Process and apparatus for the production of a coating material from ethylene tar

Abstract

This invention discloses a processing technology and equipment for manufacturing coating materials from ethylene tar, relating to the field of carbon-based functional material preparation technology. The technology includes a raw material conveying system, a multi-stage light component extraction system, a three-stage series reactor, a finished product storage and transportation system, and a heat recovery system. The process utilizes a baffle structure within a two-stage distillation column to achieve thin-film flash evaporation for light component extraction, followed by stepped-up thermal polymerization in a series reactor heated by molten salt. This application employs a heat exchanger to recover the latent heat of the gaseous light components and the sensible heat of the finished product for dual preheating of the raw materials, significantly reducing the total system energy consumption. Simultaneously, a closed-loop feedback mechanism in the finished product tank allows substandard materials to continue to polymerize within the tank. This application can replace high-cost molecular distillation equipment, reducing investment costs while achieving stable production of coating materials with high softening point and high coking value, significantly improving production flexibility and yield.

Description

Technical Field

[0001] This invention relates to the field of carbon-based functional material preparation technology, specifically a processing technology and equipment for manufacturing coating materials from ethylene tar. Background Technology

[0002] Ethylene tar, a major byproduct of ethylene cracking, is rich in aromatic compounds such as styrene, indene, and naphthalene, as well as gums and asphaltenes. Due to its high carbon-to-hydrogen ratio, high aromaticity, and high viscosity, it has become an important raw material for preparing high-performance carbon-based functional materials such as lithium-ion battery coating materials and rubber fillers. In practical applications, the initial softening point of raw ethylene tar is typically low, generally below 80°C, and its coking value, i.e., carbonization residue, is insufficient, usually only around 30% to 40%, which greatly limits its widespread application in the field of high-performance carbon materials. To enhance its application value, the industry commonly uses heat treatment processes to promote the cross-linking, aromatization, and polycondensation reactions of macromolecules in ethylene tar, thereby increasing its softening point and coking value to meet the application requirements of high-value-added products. However, existing ethylene tar processing technologies and related equipment still face many challenges in actual production processes. On the one hand, the existing processes output a relatively limited variety of products, and the internal heat energy cannot be effectively recovered and recycled, resulting in high overall production energy consumption. On the other hand, further increasing output or improving product performance often requires the addition of expensive processing equipment such as short-path molecular distillers, which significantly increases equipment investment and production costs for enterprises. Furthermore, existing processing equipment has limitations in quality control and feedback regulation. When the granulated output fails quality inspection, there is a lack of flexible online processing mechanisms, which can easily lead to material waste or even production line shutdowns. Therefore, developing an ethylene tar processing technology and equipment that can achieve efficient heat energy utilization, simplify the process flow, reduce equipment costs, and stably improve coking value is of significant practical importance for promoting the development of carbon-based functional material preparation technology. Summary of the Invention

[0003] To address the aforementioned problems, specifically those raised in the background section, this invention provides a processing technology and equipment for manufacturing coating materials from ethylene tar. This invention utilizes a coupled structure of multi-stage continuous distillation and staged thermal polymerization, coupled with a dual waste heat recovery system and an online closed-loop feedback mechanism for the finished product. This achieves efficient conversion of ethylene tar into high-softening-point, high-coking-value lithium-ion battery coating materials without the need for additional molecular distillation equipment, and significantly reduces the overall system energy consumption.

