 carbonizing Methods 0.000 description 7
- 229910052757 nitrogen Inorganic materials 0.000 description 7
- 239000000126 substance Substances 0.000 description 6
- HBBGRARXTFLTSG-UHFFFAOYSA-N Lithium ion Chemical compound [Li+] HBBGRARXTFLTSG-UHFFFAOYSA-N 0.000 description 5
- 239000010406 cathode material Substances 0.000 description 5
- 229910001416 lithium ion Inorganic materials 0.000 description 5
- 239000000428 dust Substances 0.000 description 4
- 238000005087 graphitization Methods 0.000 description 4
- 230000007547 defect Effects 0.000 description 3
- 239000012467 final product Substances 0.000 description 3
- 210000001503 joint Anatomy 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000011331 needle coke Substances 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 239000002912 waste gas Substances 0.000 description 3
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000002006 petroleum coke Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 229910021383 artificial graphite Inorganic materials 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 229910052744 lithium Inorganic materials 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 235000021317 phosphate Nutrition 0.000 description 1
- 150000003013 phosphoric acid derivatives Chemical class 0.000 description 1
- 239000007774 positive electrode material Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
The utility model discloses a reaction device for a graphite anode material of a battery, which comprises a rotary reactor which is sequentially provided with a coating granulation section and a carbonization section, wherein the outer wall of a cylinder body at the coating material making section of the rotary reactor is provided with a plurality of heating furnaces which are distributed at intervals and used for providing heat for the coating material making section, the heating furnaces comprise a low-temperature coating granulation heating furnace and a high-temperature coating granulation heating furnace which are sequentially arranged along the material flow direction, and the low-temperature coating granulation heating furnace and the high-temperature coating granulation heating furnace are internally provided with coating material making sections with gradually-increased temperature. According to the utility model, the heating zone of the coating and granulating section of the rotary reactor is divided into two sections of coating and granulating sections, so that the temperature channeling problem caused by single heating temperature of the coating and granulating section is avoided, the effective proceeding of the coating and granulating process can be ensured by the two sections of temperature partition of the coating and granulating section, the coating and granulating reaction is orderly carried out, the volatilization rate of volatile components is controllable, the tap density of the product is higher, and the specific surface area is stable and controllable.
Description
Technical Field
The utility model belongs to the field of battery materials, and particularly relates to a preparation device of a graphite anode material.
Background
At present, graphite anode materials used in the lithium ion battery industry on a large scale are generally subjected to cladding granulation before graphitization so as to improve electrochemical performance, and carbonization is adopted to reduce material volatile matters and improve material tap density so as to improve material loading and operation safety of graphitization chemical industry. The preparation process of the graphite anode material of the lithium ion battery comprises the following steps of: firstly, petroleum coke/needle coke and asphalt are respectively crushed into 8-10 microns and 2-3 microns by a crushing device; mixing the two materials according to a certain proportion, then sending the mixture into a coating reaction kettle, arranging a resistance wire outside the reaction kettle, transferring heat to materials in the reaction kettle through the wall, controlling the temperature of the materials according to a certain temperature control curve, and finishing softening, melting of asphalt and coating and carbonization of focusing powder. However, the highest temperature of the materials is limited by heat transfer of equipment, the aromatic hydrocarbon which can be decomposed only at 650 ℃ when the high temperature of the asphalt is higher than 650 ℃ can not be decomposed, the materials which are coated on the reaction kettle are cooled to be lower than 100 ℃ by a cooling kettle of a water-cooling jacket indirect cooling device, then the materials are sent into a roller kiln or a tunnel kiln to be heated to 1000 ℃, the aromatic hydrocarbon in the asphalt is further decomposed and carbonized, then the materials are sent into a graphitization furnace to complete graphitization at about 3000 ℃, and the graphite cathode material of the carbon-based lithium battery is obtained after cooling and treatment.
The existing coating granulation-carbonization process for graphite anode materials of lithium ion batteries has the following problems: 1. the main thermal equipment reaction kettle and the cooling kettle are intermittent operation equipment, and the single equipment has low processing capacity and high labor cost; 2. the single equipment has small processing capacity and low production efficiency due to heat transfer limitation; 3. the thermal system is unreasonable, the materials are heated to 650 ℃ in the coating reaction kettle, the materials are cooled to normal temperature by an indirect water cooling method through a cooling kettle during discharging, then the materials are sent into a roller kiln or a tunnel kiln, the temperature is raised to about 1000 ℃ again, and then the materials are cooled to normal temperature, so that the energy waste is serious.
