CN211789274U - Production device for co-production of anode material and isotropic coke - Google Patents
Production device for co-production of anode material and isotropic coke Download PDFInfo
- Publication number
- CN211789274U CN211789274U CN202020174605.3U CN202020174605U CN211789274U CN 211789274 U CN211789274 U CN 211789274U CN 202020174605 U CN202020174605 U CN 202020174605U CN 211789274 U CN211789274 U CN 211789274U
- Authority
- CN
- China
- Prior art keywords
- pay
- coking
- tower
- centrifuge
- screening machine
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- 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
Abstract
The utility model provides an apparatus for producing of isotropic burnt of cathode material coproduction, including melting jar, centrifuge, fractionating tower, 1# coking tower group, 2# coking tower group, rubbing crusher, 1# screening machine, 2# screening machine, retort, graphitizing furnace, melt jar connection centrifuge, centrifuge's heavy phase export is to 1# coking tower group pay-off, centrifuge's light phase exit linkage fractionating tower, fractionating tower heavy phase export is to 2# coking tower group pay-off, 2# coking tower group's solid phase export is to rubbing crusher pay-off, and rubbing crusher is to 1# screening machine pay-off, and 1# screening machine is to the carbonizing furnace pay-off, and the graphitizing furnace is to the graphitizing furnace pay-off, and graphitizing furnace is to 2# screening machine pay-off. The utility model discloses the high energy density negative pole material of preparation, battery discharge capacity height, compaction height, fast charge can be good, long cycle life, low temperature power is excellent, high temperature storage decay reduces, and simple feasible and continuous production of process method is lithium ion battery's good negative pole raw materials.
Description
Technical Field
The utility model belongs to the negative electrode material field especially relates to a production device of negative electrode material coproduction isotropic burnt.
Background
With the upgrading of industrial structures and the requirement of environmental protection in the steel industry at home and abroad, the proportion of the capacity of electric arc furnace steelmaking to the total capacity of the steel industry is gradually increased, so that the demand of graphite electrodes at home and abroad is increased year by year. The demand of coal-based needle coke, which is one of the raw materials of graphite electrodes, is also increased year by year, but the domestic production of coal-based needle coke generates a large amount of byproducts, namely solvent settling residual oil, during the pretreatment of the raw materials, the yield of the byproducts is large, a large amount of capital and storage space of enterprises are occupied, and the environmental pollution is caused due to the rich aromatic hydrocarbon. Therefore, the treatment of the solvent settling residual oil and the high value-added utilization are significant to enterprise benefits and environmental protection,
although the solvent settling residual oil is derived from heavy components generated in the pretreatment process of the coal-based needle coke raw material, the residual oil is very similar to light components, for example, the residual oil and the light components are rich in fused ring aromatic hydrocarbon and are precursors for preparing excellent carbon materials.
Meanwhile, in recent years, the industry of new energy automobiles at home and abroad is greatly developed, and electric automobiles occupy the absolute share of the market of new energy automobiles, so that the demand of carbon cathode materials in electric automobile batteries is more and more large, the price is high, and the solvent settling residual oil is developed into the carbon cathode materials capable of meeting the demand of the electric automobile batteries, so that the method has great economic significance.
The power battery cathode material has the characteristics of high energy density, long cycle life, high compaction density, excellent quick charge performance, lower production cost, good high and low temperature performance and the like. Therefore, the development of the power battery negative electrode material by using the low-cost solvent to settle the residual oil has great potential application value.
SUMMERY OF THE UTILITY MODEL
The utility model provides a production device of negative electrode material coproduction isotropic coke, with different residual oils, directly get into centrifuge separation after melting, the centrifuge heavy phase gets into 1# coking tower and obtains isotropic coke, the centrifuge light phase gets into the fractionating tower, the fractionating tower heavy phase gets into 2# coking tower group and obtains anisotropic burnt, anisotropic burnt is through smashing, screening, obtains raw coke powder, raw coke powder obtains the high energy density negative electrode material that accords with the power battery demand through carbomorphism, graphitization, screening. The utility model discloses the high energy density negative pole material of preparation, battery discharge capacity height, compaction height, fast charge can be good, long cycle life, low temperature power is excellent, high temperature storage decay reduces, and simple feasible and continuous production of process method is lithium ion battery's good negative pole raw materials.