[0004] This invention provides a processing equipment for manufacturing coating materials from ethylene tar, comprising a raw material conveying system, a multi-stage light extraction system, a multi-stage thermal polymerization system, a finished product storage and transportation system, and a heat recovery system. The raw material conveying system includes a raw material storage tank and a raw material conveying pump connected to the outlet of the storage tank. The multi-stage light extraction system includes a first distillation column and a second distillation column arranged in series. The output end of the raw material conveying pump passes through a pipeline sequentially through a first heat exchanger and a second heat exchanger, and is connected to the medium inlet of a first heater. The medium outlet of the first heater is connected to the upper-middle feed inlet of the first distillation column. The bottom outlet of the first distillation column is connected to the medium inlet of the second heater via the first conveying pump, and the medium outlet of the second heater is connected to the upper-middle feed inlet of the second distillation column. The internal structures of both the first and second distillation columns have been specifically optimized. Specifically, several sets of baffles are horizontally or staggeredly arranged in the upper region inside the columns of both columns. The baffle plate has a sawtooth or corrugated structure, which allows the liquid material entering from the feed inlet to form a large-area film-like flow along the surface of the baffle plate under the drive of gravity. This increases the contact area between the liquid material and the gas phase space inside the tower, and promotes the full flash removal of light components in the material within a shorter residence time.

[0005] Furthermore, the multi-stage thermal polymerization system includes a first reactor, a second reactor, and a third reactor connected in series. The bottom outlet of the second distillation column is connected to the inlet of the first reactor via a second transfer pump. Molten salt heating tubes are installed inside the first, second, and third reactors. These molten salt heating tubes are connected to a molten salt circulation system, utilizing high-temperature molten salt as the heat exchange medium. Specifically, the molten salt heating tubes are not perfectly horizontal inside the reactors, but rather have a downward slope of 1° to 5° relative to the horizontal plane, with the lowest point of the slope connected to the return pipe of the molten salt circulation system. This slope design utilizes gravity to allow the molten salt to automatically flow to the return pipe after the system stops operating or after heat exchange and cooling, avoiding the risk of blockage caused by molten salt solidification in the pipes and ensuring convenient equipment maintenance.

[0006] The heat recovery system is implemented through a gas phase recovery path and a liquid phase recovery path. The gas phase outlets at the top of both the first and second distillation columns are connected to the second light component removal assembly. The second light component removal assembly includes a gas phase delivery pipeline that passes through the heat source side of the first heat exchanger, allowing indirect heat exchange between the high-temperature light component vapor from the distillation column and the low-temperature feedstock from the feedstock delivery pump, achieving preliminary preheating of the feedstock. The finished product storage and transportation system includes a finished product tank and a granulator delivery pump connected to the outlet of the finished product tank. The inlet of the finished product tank is connected to the outlet of the third reactor. The finished product tank is equipped with a finished product heat exchange coil. The inlet of the finished product heat exchange coil is connected to the pipeline after the feedstock passes through the first heat exchanger, and the outlet of the finished product heat exchange coil is connected to the inlet of the second heater. This configuration utilizes the sensible heat of the high-temperature finished product in the finished product tank to perform secondary preheating of the feedstock, further reducing the heat load on the first and second heaters.

[0007] Furthermore, the finished product storage and transportation system also features online quality control. The finished product tank is connected to the granulator via a granulator delivery pump. An online detection device is installed at the feed or discharge end of the granulator to monitor the softening point and coking value of the coating material. The granulator delivery pump is linked to the control system. When the product indicators reported by the online detection device do not reach a preset threshold, the control system closes the valve leading to the granulator and activates the circulating stirring mechanism inside the finished product tank. At this time, the finished product tank utilizes the heat from the continuously supplied high-temperature material from the third reactor to maintain a thermal polymerization reaction environment within the tank, allowing the substandard material to continue undergoing condensation polymerization until the indicators meet the requirements before restarting the granulation process. This closed-loop control mechanism avoids the production of substandard products and improves the overall yield of the production line.

[0008] The present invention also provides a processing technology for manufacturing coating materials from ethylene tar based on the above-mentioned equipment, the specific steps of which are as follows: S1: Initial Lightening Stage. The raw material, ethylene tar, is pumped out and sequentially passes through the first heat exchanger for heat exchange with the high-temperature gaseous light components, and then through the finished product heat exchange coil in the finished product tank for heat exchange with the high-temperature finished product. The preheated raw material enters the first heater. The first heater uses 300℃-320℃ heat transfer oil as a heat source to heat the raw material to 240℃-260℃. The heated material enters the first distillation column, where it flows along the baffles and remains for 160-200 minutes. During this process, low-boiling-point light components are removed, increasing the softening point from the original 40℃-70℃ to 90℃-110℃, and the coking value from approximately 20% to 23%-27%. The light components removed at the top of the column enter the second light-removal component and are refluxed back to the first heat exchanger to provide heat energy for the raw material.