Patent application CN113101887A discloses a continuous reaction treatment device for graphite negative electrode materials of lithium ion batteries/phosphates of lithium ion batteries and ternary positive electrode materials, which can well solve the problems. However, the temperature of the continuous reaction equipment is only divided into two areas, namely a coating granulation reaction temperature area (medium-low temperature area) and a carbonization temperature area (high temperature area), the temperature of a coating granulation section is difficult to accurately control, the channeling temperature of a heating furnace is serious, and the temperature control requirement of the low temperature area of 250-400 ℃ is difficult to meet by the traditional burner heating. The defects and the defects can lead to a rapid increase of temperature curve in the inner length direction of the rotary reactor, the temperature is too high during coating and granulating, the volatilization rate of the volatile matters of the materials is too high during coating and granulating, the tap density of a coating and granulating product is low, the specific surface area is large, and the physical and chemical properties of the final product are low.
Disclosure of Invention
The utility model aims to overcome the defects and the shortcomings in the background art, and provides a reaction device for a battery graphite anode material with high tap density and small specific surface area. In order to solve the technical problems, the technical scheme provided by the utility model is as follows:
the utility model provides a reaction unit of battery graphite class negative pole material, includes the rotary reactor that is equipped with cladding pelleting section and carbomorphism section in proper order, the rotary reactor is equipped with on the barrel outer wall of cladding material section department of making and is used for providing a plurality of interval distribution's of heat heating furnaces for cladding material section, a plurality of the heating furnaces include the low temperature cladding pelleting heating furnace and the high temperature cladding pelleting heating furnace that arrange in proper order along the material flow direction, low temperature cladding pelleting heating furnace and high temperature cladding pelleting heating furnace are formed with the cladding material section of making that the temperature risees gradually in the rotary reactor.
In the above reaction apparatus, preferably, the coating and granulating section includes a low-temperature coating and granulating region controlled by a low-temperature coating and granulating heating furnace to form a low-temperature coating and granulating region controlled by a high-temperature coating and granulating heating furnace to form a high-temperature coating and granulating region at 350-750 ℃. More preferably, the high-temperature coating granulation heating furnace controls the formation of a high-temperature coating granulation zone with a temperature of 450-650 ℃.
In the above reaction device, preferably, the low-temperature coating granulation heating furnace includes two first heating furnaces and second heating furnaces which are distributed at intervals; the first heating furnace and the second heating furnace are internally provided with low-temperature coating granulation areas with gradually increased temperature; the low-temperature coating granulation zone comprises a first low-temperature coating granulation zone which is formed by controlling the first heating furnace and has the temperature of 250-400 ℃, and a second medium-temperature coating granulation zone which is formed by controlling the second heating furnace and has the temperature of 300-500 ℃. More preferably, the low-temperature coating granulation zone comprises a first low-temperature coating granulation zone with the temperature of 250-400 ℃ formed by controlling the first heating furnace, and a second medium-temperature coating granulation zone with the temperature of 400-650 ℃ formed by controlling the second heating furnace.
In the above reaction apparatus, preferably, the first heating furnace is a hot air heating furnace, and the second heating furnace and the high-temperature coating granulation heating furnace are natural gas burner combustion heating furnaces.
In the above reaction device, preferably, the first heating furnace is provided with a hot air inlet and a hot air outlet, the second heating furnace is provided with a first combustion-supporting fan, and the hot air outlet is communicated to the inlet of the first combustion-supporting fan through a hot air conveying pipe provided with a first induced draft fan, so as to realize energy saving of the combustion system.
In the above reaction device, preferably, a carbonization heating furnace for providing heat for the carbonization section is arranged on the outer wall of the cylinder body at the carbonization section of the rotary reactor, the carbonization heating furnace is arranged close to the Gao Wenbao granulation heating furnace, and the carbonization heating furnace is provided with the carbonization section with the temperature higher than that of the coating material making section in the rotary reactor. The carbonization section comprises a carbonization zone which is formed by controlling a carbonization heating furnace and has the temperature of 600-1150 ℃. The volatilization rate of volatile matters can be controlled by controlling the temperature of the carbonization heating furnace, and the specific surface area of the product is controlled.