In order to achieve the above object, the utility model adopts the following technical scheme:
the utility model provides a production device of isotropic burnt of cathode material coproduction, includes melting jar, centrifuge, fractionating tower, 1# coking tower group, 2# coking tower group, rubbing crusher, 1# screening machine, 2# screening machine, retort, graphitizing furnace, melting jar connection centrifuge, centrifuge's heavy phase export is to 1# coking tower pay-off, centrifuge's light phase exit linkage fractionating tower, fractionating tower heavy phase export is to 2# coking tower group pay-off, 2# coking tower group's solid phase export is to rubbing crusher pay-off, and the rubbing crusher is to 1# screening machine pay-off, and 1# screening machine is to the carbonizing furnace pay-off, and the carbonizing furnace is to the graphitizing furnace pay-off, and graphitizing furnace is to 2# screening machine pay-off.
The No. 1 coking tower group consists of two coking towers; the 2# coking tower group consists of two coking towers.
Compared with the prior art, the beneficial effects of the utility model are that:
1) the high-energy-density cathode material prepared by the utility model obtains a large number of streamline structures and large sheet structures by controlling the carbonization process parameters, has high energy density, good circulation, good high and low temperature performance and good quick charging performance, and is an excellent cathode material of a lithium battery;
2) the isotropic coke prepared by the utility model obtains a large amount of fine mosaic structures by controlling the carbonization process parameters, has the characteristics of high strength, high density and high purity after the isotropic coke is graphitized, and has great application potential on three-high graphite;
3) the cathode material prepared by the utility model has the advantages of high battery safety performance, high capacity, good rate performance, excellent cycle performance and outstanding attenuation resistance;
4) the coking tower adopted by the utility model is a continuous production device, continuous production is realized, and the maximization of productivity is ensured;
5) the utility model discloses a fractionating tower sell the light phase oil of distilling out.
6) Through the utility model discloses the negative pole material that production technology prepared is through the test, and its battery performance is excellent, and cycle life is long, and the quick performance of filling is good, and high low temperature performance is excellent, is a high-quality power battery negative pole material, and production technology can realize producing even, and economic benefits is considerable.
Drawings
Fig. 1 is a process flow diagram of the present invention.
In the figure: 1-a raw material tank; 2-a melting tank; 3-a centrifuge; 4-a fractionation column; a 5-1# coking tower group A tower; 6-1# coking tower B tower; 7-a light phase extraction outlet of the fractionating tower; 8-isotropic coke outlet; a 9-2# coking tower group C tower; a 10-2# coking tower group D tower; a light phase extraction outlet of the 11-2# coking tower group; 12-a pulverizer; 13-1# screening machine; 14-a carbonization furnace; 15-graphitizing furnace; 16-2# screening machine; 17-finished product warehouse.
Detailed Description
The following embodiments are further described in detail:
as shown in figure 1, different residual oils are directly melted and then enter a centrifuge 3 for separation, the heavy phase of the centrifuge 3 enters a 1# coking tower group (a tower 5 of the 1# coking tower group and a tower 6 of the 1# coking tower group) to prepare isotropic coke, the light phase of the centrifuge 3 enters a fractionating tower 4, the light phase of the fractionating tower 4 is directly taken out for sale, the heavy phase of the fractionating tower 4 enters a 2# coking tower group (a tower 9 of the 2# coking tower group and a tower D10 of the 2# coking tower group) to prepare anisotropic coke, the anisotropic coke is crushed and screened to obtain raw coke powder, and the raw coke powder is carbonized, graphitized and screened to obtain the high-energy-density negative material meeting the requirements of power batteries.