[0009] S2: Secondary Lightening Stage. After the initial lightening, the heavy components are pumped into the second heater by the first transfer pump. The second heater also uses 300℃-320℃ heat transfer oil as a heat source to further heat the material to 280℃-300℃. The material then enters the second distillation column, where it undergoes another thin-film evaporation through the distribution of baffles within the column, with a residence time controlled at 160-200 minutes. In the second distillation column, the remaining medium-boiling-point components are further separated, increasing the softening point of the material to 115℃-125℃ and the coking value to 28%-32%.

[0010] S3: Staged Thermal Polymerization. After two stages of lightening, the material is pumped into the multi-stage thermal polymerization system by a second conveying pump. The material flows sequentially through the first, second, and third reactors connected in series. In the first reactor, the material temperature is maintained at 310℃-330℃ using molten salt heating pipes for preliminary thermal polymerization, shifting the molecular weight distribution towards the higher molecular weight range. The softening point of the outlet material reaches 125℃-135℃, and the coking value reaches 38%-42%. Subsequently, the material enters the second reactor, where the temperature is maintained at 330℃-350℃, further promoting the condensation and cross-linking of aromatic molecules. The softening point of the outlet material reaches 5℃-155℃, and the coking value reaches 43%-47%. Finally, the material enters the third reactor, where the temperature is maintained at 350℃-370℃, completing the final deep thermal polymerization. The softening point of the outlet material reaches 165℃-175℃, and the coking value increases to 48%-52%. Throughout the thermal polymerization process, the gaseous components generated in the reactor are condensed and recovered through the first light-removal component.

[0011] S4: Finished Product Storage, Transportation, and Index Feedback Control Stage. The high-temperature finished product output from the third reactor enters the finished product tank for temporary storage. Heat within the tank is transferred to the raw materials to be processed via the finished product heat exchange coil. The material is then pumped to the granulator for finished product forming. During granulation, the softening point and coking value of the product are acquired in real-time using an online detector. If the detected product index is lower than the set standard, the control system immediately switches valves to retain the material at a temperature above 300°C via a baffle plate, allowing the material to continue the thermal polymerization reaction within the finished product tank. This extended residence time in the finished product tank achieves a remedial improvement in the index until the online detection data is satisfactory, at which point the normal granulation process resumes.

[0012] The beneficial effects of this invention are reflected in the following aspects: First, this invention replaces the high-cost short-range molecular evaporator in traditional processes with a combination of a two-stage baffle plate distillation column and a three-stage molten salt reactor. Utilizing the thin-film evaporation effect formed by the baffles, deep removal of light components is achieved under normal or slightly negative pressure conditions. Combined with a three-stage stepped heating thermal polymerization reaction, the material undergoes a continuous and controlled polycondensation reaction during heating, successfully increasing the coking value of ethylene tar from less than 40% to over 50%, and raising the softening point to approximately 170°C. This significantly enhances the product's applicability in lithium battery coating materials while substantially reducing fixed asset investment in equipment.

[0013] Secondly, this invention constructs a complete energy cascade utilization system. By setting up a first heat exchanger to recover the latent heat of condensation of the light components in the gas phase at the top of the tower, and setting up a finished product heat exchange coil to recover the sensible heat of the finished product, dual preheating of the raw materials is achieved. This design ensures that the raw materials have a high initial temperature before entering the first heater, reducing consumption and shortening the time required for the materials to heat up to the reaction temperature. Overall production energy consumption is reduced by more than 20% compared to traditional processes.