In the above reaction device, preferably, a first cooling component for primarily cooling the material after passing through the carbonization section is further disposed on an outer wall of the barrel of the rotary reactor, and the first cooling component is disposed close to the carbonization section (the first cooling component is disposed close to the carbonization heating furnace). The first cooling assembly is used for cooling the reaction material to below 200 ℃.
In the above reaction apparatus, preferably, a second cooling unit for further cooling the reaction material to 60 ℃ or lower is further provided behind the first cooling unit along the material flow direction.
A first cooling component is arranged between the carbonization section of the rotary reactor and the middle discharging system to cool the reaction materials below 200 ℃, and a second cooling component is arranged between the middle discharging system and the discharging system to cool the materials below 60 ℃. The first cooling component and the second cooling component comprise a cooling machine, a water inlet pipe, a water outlet pipe, a spraying mechanism, a water spraying collecting tank, a water return pump and the like, wherein the water spraying collecting tank is arranged at the lower parts of the rotary reactor and the cooling machine, and the spraying mechanism is arranged above the rotary reactor and the cooling machine.
In the above reaction device, preferably, the carbonized flue gas discharged from the rotary reactor enters the flue gas incinerator through a flue gas pipeline after being dedusted by a flue gas deduster, the flue gas incinerator is provided with a hot gas outlet, and the hot gas outlet is communicated to a hot air inlet of the first heating furnace through a hot air furnace after being connected with a heat exchanger; and the flue gas pipeline is provided with a heat preservation device for preventing carbonized flue gas from condensing in the pipeline.
In the above reaction device, preferably, the rotary reactor is arranged obliquely, the feeding end of the rotary reactor is at a high position, and the discharging end of the rotary reactor is at a low position; the included angle between the central axis of the rotary reactor and the horizontal line is less than or equal to 10 degrees. The feeding end of the rotary reactor is provided with a kiln tail box body and a kiln tail sealing device, the discharging end of the rotary reactor is provided with a kiln head box body and a kiln head sealing device, and the kiln tail box body is provided with a smoke outlet for exhausting carbonized smoke in the rotary reactor; and the kiln tail sealing device and the kiln head sealing device are connected with a nitrogen pipeline.
The research of the inventor finds that the tap density and the specific surface area of the coated granulation product are greatly influenced by treatment of different temperature sections during the coating granulation reaction, and particularly, the tap density of the material after coating can be influenced within the temperature range of 250-500 ℃; the specific surface area of the coated material can be influenced at 350-750 ℃. More specifically, the tap density of the materials after coating is mainly affected within the temperature range of 250-450 ℃; the specific surface area of the coated material is mainly affected at 450-650 ℃.
To increase the tap density of the coated granulated product, the coated granulation should be subjected to a treatment at 250-450 ℃ for a period of time. In order to reduce the specific surface area of the product after coating granulation, the coating granulation should be performed at 450-650 ℃ for a period of time. According to the research results, during the continuous coating granulation reaction, the negative electrode base material and the coating material are respectively mixed and then sequentially pass through a specific temperature zone for heating reaction, and the final product has high tap density and small specific surface area. In a more preferred scheme, a coating section heating furnace of the rotary reactor is divided into three sections, the temperature of the first heating furnace is controlled to be between 250 and 400 ℃, the temperature of the second heating furnace is controlled to be between 400 and 450 ℃, and the temperature of a high-temperature coating granulation heating furnace is controlled to be between 450 and 650 ℃, so that the requirement of heating a material in a temperature division region within the range of between 250 and 450 ℃ of the coating section of the rotary reactor is met, and the phenomenon that the temperature of a low-temperature section is not controlled due to temperature channeling in the furnace when a single heating furnace is adopted in the coating section of the rotary reactor is prevented, and the reaction time of the low-temperature region is too short is further caused. By adopting the coated granulation temperature zone control of the utility model, the final product has high density, small specific surface area and good physical and chemical properties.
In addition, the heating mode of the first heating furnace is hot air heating, the heating temperature is easier to control, heat exchange hot air can be utilized, and energy sources are saved.
In the above reaction device, preferably, the first heating furnace, the second heating furnace, the high-temperature coating granulation heating furnace, the carbonization heating furnace and the cooling component are all coaxial with and spaced from the rotary reactor.