The specific process steps comprise:
1) pretreatment of raw materials: residual oil is pumped out from the raw material tank 1 by a pump and directly enters the melting tank 2 for melting;
2) centrifuging: the residual oil is separated into a light phase and a heavy phase after being centrifuged by a centrifuge 3;
3) centrifuge 3 heavy phase coking: pumping out the heavy phase of the centrifuge 3 by a pump, and coking the heavy phase in a No. 1 coking tower set (a tower 5 of the No. 1 coking tower set and a tower B of the No. 1 coking tower set) to prepare isotropic coke; directly extracting a light phase coked and distilled by the No. 1 coking tower group (the No. 1 coking tower group A tower 5 and the No. 1 coking tower group B tower) for sale;
4) centrifuge 3 light phase distillation: a light phase of the centrifuge 3 is pumped out by a pump and enters a fractionating tower 4, light phase oil and heavy phase oil are obtained by distillation, the light phase oil fraction is directly extracted for sale, the heavy phase of the fractionating tower 4 is pumped out by a pump and enters a 2# coking tower set (a 2# coking tower set C tower 9 and a 2# coking tower set D tower 10) to be coked, and the light phase of the 2# coking tower set (a 2# coking tower set C tower 9 and a 2# coking tower set D tower 10) is directly extracted for sale;
5) crushing and screening: after the 2# coking tower group (2# coking tower group C tower 9 and 2# coking tower group D tower 10) is coked, the raw coke enters a crusher 12 for crushing and a 1# sieving machine 13 for sieving, and finally qualified raw coke powder is obtained;
6) carbonizing: the raw coke powder enters a carbonization furnace 14 for carbonization;
7) graphitization: and (4) graphitizing the carbonized product in a graphitization furnace 15, screening the graphitized sample into a finished product by using a 2# screening machine 16, and packaging the finished product.
The residual oil is residual oil obtained after the needle coke raw material solvent is settled, petroleum crude oil vacuum residual oil and petroleum crude oil atmospheric residual oil.
In the step 1), the melting temperature of the melting tank 2 is 100-220 ℃, the heating rate is 1-20 ℃/min, the constant temperature time is 0.5-12 h, and the stirring speed is 5-50 r/min.
The rotating speed of the centrifuge 3 in the step 2) is 100-.
The pressure of the 1# coking tower set (the 1# coking tower set A tower 5 and the 1# coking tower set B tower) in the step 3) is 0.1-3 Mpa, the coking temperature is 450-580 ℃, the heating rate is 1-30 ℃/min, and the constant temperature time is 1-20 h; the micro structure of the coked green coke is a sheet structure with the length of 0-2 mu m and the width of 0-2 mu m.
The temperature of the fractionating tower 4 in the step 4) is 200-300 ℃; the pressure of the 2# coking tower set (the 2# coking tower set C tower 9 and the 2# coking tower set D tower 10) is 0.1-3 Mpa, the coking temperature is 450-580 ℃, the heating rate is 1-30 ℃/min, and the constant temperature time is 1-20 h.
The crushing and screening granularity D50 in the step 5) is 14-18 mu m.
The carbonization temperature in the step 6) is 1100-1300 ℃, the heating rate is 1-15 ℃/min, and the constant temperature time is 1-6 h.
The graphitization temperature in the step 7) is 2800 ℃, the heat preservation time is 1-4h, and the heating rate is 10-20 ℃; the screening particle size D50 is 14-18 μm.