[0014] Furthermore, this invention possesses extremely high quality control stability. The finished product tank is no longer merely a storage and transportation transit facility, but is transformed into an auxiliary reactor with an "online repair" function through linkage with the granulator and control system. When fluctuations in the upstream process cause instantaneous product indicators to fail to meet standards, the system corrects the indicators without shutting down through internal circulation and re-reaction mechanisms, greatly improving the continuous operation capability and material utilization rate of the production line, and avoiding material downgrading or scrapping due to quality issues.

[0015] Finally, the structural design of this invention fully considers the reliability of industrial operation. The inclined slope design of the molten salt heating tubes inside the reactor solves the industry problem of easy condensation and blockage of high-melting-point heat transfer media during shutdown. Compared with single-stage large-capacity reactors, the multi-stage series reactor design can more accurately control the residence time distribution of materials, avoid the "short-circuit" or "over-reaction" phenomenon of materials, and ensure the uniformity of molecular weight distribution of the produced coating material.

[0016] In summary, this invention, through specific equipment structure innovation and process optimization, achieves high-value utilization of ethylene tar, possessing significant advantages such as low process cost, high energy efficiency, and stable product quality. It provides a practical and feasible technical solution for the large-scale production of high-performance carbon-based functional materials. Those skilled in the art will understand that the above descriptions of the connection relationships of various components, temperature ranges, residence times, and structural parameters are all specific designs made to achieve the aforementioned technical effects, possessing strong operability and industrial application value. Attached Figure Description

[0017] Figure 1This is a schematic diagram of the overall process route of the present invention.

[0018] Reference numerals: 1. Raw material transfer pump; 2. Heat exchanger; 3. Finished product tank; 4. Granulator transfer pump; 5. First heater; 6. First distillation column; 7. First transfer pump; 8. Second heater; 9. Second distillation column; 10. Second transfer pump; 11. Reactor assembly; 12. First light component removal assembly; 13. Second light component removal assembly. Detailed Implementation

[0019] The following is a reference to the appendix. Figure 1 The preferred embodiments of this invention are described below. Those skilled in the art should understand that these embodiments are merely for explaining the technical principles of this invention and are not intended to limit the scope of protection of this invention.

[0020] This equipment system constitutes a closed-loop, complete production line with cascaded thermal energy utilization capabilities. The equipment mainly includes a raw material transfer pump 1, a heat exchanger 2, a finished product tank 3, a granulator transfer pump 4, a first heater 5, a first distillation column 6, a first transfer pump 7, a second heater 8, a second distillation column 9, a second transfer pump 10, a reaction vessel assembly 11, a first light-light waste removal assembly 12, a second light-light waste removal assembly 13, and baffles installed inside the distillation columns. All components are connected via high-temperature and corrosion-resistant industrial pipelines and are equipped with corresponding pressure sensors, temperature sensors, and flow control valves to ensure precise control of the entire process.

[0021] The raw material transfer pump 1, serving as the power source for the entire system, is connected at its inlet to the raw material storage tank. It pumps raw ethylene tar material, with an initial temperature of approximately 60°C, a softening point close to 0°C, and a coking value of approximately 0%, into the processing system. The output pipeline of the raw material transfer pump 1 is first connected to heat exchangers 2. In this embodiment, there are two heat exchangers 2, each undertaking a different heat exchange task. The first set of heat exchangers 2 utilizes the light vapor components from the top of the first distillation column 6 and the second distillation column 9 as a heat source. Through a shell-and-tube heat exchange structure, the high-temperature vapor components flow in the tube side, while the low-temperature raw material flows in the shell side, thus achieving initial heating of the raw material. The second set of heat exchangers 2 is connected to the finished product tank 3, utilizing the sensible heat of the high-temperature finished product within the tank 3 to preheat the raw material. This multi-stage heat exchange design ensures that the temperature of the raw material is raised to between 150°C and 180°C before entering subsequent heating stages, significantly reducing external energy consumption.

[0022] The preheated feedstock enters the first heater 5. The first heater 5 is filled with heat transfer oil, which is heated to 300°C to 320°C by an external oil furnace and circulates. Inside the first heater 5, the feedstock undergoes thorough heat exchange with the heat transfer oil through a spiral tube bundle, raising its temperature to approximately 250°C. At this point, the material is fed into the first distillation column 6. The upper interior of the first distillation column 6 is equipped with several sets of staggered baffles. When the 250°C feedstock is sprayed down from the top inlet, it impacts the baffles and forms a very thin liquid film along the surface. Because the baffles increase the spreadable area of ​​the material, the lighter components in the material are more easily able to overcome surface tension and flash evaporate during their residence in the column. This thin-film evaporation effect enables efficient separation of low-boiling-point components even under normal pressure.

[0023] After the initial lightening process in the first distillation column 6, the heavy components accumulate at the bottom of the column and are then fed into the second heater 8 via the first transfer pump 7. The second heater 8 also uses 300°C heat transfer oil as a heat source to further heat the lightened material to approximately 290°C. The heated material then enters the second distillation column 9. The internal structure of the second distillation column 9 is similar to that of the first distillation column 6, also relying on baffles to ensure the material flows and spreads sufficiently. In the second distillation column 9, the material undergoes a second lightening process, further removing residual medium-boiling-point components. At this point, the softening point of the material increases to 120°C, and the coking value reaches approximately 30%. The gaseous light components extracted from the first distillation column 6 and the second distillation column 9 are collected through pipelines and enter the second light-removal assembly 13. After releasing heat through the heat exchanger 2, they enter the by-product collection column for condensation and recovery. These by-products can be further utilized as industrial fuel oil or chemical raw materials.

[0024] The recombinant material after secondary lightening is fed into reactor assembly 11 by the second transfer pump 10. Reactor assembly 11 consists of three reactors connected in series: a first reactor, a second reactor, and a third reactor. All three reactors use molten salt as the heating medium. The molten salt is a mixture of salts such as potassium nitrate and sodium nitrate, possessing extremely high thermal stability and heat transfer efficiency. Inside the reactors, molten salt heating tubes are inserted into the material. To address the problem of molten salt easily remaining and solidifying in the pipelines during industrial production, this invention specifically sets the heating tubes inside the reactors with a downward slope of 1 to 5 degrees. This slope design utilizes gravity to ensure that when the system stops or during heat exchange and cooling, the molten salt in the tubes can automatically flow back to the molten salt storage tank along the slope, thus eliminating the risk of heating tube blockage.

[0025] The material undergoes a continuous thermal polymerization reaction in reactor assembly 11. In the first reactor, the material undergoes a preliminary condensation reaction at a high temperature of approximately 320°C, raising the softening point to 130°C and the coking value to 40%. Subsequently, the material overflows into the second reactor, where, with the extension of reaction time and the increase of molecular weight, the softening point further increases to 150°C, and the coking value reaches 45%. Finally, the material enters the third reactor to complete a deep thermal polymerization reaction, ultimately producing a material with a softening point of 170°C and a stable coking value of approximately 50%. Trace gaseous components generated during the entire thermal polymerization process are collected and treated by the first light-removal assembly 12.

[0026] The high-temperature finished product output from the third reactor enters the finished product tank 3. Finished product tank 3 not only serves as an intermediate storage tank but also as an energy recovery center. Before entering the first heater 5, the raw materials pass through the heat exchange coils inside finished product tank 3, where the heat from the finished product forces heat exchange onto the raw materials. Finished product tank 3 also has a quality feedback adjustment function. The material is sent to different granulators for molding via granulator conveying pump 4. An online detection branch is installed on the outlet pipe of granulator conveying pump 4 to monitor the softening point and coking value of the product in real time. Once a batch of products is found to be substandard, the control system immediately issues a command to stop granulator conveying pump 4 from feeding the granulators and to open the circulation loop between finished product tank 3 and reactor assembly 11. At this time, the substandard product continues to undergo thermal polymerization in finished product tank 3 using the high-temperature sensible heat from the newly produced material in reactor assembly 11. By extending the reaction time, the product indicators are corrected until they pass the test, and then the granulation process resumes. This design achieves online repair of defective products by increasing the residence time, avoiding energy waste caused by material rework.