The utility model relates to a reaction device for a graphite anode material of a battery, which is a continuous coating granulation-carbonization reaction device and sequentially comprises a feeding system, a kiln tail box body, a rotary reactor, a kiln head box body, an intermediate discharging system, a second cooling component and a discharging system along the material flow direction, wherein the feeding system and the intermediate discharging system are in butt joint with corresponding feeding ends and discharging ends of the rotary reactor, and the rotary reactor comprises a graphite anode material coating granulation section connected with the feeding ends, a carbonization section connected with the coating granulation section and a cooling section, so that the reaction material is sequentially and continuously conveyed from the feeding ends, the coating granulation section, the carbonization section and the cooling section to the discharging ends.
A first heating furnace, a second heating furnace and a high-temperature coating granulation heating furnace which are used for realizing coating granulation of the reaction materials through heating are arranged outside the coating granulation section of the rotary reactor; a carbonization heating furnace for carbonizing the reaction materials by heating is arranged outside the carbonization section of the rotary reactor; and a water spraying device for cooling the reaction materials through water spraying is arranged outside the first cooling component and the second cooling component of the rotary reactor. The heating mode of the first heating furnace is hot air heating, and the heating modes of the second heating furnace, the high-temperature cladding granulation heating furnace and the carbonization heating furnace are natural gas burner burning heating. The second heating furnace, the high-temperature cladding granulation heating furnace and the carbonization heating furnace comprise a furnace body and heating parts which are arranged on the furnace body and extend into the furnace body. The high-temperature cladding granulation heating furnace and the carbonization heating furnace have higher temperature, and heat is recovered through the regenerative burner.
Support devices for forming support for the corresponding positions of the rotary reactor are arranged outside the rotary reactor at intervals; the rotary reactor comprises a reactor body and a rotary driving piece, wherein the reactor body is arranged in the first heating furnace, the second heating furnace, the high-temperature cladding granulation heating furnace, the carbonization heating furnace and the first cooling component in a penetrating manner and is in butt joint with the feeding system and the discharging system, and the rotary driving piece is arranged outside the reactor body and drives the reactor body to rotate.
The feeding system of the rotary reactor is communicated with the kiln tail box body through a feeding screw mechanism, and the discharge end of the rotary reactor is connected with the second cooling assembly through the middle discharge system and then discharged through the discharge system. Kiln tail sealing devices and kiln head sealing devices are respectively arranged on two sides of the feeding and discharging materials of the rotary reactor so as to ensure that external air does not enter the reactor; the sealing devices on the two sides of the material inlet and outlet of the rotary reactor and the second cooling assembly are provided with nitrogen inlet pipelines so as to ensure that nitrogen is filled into the reactor and ensure that the material is subjected to cladding granulation-carbonization reaction under the protection of nitrogen inert atmosphere.
When the reaction device for the graphite anode material of the battery is in operation, the rotary reactor is started first, so that the rotary reactor is operated and rotated; then starting the first heating furnace, the second heating furnace, the high-temperature cladding granulation heating furnace, the carbonization heating furnace and the first cooling component and the second cooling component, so that the body of the corresponding section reaches a corresponding preset temperature zone; starting the feeding system again, and enabling materials (such as needle coke and asphalt mixed according to a certain proportion) to enter the rotary reactor through the feeding system; and finally, starting a discharging system to ensure that the materials subjected to the coating carbonization are output from the discharging system. Compared with the traditional structure, the device realizes the continuity of the working procedures of coating, carbonizing and cooling the battery graphite negative electrode material through the integrated rotary reactor, ensures the consistency of products and obviously improves the quality of the products; the equipment for coating the anode material coating reaction kettle, cooling the cooling kettle, carbonizing the roller kiln or the tunnel kiln and indirectly cooling water is replaced, the process flow and the labor intensity and the number of operators are greatly simplified, the energy consumption per ton of products is also greatly reduced, the equipment investment, the labor cost and the energy consumption cost are obviously reduced, and the equipment can be enlarged; meanwhile, the computer automatic control is easy to realize, so that the production cost is greatly reduced.
Compared with the prior art, the utility model has the advantages that:
1. according to the reaction device for the graphite anode material of the battery, disclosed by the utility model, the temperature zone of the coating and granulating section is controlled, so that the volatilization rate of the material is proper during coating and granulating, the tap density of a coating and granulating product is high, the specific surface area is small, the physical and chemical properties are good, and the finally obtained graphite anode material is good in electrochemical properties.