A production device for co-production of anode materials and isotropic coke comprises a raw material tank 1, a melting tank 2, a centrifugal machine 3, a fractionating tower 4, a # 1 coking tower set, a # 2 coking tower set, a pulverizer 12, a # 1 sieving machine 13, a # 2 sieving machine 16, a carbonization furnace 14 and a graphitization furnace 15, wherein the raw material tank 1 feeds materials to the melting tank 2 through an oil pump, the melting tank 2 is connected with a centrifuge 3, a heavy phase outlet of the centrifuge 3 feeds materials to a No. 1 coking tower group, the light phase outlet of the centrifuge 3 is connected with a fractionating tower 4, the light phase of the fractionating tower 4 is directly extracted for sale, the heavy phase outlet of the fractionating tower 4 feeds materials to the # 2 coking tower set, the solid phase outlet of the # 2 coking tower set feeds materials to the crusher 12, the crusher 12 feeds materials to the # 1 screening machine 13, the # 1 screening machine 13 feeds materials to the carbonization furnace 14, the carbonization furnace 14 feeds materials to the graphitization furnace 15, and the graphitization furnace 15 feeds materials to the # 2 screening machine 16.
The raw material tank 1 is provided with a stirrer, and the melting tank 2 is provided with a stirrer and a heater.
The 1# coking tower group consists of two coking towers, namely a 1# coking tower group A tower 5 and a 1# coking tower group B tower, and coking and coke discharging are alternately used; the 2# coking tower group consists of two coking towers, namely a 2# coking tower group C tower 9 and a 2# coking tower group D tower 10, and coking and coke discharging are alternately used.
Example (b):
by adopting the production device and the production process for co-producing the anode material and the isotropic coke, the main indexes of 3 batches are recorded and are shown in the table 1;
TABLE 1 batches of raw materials and their main indices
| Batches of | Raw materials | Softening Point (. degree. C.) | QI(wt％) | Ash content (wt%) |
| 1 | Solvent settled residua | Is free of | 4.57 | 0.52 |
| 2 | Atmospheric residuum | Is free of | 1.24 | 0.29 |
| 3 | Vacuum residuum | Is free of | 2.36 | 0.14 |
The centrifuge process parameters in the examples are shown in Table 2
TABLE 2 centrifuge Process Key parameters
The technological parameters of the coking tower set No. 1 in the example are shown in the table 3:
TABLE 31 # coking Tower set delayed coking Process Main parameters
The process parameters of the coking tower set No. 2 in the example are shown in the table 4:
TABLE 42 # coking Tower set delayed coking Process Main parameters
The indexes of the negative electrode materials of the respective batches in the examples are shown in Table 5
TABLE 5 Main indices of negative electrode materials
| Batches of | D50(μm) | d002(nm) | Specific charging capacity (mAh/g) | Efficiency (%) |
| 1 | 14.50 | 0.3361 | 372.8 | 95.49 |
| 2 | 16.20 | 0.3365 | 372.0 | 96.22 |
| 3 | 17.85 | 0.3359 | 374.8 | 96.58 |
The isotropic coke index of each batch in the examples is shown in Table 6
TABLE 6 main indices of Isotropic Coke
The above embodiments are implemented on the premise of the technical solution of the present invention, and are only preferred embodiments of the present invention, which are not intended to limit other forms of the present invention, and any skilled person familiar with the art can easily modify the technical solution of the present invention without departing from the technical solution of the present invention, and the equivalent changes and modifications can still belong to the protection scope of the present invention.
Claims (2)
1. The utility model provides a production device of isotropic burnt of cathode material coproduction, its characterized in that, includes melting jar, centrifuge, fractionating tower, 1# coking tower group, 2# coking tower group, rubbing crusher, 1# screening machine, 2# screening machine, retort, graphitizing furnace, melting jar connection centrifuge, centrifuge's heavy phase export is to 1# coking tower group pay-off, centrifuge's light phase exit linkage fractionating tower, fractionating tower heavy phase export is to 2# coking tower group pay-off, 2# coking tower group's solid phase export is to rubbing crusher pay-off, and the rubbing crusher is to 1# screening machine pay-off, and 1# screening machine is to the carbonizing furnace pay-off, and the graphitizing furnace is to the graphitizing furnace pay-off, and graphitizing furnace is to 2# screening machine pay-off.