[0027] The present invention provides a processing technology for manufacturing coating materials from ethylene tar, which specifically follows the steps S1 to S4.

[0028] S1: Initial Lightening Step. Ethylene tar feedstock with an initial temperature of 60°C, a softening point of 0°C, and a coking value of 0% is fed into the system via feedstock pump 1. The feedstock first undergoes indirect heat exchange in heat exchanger 2 with the vapor phase from the top of the distillation column and the high-temperature finished product in the finished product tank 3. The preheated feedstock then enters the first heater 5. In the first heater 5, the feedstock is heated to 250°C using 300°C heat transfer oil. Subsequently, the heated feedstock enters the first distillation column 6. The material flows downwards along the surface of the baffles inside the column, forming a thin film distribution, allowing the light components to fully evaporate within a 3-hour residence time. After this step, the softening point of the material increases to 100°C, and the coking value reaches 25%.

[0029] S2: Secondary Lightening Step. The heavy components, after the initial lightening, are drawn from the bottom of the first distillation column 6 by the first transfer pump 7 and fed into the second heater 8. The material temperature is raised to 290°C through secondary heating with heat transfer oil within the second heater 8. Subsequently, the material enters the second distillation column 9. Inside the second distillation column 9, the material undergoes secondary thin-film evaporation again through the action of baffles, with a residence time also set to 3 hours. During this process, medium-boiling-point components are further removed, increasing the softening point of the material from 100°C to 120°C and the coking value from 25% to 30%.

[0030] S3: Staged thermal polymerization step. The heavy component material after secondary lightening is fed into reactor assembly 11 via the second transfer pump 10. The material flows sequentially through three reactors connected in series. In the first reactor, the material begins to undergo aromatization and condensation reactions at high temperature, with the softening point rising to 130°C and the coking value reaching 40%. In the second reactor, as the reaction progresses, the material's softening point reaches 150°C, and the coking value reaches 45%. In the third reactor, the material completes the final thermal polymerization reaction, with the softening point reaching 170°C and the coking value reaching 50%. Throughout the process, the gaseous components generated in the reactors are recovered through the first lightening component assembly 12.

[0031] S4: Finished Product Forming and Feedback Adjustment Steps. The high-temperature finished product after thermal polymerization enters the finished product tank 3. Heat within the finished product tank 3 is transferred to the raw materials to be processed via heat exchanger 2. Subsequently, the material is sent to the granulator by granulator delivery pump 4 for flake formation or granulation. During the granulation process, if online monitoring detects that the product quality is substandard, granulator delivery pump 4 immediately stops conveying the material. The material continues the thermal polymerization reaction within the finished product tank 3 through continuous heating and mixing with fresh material from the reactor assembly 11, until all indicators meet the requirements of lithium battery coating materials, at which point the granulation process is restarted.

[0032] The operating principle of this process and equipment in practical applications is as follows. Ethylene tar is an extremely complex cracking byproduct with a very wide molecular weight distribution. Traditional single-stage distillation processes often struggle to achieve high coking values ​​while maintaining a high softening point. This invention uses two stages, S1 and S2, to lighten the tar, utilizing a large evaporation surface created by baffles to achieve deep removal of light and medium components at relatively low temperatures. This lays a high-purity foundation for subsequent thermal polymerization reactions.

[0033] In the S3 step of thermal polymerization, this invention employs a three-reactor series gradient heating mode. This design simulates the characteristics of a plug flow reactor, effectively avoiding the "back-mixing" phenomenon that easily occurs in single-reactor reactions, resulting in a more uniform molecular weight distribution of the produced coating material. Since the quality of the coating material largely depends on the regularity of its molecular structure, a uniform molecular weight distribution can significantly improve its coating performance on the surface of the negative electrode material. Simultaneously, using molten salt as a heat source solves the problem of coking failure of heat transfer oil above 300℃, enabling the reactor to operate stably for a long time at high temperatures of 350℃ to 370℃, thereby ensuring a high coking value of over 50%.

[0034] In terms of energy balance, this system achieves a closed-loop circulation of thermal energy through heat exchanger 2. The gaseous components produced at the top of the distillation column carry a large amount of latent heat, while the finished product from the reactor carries a large amount of sensible heat. By transferring these two portions of heat back to the raw materials, the system reduces its dependence on external energy by more than 30% while maintaining a high-temperature reaction environment. This cascaded utilization is not only for energy conservation but, more importantly, reduces the thermal stress of the material entering the heater through preheating, thus extending the service life of the heating pipeline.

[0035] Furthermore, the "auxiliary reactor" design of the finished product tank 3 is the core solution of this invention to address fluctuations in industrial production. In actual production, the composition of the raw material ethylene tar often fluctuates with changes in the operating conditions of the upstream cracking furnace, which can lead to occasional deviations in the finished product indicators under fixed process parameters. This invention, through online detection and reheating mechanisms within the finished product tank in step S4, endows the production line with extremely strong flexible control capabilities. When the material indicators produced upstream are low, the system automatically switches to internal circulation mode, utilizing the large-capacity buffering effect of the finished product tank 3 and the continuous high-temperature heat output from the reactor assembly 11 to complete the "make-up" reaction within the tank. This solution, which corrects indicators without shutting down the machine, greatly improves the equipment uptime and the consistency of the finished product.

[0036] In summary, this invention successfully solves the technical challenges of high energy consumption, unstable product indicators, and easy equipment blockage in ethylene tar processing by deeply coupling two-stage baffle distillation and three-stage molten salt thermal polymerization, combined with dual waste heat recovery and online quality recovery mechanisms. The equipment has a compact structure and a reasonable process, enabling the continuous and stable production of high-quality carbon-based materials that meet the requirements of high-performance lithium battery anode coating, and possesses extremely high industrial application value. Those skilled in the art should understand that conventional parameter adjustments to reaction temperature, residence time, or the specific inclination angle of the baffles, without departing from the core design concept of this invention, should be included within the scope of protection of this invention.

[0037] Although the present invention has been described with reference to preferred embodiments, various modifications can be made and components can be replaced with equivalents without departing from the scope of the present invention. In particular, the technical features mentioned in the various embodiments can be combined in any manner, provided there is no structural conflict. The present invention is not limited to the specific embodiments disclosed herein, but includes all technical solutions falling within the scope of the claims.

[0038] In the description of this invention patent, terms such as "center," "upper," "lower," "left," "right," "vertical," "horizontal," "inner," and "outer," which indicate direction or positional relationships, are based on the direction or positional relationships shown in the accompanying drawings. These are used merely for ease of description and do not indicate or imply that the device or element must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this invention patent. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and should not be construed as indicating or implying relative importance.

[0039] Furthermore, it should be noted that, in the description of this invention patent, unless otherwise explicitly specified and limited, the terms "installation," "connection," and "linking" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this invention patent according to the specific circumstances.

[0040] The term "comprising" or any other similar term is intended to cover non-exclusive inclusion, such that a process, article, or apparatus / device that comprises a list of elements includes not only those elements but also other elements not expressly listed, or elements inherent to those processes, articles, or apparatus / devices.

[0041] The technical solution of this invention has been described above with reference to the preferred embodiments shown in the accompanying drawings. However, it will be readily understood by those skilled in the art that the scope of protection of this invention is obviously not limited to these specific embodiments. Without departing from the principles of this invention, those skilled in the art can make equivalent changes or substitutions to the relevant technical features, and the technical solutions resulting from these changes or substitutions will all fall within the scope of protection of this invention.

Claims

1. A processing device for manufacturing coating materials from ethylene tar, characterized in that, The system includes a raw material transfer pump (1), a heat exchanger (2), a first heater (5), a first distillation column (6), a first transfer pump (7), a second heater (8), a second distillation column (9), a second transfer pump (10), a reactor assembly (11), and a finished product tank (3). The output end of the raw material transfer pump (1) passes through the heat source side of the heat exchanger (2) via a pipeline and is connected to the medium inlet of the first heater (5). The medium outlet of the first heater (5) is connected to the upper middle feed inlet of the first distillation column (6). The bottom outlet of (6) is connected to the medium inlet of the second heater (8) through the first delivery pump (7), and the medium outlet of the second heater (8) is connected to the upper middle feed inlet of the second distillation column (9); the bottom outlet of the second distillation column (9) is connected to the feed inlet of the reactor assembly (11) through the second delivery pump (10), and the outlet of the reactor assembly (11) is connected to the finished product tank (3); the interior of the first distillation column (6) and the second distillation column (9) is provided with several sets of baffles.

2. The processing equipment for manufacturing coating materials from ethylene tar as described in claim 1, characterized in that, The baffle plate has a wave-like structure.

3. The processing equipment for manufacturing coating materials from ethylene tar as described in claim 2, characterized in that, The first distillation column (6) and the second distillation column (9) have several sets of baffles arranged in an alternating manner inside the column cavity, so that the liquid material forms a thin film flow field along the surface of the baffles under the drive of gravity.

4. The processing equipment for manufacturing coating materials from ethylene tar as described in claim 1, characterized in that, The reactor assembly (11) includes a first reactor, a second reactor, and a third reactor connected in series. The first reactor, the second reactor, and the third reactor are all equipped with molten salt heating tubes for circulating high-temperature molten salt. The molten salt heating tubes are inclined downward at a slope of 1° to 5° relative to the horizontal plane, and the lowest point of the inclined slope is connected to the return pipeline of the molten salt circulation system.

5. The processing equipment for manufacturing coating materials from ethylene tar as described in claim 1, characterized in that, It also includes a second light removal component (13), the top gas phase outlets of the first distillation column (6) and the second distillation column (9) are both connected to the second light removal component (13), and the gas phase delivery pipeline of the second light removal component (13) passes through the heat source side of the heat exchanger (2).

6. The processing equipment for manufacturing coating materials from ethylene tar as described in claim 5, characterized in that, The finished product tank (3) is equipped with a finished product heat exchange coil. The inlet of the finished product heat exchange coil is connected to the raw material pipeline after passing through the heat exchanger (2), and the outlet of the finished product heat exchange coil is connected to the inlet of the second heater (8).

7. The processing equipment for manufacturing coating materials from ethylene tar as described in claim 1, characterized in that, It also includes a granulator conveying pump (4) and an online detection device. The finished product tank (3) is connected to the granulator through the granulator conveying pump (4). The online detection device is installed on the outlet pipeline of the granulator conveying pump (4). The finished product tank (3) is equipped with a circulating stirring mechanism. The control system controls the opening and closing of the valve leading to the granulator and the circulation loop of the finished product tank (3) according to the product index signal fed back by the online detection device.

8. A processing method for manufacturing coating materials from ethylene tar based on the equipment described in any one of claims 1 to 7, characterized in that, Includes the following steps: S1: The raw material ethylene tar is sent out by the raw material conveying pump (1), and after being preheated by the heat exchanger (2) and the finished product heat exchange coil in the finished product tank (3), it enters the first heater (5), and after being heated to 240°C to 260°C, it enters the first distillation column (6). The material flows along the baffle plate in the column and stays for 160 min to 200 min. S2: The heavy component material after initial lightening is sent to the second heater (8) by the first transfer pump (7), heated to 280°C to 300°C and then enters the second distillation column (9). The material flows along the baffle plate in the column and stays for 160 min to 200 min. S3: The material after two-stage lifting is fed into the reactor assembly (11) by the second conveying pump (10). The material flows through the first reactor, the second reactor and the third reactor in series. The material temperature in the first reactor is maintained at 310°C to 330°C, the material temperature in the second reactor is maintained at 330°C to 350°C, and the material temperature in the third reactor is maintained at 350°C to 370°C.

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