2. According to the reaction device for the graphite anode material of the battery, the heating zone of the coating and granulating section of the rotary reactor is divided into two sections of coating and granulating sections, so that the temperature channeling problem caused by single heating temperature of the coating and granulating sections is avoided, the two sections of temperature partitions of the coating and granulating sections can ensure that the coating and granulating process is effectively carried out, the coating and granulating (such as asphalt coating coke powder) reaction is carried out orderly, the volatile component volatilization rate is controllable, the tap density of the product is higher, and the specific surface area is stable and controllable.
3. The reaction device for the graphite negative electrode material of the battery has the advantages of high tap density, small specific surface area and good physical and chemical properties of the graphite negative electrode product.
Drawings
In order to more clearly illustrate the embodiments of the present utility model or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described, and it is obvious that the drawings in the following description are some embodiments of the present utility model, and other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
Fig. 1 shows a reaction apparatus for a graphite-based negative electrode material of a battery according to an example.
Fig. 2 is another reaction device of the graphite-based negative electrode material of the battery of the embodiment.
Legend description:
1. a feed system; 2. a kiln tail box body; 3. kiln tail sealing device; 4. a rotary reactor; 5. a first heating furnace; 6. a second heating furnace; 7. coating a granulating heating furnace at a high temperature; 8. a carbonization heating furnace; 9. a first cooling assembly; 10. kiln head sealing device; 11. a kiln head box body; 12. a support device; 13. a driving device; 14. a second cooling assembly; 15. hot blast stove; 16. a first combustion fan; 17. a first induced draft fan; 18. a second induced draft fan; 19. a second combustion fan; 20. a third induced draft fan; 21. a water spraying collecting tank; 22. a water return pump; 23. a discharging system; 24. a flue gas dust remover; 25. and (5) coating a granulating heating furnace at a low temperature.
Detailed Description
The present utility model will be described more fully hereinafter with reference to the accompanying drawings, in which preferred embodiments are shown, for the purpose of illustrating the utility model, but the scope of the utility model is not limited to the specific embodiments shown.
Unless defined otherwise, all technical and scientific terms used hereinafter have the same meaning as commonly understood by one of ordinary skill in the art. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the scope of the present utility model.
Unless otherwise specifically indicated, the various raw materials, reagents, instruments, equipment and the like used in the present utility model are commercially available or may be prepared by existing methods.
Examples:
as shown in fig. 1, the reaction device for graphite cathode materials of a battery of this embodiment includes a rotary reactor 4 sequentially provided with a coating granulation section and a carbonization section, the rotary reactor 4 is provided with a plurality of heating furnaces which are distributed at intervals and used for providing heat for the coating granulation section on the outer wall of a cylinder at the coating granulation section, the plurality of heating furnaces include a low-temperature coating granulation heating furnace 25 and a high-temperature coating granulation heating furnace 7 which are sequentially arranged along the material flow direction, and the low-temperature coating granulation heating furnace 25 and the high-temperature coating granulation heating furnace 7 are provided with coating granulation sections with gradually-increased temperature in the rotary reactor 4.
In this embodiment, the coated strand comprises a low temperature coated strand region controlled by a low temperature coated strand furnace 25 to a temperature of 250-500℃ (all ranges described above) and a high temperature coated strand region controlled by a high temperature coated strand furnace 7 to a temperature of 350-750℃ (all ranges described above).
In the preferred embodiment, as shown in fig. 2, the low-temperature coating granulation heating furnace 25 comprises two first heating furnaces 5 and second heating furnaces 6 which are distributed at intervals; the first heating furnace 5 and the second heating furnace 6 are provided with low-temperature coating granulation areas with gradually increased temperature in the rotary reactor 4; the low-temperature coating granulation zone comprises a first low-temperature coating granulation zone which is formed by controlling the first heating furnace 5 at the temperature of 250-400 ℃ (all the above ranges), and a second medium-temperature coating granulation zone which is formed by controlling the second heating furnace 6 at the temperature of 300-500 ℃ (all the above ranges).
In a further preferred embodiment, the low-temperature coating granulation zone includes a first low-temperature coating granulation zone controlled by the first heating furnace 5 to have a temperature of 250-400 ℃ (all ranges can be used), and a second medium-temperature coating granulation zone controlled by the second heating furnace 6 to have a temperature of 400-450 ℃ (all ranges can be used), and the high-temperature coating granulation heating furnace 7 is controlled to have a temperature of 450-650 ℃ (all ranges can be used).
In this embodiment, the first heating furnace 5 is a hot air heating furnace, and the second heating furnace 6 and the high-temperature coating granulation heating furnace 7 are natural gas burner combustion heating furnaces.
In this embodiment, the first heating furnace 5 is provided with a hot air inlet and a hot air outlet, the second heating furnace 6 is provided with a first combustion-supporting fan 16, and the hot air outlet is communicated to the inlet of the first combustion-supporting fan 16 through a hot air conveying pipe provided with a first induced draft fan 17.
In the embodiment, a carbonization heating furnace 8 for providing heat for the carbonization section is arranged on the outer wall of the cylinder body at the carbonization section of the rotary reactor 4, the carbonization heating furnace 8 is arranged close to a high-temperature cladding granulation heating furnace 7, and the carbonization heating furnace 8 is provided with a carbonization section with the temperature higher than that of the cladding material making section in the rotary reactor 4. The carbonization section comprises a carbonization zone with the temperature of 600-1150 ℃ which is controlled by a carbonization heating furnace 8.
In this embodiment, a first cooling component 9 for primarily cooling the material after passing through the carbonization section is further disposed on the outer wall of the barrel of the rotary reactor 4, the first cooling component 9 is disposed near the carbonization section, and the first cooling component 9 is used for cooling the reaction material to below 200 ℃. A second cooling assembly 14 is also arranged behind the first cooling assembly 9 along the material flow direction, and the second cooling assembly 14 is used for further cooling the reaction material to below 60 ℃.
In the embodiment, carbonized flue gas discharged from the rotary reactor 4 enters a flue gas incinerator through a flue gas pipeline after being dedusted by a flue gas deduster 24, and the flue gas incinerator is provided with a hot gas outlet which is communicated with a hot air inlet of the first heating furnace 5 through a hot air furnace 15 after being connected with a heat exchanger; the flue gas pipeline is provided with a heat preservation device for preventing carbonized flue gas from condensing in the pipeline.
In the embodiment, the rotary reactor 4 is obliquely arranged, the feeding end of the rotary reactor 4 is at a high position, and the discharging end of the rotary reactor 4 is at a low position; the included angle between the central axis of the rotary reactor 4 and the horizontal line is less than or equal to 10 degrees.
Specifically, the reaction device for the graphite cathode material of the battery of the embodiment comprises a feeding system 1, a kiln tail box 2, a rotary reactor 4, a kiln head box 11, an intermediate discharging system, a second cooling component 14 and a discharging system 23, wherein the feeding system 1 and the discharging system 23 are in butt joint with corresponding feeding ends and discharging ends of the rotary reactor 4, and the rotary reactor 4 comprises a graphite cathode material coating granulating section connected with the feeding ends and a graphite cathode material carbonizing section and a cooling section connected with the coating granulating section, so that the reaction materials are sequentially and continuously conveyed from the feeding ends, the coating granulating section, the carbonizing section and the cooling section to the discharging ends. A first heating furnace 5, a second heating furnace 6 and a high-temperature coating granulation heating furnace 7 which are used for realizing coating granulation of the reaction materials by heating are arranged outside the coating granulation section of the rotary reactor 4; a carbonization heating furnace 8 for carbonizing the reaction materials by heating is arranged outside the carbonization section of the rotary reactor 4; outside the first cooling module 9 and the second cooling module 14 of the rotary reactor 4 are arranged water spraying devices for cooling the reaction mass by spraying water.
The first heating furnace 5 is heated by hot air, and the second heating furnace 6, the high-temperature cladding granulation heating furnace 7 and the carbonization heating furnace 8 are heated by natural gas burner combustion. In the process of establishing the first, second, third and fourth temperature fields (corresponding to the first heating furnace 5, the second heating furnace 6, the high-temperature cladding granulation heating furnace 7 and the carbonization heating furnace 8 respectively), no material exists in the rotary reactor 4, no volatile matters enter the incinerator for incineration treatment, and the hot air of the first heating furnace 5 is provided by adopting a hot air furnace 15 for burning natural gas. After the materials enter the rotary reactor 4 for treatment, the flue gas enters an incinerator for incineration, and hot air obtained by heat exchange between high-temperature waste gas generated by the flue gas incineration and fresh air enters the hot air furnace 15 to provide a heat source for the first heating furnace 5. The hot air at the outlet of the first heating furnace 5 is sent out to the inlet of the first combustion-supporting fan 16 of the second heating furnace 6 through the first induced draft fan 17 to be used as the combustion air of the second heating furnace 6 to realize energy saving of a combustion system, a natural gas combustion burner device is arranged on the second heating furnace 6, natural gas and the combustion air sent in through the first combustion-supporting fan 16 are mixed to burn and release heat, and the combustion waste gas of the second heating furnace 6 is discharged outside through the second induced draft fan 18. The high-temperature coating granulation heating furnace 7 and the carbonization heating furnace 8 are both provided with natural gas combustion burner devices, natural gas and combustion air fed by the second combustion-supporting fan 19 are mixed and combusted to release heat, and combustion waste gas of the high-temperature coating granulation heating furnace 7 and the carbonization heating furnace 8 is discharged through the third induced draft fan 20.
The first cooling component 9 and the second cooling component 14 comprise a cooling machine, a water inlet pipe, a water outlet pipe, a spraying mechanism, a water spraying collecting tank 21, a water return pump 22 and the like, wherein the water spraying collecting tank 21 is arranged at the lower parts of the rotary reactor 4 and the cooling machine, and the spraying mechanism is arranged above the rotary reactor 4 and the cooling machine.
Nitrogen with purity not lower than 99% is introduced into the kiln tail box body 2, the kiln tail sealing device 3, the kiln head box body 11, the kiln head sealing device 10 and the second cooling component 14 of the rotary reactor 4 so that the materials react under the protection of nitrogen inert atmosphere.
The outside of the rotary reactor 4 is provided with supporting devices 12 at intervals for supporting the respective corresponding positions of the rotary reactor 4. Because the rotary reactor 4 is of a continuous integral structure, the length of the rotary reactor is longer, and the supporting devices 12 are arranged at intervals, so that the rotary reactor 4 is conveniently supported, and the stability of equipment is improved.
A driving device 13 for rotationally driving the rotary reactor 4 is installed outside the rotary reactor 4.
A flue gas dust remover 24 (such as a cloth bag filter treatment device) is arranged on a flue gas outlet pipeline of the kiln tail box body 2 of the rotary reactor 4 to carry out dust purification on flue gas so as to prevent dust from settling and blocking in a subsequent flue gas pipeline. An electric tracing device is arranged on a flue gas outlet pipeline of a kiln tail box body 2 of the rotary reactor 4 so as to prevent low boiling point substances such as asphalt in flue gas from condensing in the flue gas pipeline to block the pipeline.
Specifically, when the reaction device for graphite-based negative electrode material of the battery of this embodiment is used, the following steps may be included: first, the rotary reactor 4 and the first cooling component 9 are started; then starting each heating furnace and cooling water arranged outside the first cooling component 9 and the second cooling component 14 to enable the corresponding sections to reach the corresponding preset temperature areas; starting the feeding system 1 again, and conveying the mixed materials (such as needle coke and asphalt) mixed according to a certain proportion into the rotary reactor 4 through the feeding system 1; and finally, starting the middle discharging system and the discharging system 23 to ensure that the materials subjected to coating carbonization are output from the discharging system 23.
In order to better understand the scheme in the above embodiment, the present embodiment provides a typical process for coating, granulating and carbonizing an artificial graphite anode material by using the reaction device, and the preparation method includes the following steps:
(1) Selecting ash less than 0.6%, sulfur less than 0.5%, volatile less than 13%, and water<10% of petroleum coke is used as raw material, and is dried to moisture by a roller dryer<3, grinding with a mechanical mill, wherein the particle size distribution D of the ground coke powder 50 Material a was obtained =10 μm.
(2) Mixing the material A with asphalt with a softening point of 200-250 ℃ to obtain a mixture of 100:4, sending the mixture into a mixer for mixing to obtain a material B; the mixed materials are sent into a continuous feed bin through a vacuum feeder, then sent into a rotary reactor 4 through a screw conveyor, and are subjected to cladding granulation and carbonization under the protection of nitrogen along with the rotation and self-pushing of the rotary reactor 4, wherein the included angle between the axis of the rotary reactor 4 and a horizontal line is 1.5 degrees, the rotating speed is 0.5rpm, the temperatures of a first heating furnace 5, a second heating furnace 6, a high-temperature cladding granulation heating furnace 7 and a carbonization heating furnace 8 are respectively controlled to be 300 ℃, 450 ℃, 650 ℃ and 950 ℃, and a cladding granulation carbonized product C is obtained after cooling through a cooling section.
Through detection, the granularity distribution D of the material C 50 =15.60 μm, tap density of 0.90g/cm3, specific surface area of 1.8m 2 /g, volatile content<0.6%. The product has excellent tap density and specific surface area performance data, and the electrochemical performance of the finally obtained battery is excellent.
Claims (10)
1. The utility model provides a reaction unit of battery graphite class negative pole material, includes rotary reactor (4) that are equipped with cladding pelleting section and carbomorphism section in proper order, its characterized in that, rotary reactor (4) are equipped with on the barrel outer wall of cladding material section department and are used for providing thermal a plurality of interval distribution's heating furnace for cladding material section, a plurality of the heating furnace is including low temperature cladding pelleting heating furnace (25) and high temperature cladding pelleting heating furnace (7) that follow the material flow direction and arrange in proper order, low temperature cladding pelleting heating furnace (25) and high temperature cladding pelleting heating furnace (7) are formed with the cladding material section of making that the temperature gradually risees in rotary reactor (4).
2. The reaction apparatus according to claim 1, characterized in that the coated strand comprises a low-temperature coated granulation zone with a temperature of 250-500 ℃ controlled by a low-temperature coated granulation heating furnace (25), and a high-temperature coated granulation zone with a temperature of 350-750 ℃ controlled by a high-temperature coated granulation heating furnace (7).
3. The reaction device according to claim 2, characterized in that the low-temperature coating granulation heating furnace (25) comprises two first heating furnaces (5) and second heating furnaces (6) which are distributed at intervals; the first heating furnace (5) and the second heating furnace (6) are internally provided with low-temperature coating granulation areas with gradually increased temperature in the rotary reactor (4);
the low-temperature coating granulation zone comprises a first low-temperature coating granulation zone which is formed by controlling the first heating furnace (5) at the temperature of 250-400 ℃ and a second medium-temperature coating granulation zone which is formed by controlling the second heating furnace (6) at the temperature of 300-500 ℃.
4. A reaction device according to claim 3, characterized in that the first heating furnace (5) is a hot air heating furnace, and the second heating furnace (6) and the high temperature coated granulation heating furnace (7) are natural gas burner combustion heating furnaces.
5. The reaction device according to claim 4, characterized in that the first heating furnace (5) is provided with a hot air inlet and a hot air outlet, the second heating furnace (6) is provided with a first combustion fan (16), and the hot air outlet is communicated to the inlet of the first combustion fan (16) through a hot air conveying pipe provided with a first induced draft fan (17).
6. The reaction device according to any one of claims 1-5, characterized in that the rotary reactor (4) is provided with a carbonization heating furnace (8) on the outer wall of the cylinder at the carbonization section for providing heat to the carbonization section, the carbonization heating furnace (8) is arranged close to the Gao Wenbao granulation heating furnace (7), and the carbonization heating furnace (8) is provided with a carbonization section with a temperature higher than that of the cladding material making section in the rotary reactor (4).
7. The reaction device according to any one of claims 1 to 5, characterized in that a first cooling component (9) for primarily cooling the material after passing through the carbonization section is further arranged on the outer wall of the cylinder of the rotary reactor (4), and the first cooling component (9) is arranged close to the carbonization section.
8. The reaction device according to claim 7, characterized in that a second cooling module (14) for further cooling the reaction mass to below 60 ℃ is also provided downstream of the first cooling module (9) in the mass flow direction.
9. The reaction device according to any one of claims 4 to 5, characterized in that the carbonized flue gas discharged from the rotary reactor (4) enters a flue gas incinerator through a flue gas duct after being dedusted by a flue gas deduster (24), the flue gas incinerator is provided with a hot gas discharge port which is communicated to a hot air inlet of the first heating furnace (5) through a hot air furnace (15) after being connected with a heat exchanger; and the flue gas pipeline is provided with a heat preservation device for preventing carbonized flue gas from condensing in the pipeline.
10. The reaction device according to any one of claims 1 to 5, characterized in that the rotary reactor (4) is arranged obliquely, the feed end of the rotary reactor (4) being in a high position and the discharge end being in a low position; the included angle between the central axis of the rotary reactor (4) and the horizontal line is less than or equal to 10 degrees.
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| CN202321737038.8U CN220502683U (en) | 2023-07-04 | 2023-07-04 | Reaction device for graphite negative electrode material of battery |
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| CN202321737038.8U CN220502683U (en) | 2023-07-04 | 2023-07-04 | Reaction device for graphite negative electrode material of battery |
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