2. The apparatus for co-producing isotropic coke from anode material as claimed in claim 1, wherein the # 1 coking tower group is composed of two coking towers; the 2# coking tower group consists of two coking towers.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020174605.3U CN211789274U (en) | 2020-02-17 | 2020-02-17 | Production device for co-production of anode material and isotropic coke |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020174605.3U CN211789274U (en) | 2020-02-17 | 2020-02-17 | Production device for co-production of anode material and isotropic coke |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN211789274U true CN211789274U (en) | 2020-10-27 |
Family
ID=72907850
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202020174605.3U Active CN211789274U (en) | 2020-02-17 | 2020-02-17 | Production device for co-production of anode material and isotropic coke |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN211789274U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111180726A (en) * | 2020-02-17 | 2020-05-19 | 中钢集团鞍山热能研究院有限公司 | Production process and device for co-producing isotropic coke by using negative electrode material |
-
2020
- 2020-02-17 CN CN202020174605.3U patent/CN211789274U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111180726A (en) * | 2020-02-17 | 2020-05-19 | 中钢集团鞍山热能研究院有限公司 | Production process and device for co-producing isotropic coke by using negative electrode material |
| CN111180726B (en) * | 2020-02-17 | 2024-02-06 | 中钢集团鞍山热能研究院有限公司 | Production process and device for co-producing isotropic coke by using anode material |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101294090B (en) | Fine purification method for coal tar pitch | |
| CN110437862B (en) | Preparation method of intermediate phase pitch coke, negative electrode material and lithium battery | |
| CN103614153B (en) | Preparation method of polycondensed asphalt, preparation method of needle coke and needle coke | |
| CN107694552A (en) | A kind of technique that coal-based needle coke is produced as raw material using middle coalite tar pitch | |
| CN111834634B (en) | High-performance artificial graphite negative electrode material and production process thereof | |
| CN103361096B (en) | Preparation method of high-softening-point asphalt for producing general-grade carbon fibers | |
| CN107892937A (en) | A kind of efficient solvent preparation method of refined bitumen | |
| CN115093874B (en) | Preparation method and system of low-quinoline insoluble high-softening-point petroleum-based coated asphalt | |
| CN108584904A (en) | A kind of method that by-product pitch cycle thermal polycondensation prepares mesocarbon microspheres | |
| CN211789274U (en) | Production device for co-production of anode material and isotropic coke | |
| CN109319758B (en) | Co-production process method of mesocarbon microbeads and negative electrode material coke | |
| CN109233888B (en) | Method for deep processing coal tar pitch | |
| CN106635102B (en) | Process for producing negative electrode material coke by using supercritical extraction oil slurry as raw material and application thereof | |
| CN104479707B (en) | A kind of method for preparing needle coke | |
| CN111180726B (en) | Production process and device for co-producing isotropic coke by using anode material | |
| CN114806620B (en) | Pretreatment process for preparing raw materials from coal-based needle coke | |
| CN109504415B (en) | Production method of needle coke | |
| CN109504416B (en) | Production process of coal-based needle coke | |
| CN109135789B (en) | Method for preparing needle coke from medium-low temperature coal tar | |
| CN214654660U (en) | Refined asphalt production device for efficiently separating quinoline insoluble substances from low-temperature asphalt | |
| CN109868146A (en) | A kind of medium temperature coal pitch environmental protection and efficiently utilize combined producing process method | |
| CN105645379A (en) | Asphalt hard carbon material, and preparation method and application thereof | |
| CN111171851A (en) | Production process and device of fast-charging negative electrode material | |
| CN110408418B (en) | Preparation method of high-regular-carbon microcrystalline pitch coke | |
| CN106753495A (en) | A kind of method of high temperature coal-tar/residual oil production carbosphere and dipping agent bitumen |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |