A device and method for continuously producing a lithium ion battery negative electrode coated with pitch

Abstract

The present application relates to the field of graphite negative electrode material, specifically to a device and method for continuous production of lithium ion battery negative electrode coated pitch, four reaction kettles are divided into upper and lower two layers and arranged symmetrically, the liquid phase product lines of the two reaction kettles arranged in the upper layer are connected in series with the liquid phase raw material lines of the reaction kettles arranged directly below, to form two completely same reaction units, the two reaction units are connected in parallel for switching operation, so that the continuous production of lithium ion battery negative electrode coated pitch can be realized. Further, by using the designed device, through the combined process of oxidation crosslinking first and nitrogen stripping later, the softening point and quinoline insoluble content of the negative electrode coated pitch can be flexibly controlled, and the quality stability of the negative electrode coated pitch is improved.

Description

Technical Field

[0001] This invention relates to the field of graphite anode materials, specifically to an apparatus and method for the continuous production of lithium-ion battery anodes coated with asphalt. Background Technology

[0002] Lithium-ion batteries are currently the portable chemical power source with the highest specific energy. They have advantages such as high operating voltage, excellent safety performance, long cycle life, good low-temperature performance, no memory effect, and no pollution. They are the fastest-growing battery type in the fields of electric vehicles and chemical energy storage.

[0003] Graphite materials are currently the preferred anode materials for lithium-ion batteries, possessing advantages such as high specific capacity, good cycle performance, low lithium intercalation / deintercalation plateau, and low cost. However, graphite materials have poor compatibility with organic solvent electrolytes, and during charge and discharge, lithium-ion solvation co-intercalation reactions easily occur, causing the graphite layer to dissociate or even peel off, resulting in low charge / discharge efficiency and unsatisfactory cycle performance. Chinese patent applications CN201810402456.9 and CN202011312113.7 modify graphite materials by coating them with pitch, coating their surface with a layer of amorphous carbon with a core-shell structure. This retains the advantages of graphite materials such as high capacity and low voltage plateau, while also possessing the advantages of amorphous carbon materials such as good compatibility with electrolyte solvents, high capacity, and good rate performance, thereby improving the cycle performance, rate performance, specific capacity, and lifespan of lithium-ion batteries. The heavy fraction of ethylene tar above 300℃ accounts for about 40%, mainly composed of 3-6 ring polycyclic aromatic hydrocarbons. It has high carbon content, compact molecular structure, low impurity content, and good reactivity, making it an ideal raw material for preparing anode-coated pitch with high softening point, high toluene insoluble content, high coking value, and low quinoline insoluble content.

[0004] Chinese patent application CN111628146A discloses a process for preparing lithium-ion battery anode materials using pitch-filled microcrystalline graphite. Specifically, it involves using microcrystalline graphite as raw material, first modifying it with low-temperature coal tar, and then mixing it with liquid medium-temperature pitch to prepare anode sheets with low rebound performance and long cycle life. However, the closed pores generated by the pitch coating may affect the stability of the anode material. Generally, the higher the softening point of the pitch used for coating lithium-ion battery anodes, the higher the carbon yield after carbonization, and the better the coating effect. Currently, commonly used methods for preparing coated pitch mainly include oxidation, thermal polycondensation, vacuum distillation, and combinations thereof. Oxidation and thermal polycondensation are advantageous for producing coated pitch with high softening points and high target product yields, but they have two main drawbacks: first, the production process is intermittent, resulting in low capacity and unstable product quality; second, the reaction process generates a small amount of highly adhesive components that easily adhere to the inner wall of the reactor and the stirring equipment, requiring manual cleaning after cooling and embrittlement, increasing labor intensity and further reducing production efficiency. Although vacuum distillation (including negative pressure flash distillation) can achieve continuous production, this process is a purely physical process and lacks the necessary cross-linking and condensation reactions. Therefore, the softening point and yield of the product are both low, making it difficult to meet the downstream users' demand for high softening point coated asphalt. Summary of the Invention

[0005] To address the problems existing in the background technology, the present invention provides an apparatus and method for continuous production of lithium-ion battery negative electrode coated with asphalt, which can realize continuous production of high softening point lithium-ion battery negative electrode coated with asphalt, reduce labor intensity, shorten process time, improve production efficiency, and stabilize product quality.

[0006] This invention provides an apparatus for the continuous production of lithium-ion battery negative electrode coated asphalt, comprising at least four high-pressure reactors (RA, RB, RC, and RD) with temperature control functions. The first high-pressure reactor (RA) is equipped with a first pressure detection component (PA) and a first temperature monitoring component (TA); the second high-pressure reactor (RB) is equipped with a second pressure detection component (PB) and a second temperature monitoring component (TB); the third high-pressure reactor (RC) is equipped with a third pressure detection component (PC) and a third temperature monitoring component (TC); and the fourth high-pressure reactor (RD) is equipped with… A fourth pressure detection unit (PD) and a fourth temperature monitoring unit (TD) are provided; a first liquid-phase feed line (L2A), a first gaseous product line (L4A), and a first drying exhaust gas line (L5A) are provided on the upper cover of the first high-pressure reactor (RA); a second liquid-phase feed line (L2B), a second gaseous product line (L4B), and a second drying exhaust gas line (L5B) are provided on the upper cover of the second high-pressure reactor (RB); a third liquid-phase feed line (L2C), a third gaseous product line (L4C), and a third drying exhaust gas line (L5C) are provided on the upper cover of the third high-pressure reactor (RC); and a fourth liquid-phase feed line (L2A) is provided on the upper cover of the fourth high-pressure reactor (RD). The reactor comprises a first gas production line (L2D), a fourth gaseous product line (L4D), and a fourth drying exhaust gas line (L5D). The first to fourth gaseous product lines are all connected to the inlet of the gaseous product heat exchanger (HE2), and the first to fourth drying exhaust gas lines are all connected to the inlet of the drying exhaust gas heat exchanger (HE1). A first gas distributor (DA) is located at the bottom of the inner cavity of the first high-pressure reactor (RA), a second gas distributor (DB) is located at the bottom of the inner cavity of the second high-pressure reactor (RB), a third gas distributor (DC) is located at the bottom of the inner cavity of the third high-pressure reactor (RC), and a fourth gas distributor (D) is located at the bottom of the inner cavity of the fourth high-pressure reactor (RD). D); wherein the first gas distributor (DA) arranged in the first high-pressure reactor (RA) in the upper layer is connected to the first air feed line (L7A) and the total nitrogen stripping line (L9); the second gas distributor (DB) arranged in the second high-pressure reactor (RB) in the upper layer is connected to the second air feed line (L7B) and the total nitrogen stripping line (L9); the third gas distributor (DC) arranged in the third high-pressure reactor (RC) in the lower layer is only connected to the third nitrogen stripping line (L7C); and the fourth gas distributor (DD) arranged in the fourth high-pressure reactor (RD) in the lower layer is only connected to the fourth nitrogen stripping line (L7D).The bottom cover of the third high-pressure reactor (RC) is equipped with a third liquid product line (L6C), and the bottom cover of the fourth high-pressure reactor (RD) is equipped with a fourth liquid product line (L6D). Both the third liquid product line (L6C) and the fourth liquid product line (L6D) are connected to the asphalt coating product line (PC).

[0007] As a preferred technical solution, the first high-pressure reactor (RA), the second high-pressure reactor (RB), the third high-pressure reactor (RC), and the fourth high-pressure reactor (RD) are arranged in two layers, with the first high-pressure reactor (RA) and the second high-pressure reactor (RB) arranged on the upper layer, and the third high-pressure reactor (RC) and the fourth high-pressure reactor (RD) arranged directly below the first high-pressure reactor (RA) and the second high-pressure reactor (RB). The first liquid phase product line (L6A) on the bottom cover of the first high-pressure reactor (RA) and the third liquid phase raw material line (L2C) on the top cover of the third high-pressure reactor (RC) are connected in series to form a first reaction unit. The second liquid phase product line (L6B) on the bottom cover of the second high-pressure reactor (RB) and the fourth liquid phase raw material line (L2D) on the top cover of the fourth high-pressure reactor (RD) are connected in series to form a second reaction unit. The first reaction unit and the second reaction unit are connected in parallel. The above design constitutes the core of the continuous production device for coating asphalt with lithium-ion battery negative electrodes according to the present invention.

[0008] As a preferred technical solution, the first liquid phase product line (L6A) on the bottom cover of the first high-pressure reactor (RA) is connected to the fourth liquid phase feed line (L2D) on the top cover of the fourth high-pressure reactor (RD); the second liquid phase product line (L6B) on the bottom cover of the second high-pressure reactor (RB) is connected to the third liquid phase feed line (L2C) on the top cover of the third high-pressure reactor (RC).

[0009] As a preferred technical solution, the upper part of the inner cavity of the first high-pressure reactor (RA) is provided with a first high-pressure water cleaner (FNA) that can move up and down and rotate; the upper part of the inner cavity of the second high-pressure reactor (RB) is provided with a second high-pressure water cleaner (FNB) that can move up and down and rotate; the upper part of the inner cavity of the third high-pressure reactor (RC) is provided with a third high-pressure water cleaner (FNC) that can move up and down and rotate; and the upper part of the inner cavity of the fourth high-pressure reactor (RD) is provided with a fourth high-pressure water cleaner (FND) that can move up and down and rotate. The first high-pressure water cleaner (FNA) is located in the first high-pressure reactor (RA). One end of the first high-pressure cleaning water line (L1A) on the top cover is connected; the second high-pressure water cleaner (FNB) is connected to one end of the second high-pressure cleaning water line (L1B) on the top cover of the second high-pressure reactor (RB); the third high-pressure water cleaner (FNC) is connected to one end of the third high-pressure cleaning water line (L1C) on the top cover of the third high-pressure reactor (RC); and the fourth high-pressure water cleaner (FND) is connected to one end of the fourth high-pressure cleaning water line (L1D) on the top cover of the fourth high-pressure reactor (RD). The other ends of the first to fourth high-pressure cleaning water lines are all connected to the high-pressure cleaning water main pipe (FW).

[0010] As a preferred technical solution, the top cover of the first high-pressure reactor (RA) is provided with a first pressurized nitrogen line (L3A), the top cover of the second high-pressure reactor (RB) is provided with a second pressurized nitrogen line (L3B), the top cover of the third high-pressure reactor (RC) is provided with a third pressurized nitrogen line (L3C), and the top cover of the fourth high-pressure reactor (RD) is provided with a fourth pressurized nitrogen line (L3D); the first to fourth pressurized nitrogen lines are all connected to the pressurized nitrogen main pipe (NP).

[0011] As a preferred technical solution, the bottom cover of the first high-pressure reactor (RA) is provided with a first cleaning wastewater line (L8A), the bottom cover of the second high-pressure reactor (RB) is provided with a second cleaning wastewater line (L8B), the bottom cover of the third high-pressure reactor (RC) is provided with a third cleaning wastewater line (L8C), and the bottom cover of the fourth high-pressure reactor (RD) is provided with a fourth cleaning wastewater line (L8D); the first to fourth cleaning wastewater lines are all connected to the main cleaning wastewater pipe (SW).

[0012] Another aspect of the present invention provides a method for continuously producing lithium-ion battery negative electrode coated asphalt, which is implemented by the apparatus for continuously producing lithium-ion battery negative electrode coated asphalt.

[0013] As a preferred technical solution, the method for continuously producing lithium-ion battery negative electrode coated with asphalt specifically includes the following steps:

[0014] (1) An oxidative crosslinking reaction is carried out in the first reaction unit or the second reaction unit;

[0015] (2) Perform nitrogen stripping operation;

[0016] (3) Perform the reactor cleaning operation;

[0017] (4) Perform the drying operation of the reactor.

[0018] As a preferred technical solution, the oxidation-crosslinking reaction process in the first reaction unit of step (1) is as follows: ethylene heavy tar preheated to a certain temperature is fed into the first high-pressure reactor (RA) arranged on the upper layer through the first liquid phase feed line (L2A), and heated to the reaction temperature at a certain rate. Then, hot air is introduced into the first high-pressure reactor (RA) along the first air feed line (L7A) and the first gas distributor (DA) for stirring and oxidation-crosslinking reaction. The gas generated in the reaction process and the gas that did not participate in the reaction enter the gas phase product heat exchanger (HE2) along the first gas phase product line (L4A) on the cover of the first high-pressure reactor (RA) for condensation. The condensed gas-liquid mixture enters the gas-liquid separator (GLS) for gas-liquid separation. The gas phase component is used as reaction tail gas (TG2) for post-treatment, and the liquid phase component is collected as light chemical oil (HO).

[0019] Preferably, the oxidative crosslinking reaction process in the first reaction unit in step (1) is exactly the same as the oxidative crosslinking reaction process in the second reaction unit, and the oxidative crosslinking reaction process in the first reaction unit and the oxidative crosslinking reaction process in the second reaction unit are carried out alternately.

[0020] Preferably, the ethylene heavy tar is the heavy component remaining after the removal of methylnaphthalene and previous light fractions.

[0021] This invention uses ethylene heavy tar as raw material and achieves continuous production of high softening-point lithium-ion battery anode coating asphalt through switching operations between four reaction vessels. Furthermore, this invention employs a designed apparatus that, through a combined process of oxidative cross-linking followed by nitrogen stripping, can flexibly control the softening point and quinoline insoluble content of the anode coating asphalt, thereby improving the quality stability of the anode coating asphalt.

[0022] As a preferred technical solution, step (2) nitrogen stripping operation specifically involves: pressurized nitrogen supplied through the first pressurized nitrogen line (L3A) or the second pressurized nitrogen line (L3B) via the pressurized nitrogen manifold (NP) to pressurize the liquid phase product in the first high-pressure reactor (RA) or the second high-pressure reactor (RB) into the third high-pressure reactor (RC) or the fourth high-pressure reactor (RD) located directly below it. Then, through the third stripping nitrogen line (L7C) and the third gas distributor (DC), or the fourth stripping nitrogen line (L7D) and the fourth gas distributor (DD), nitrogen is supplied to the respective connected third high-pressure reactor (RC) or the second high-pressure reactor (RD). Hot stripping nitrogen (N2) is continuously introduced into the four high-pressure reactors (RD) for stirring and stripping. The stripped light components and stripping nitrogen are fed together through the third gas phase product line (L4C) or the fourth gas phase product line (L4D) into the gas phase product heat exchanger (HE2) for condensation, and then gas-liquid separation is carried out in the gas-liquid separator (GLS). After the stripping process is completed, pressurized nitrogen supplied by the pressurized nitrogen main pipe (NP) through the third pressurized nitrogen line (L3C) or the fourth pressurized nitrogen line (L3D) is used to pressurize the liquid phase product in the third high-pressure reactor (RC) or the fourth high-pressure reactor (RD), which is the lithium-ion battery negative electrode coated asphalt product (PC).

[0023] As a preferred technical solution, the nitrogen stripping operation conditions in step (2) are as follows: the temperature adjustment rate of the liquid product being pressed from the upper reactor into the lower reactor is 3-6℃ / min; the pressure is 0.1MPa-0.6MPa (gauge pressure); the temperature is 340-380℃; and the amount of nitrogen used for stripping is 12L / (kg ethylene heavy tar). min).

[0024] As a preferred technical solution, the reactor cleaning operation in step (3) is specifically as follows: after the reaction process is completed, the high-pressure cleaning water from the high-pressure cleaning water main (FW) is used to clean the first to fourth high-pressure reactors through their respective first to fourth high-pressure cleaning water lines and the first to fourth high-pressure water cleaners connected to them. The cleaning wastewater is sent to the wastewater treatment system through the first to fourth cleaning wastewater lines set at the bottom of each reactor. The present invention uses high-pressure water continuous rinsing to replace manual removal of the reactor adhering substances, which significantly improves the cleaning speed of the reactor, shortens the cooling and cleaning time, reduces labor intensity, and improves production efficiency.

[0025] As a preferred technical solution, the reactor drying operation in step (4) specifically involves: after the high-pressure reactor is cleaned, the first high-pressure reactor (RA) and the second high-pressure reactor (RB) are dried with hot air (AIR); the third high-pressure reactor (RC) and the fourth high-pressure reactor (RD) are dried with hot stripped nitrogen (N2); and the waste gas generated during the drying process is cooled and released into the drying waste gas heat exchanger (HE1) through the first to fourth drying waste gas lines.

[0026] Beneficial effects

[0027] 1. This invention provides an apparatus and method for continuous production of lithium-ion battery negative electrode coated asphalt, which can realize continuous production of high softening point lithium-ion battery negative electrode coated asphalt, reduce labor intensity, shorten process time, improve production efficiency, and stabilize product quality.

[0028] 2. The device provided by the present invention is designed to divide at least four reactors into upper and lower layers and arrange them symmetrically. The liquid phase product lines of the two reactors arranged in the upper layer are connected in series with the liquid phase raw material lines of the reactor arranged directly below them to form two identical reaction units. By switching the two reaction units in parallel, continuous production of lithium-ion battery negative electrode coating asphalt can be realized.

[0029] 3. The method provided by this invention first involves oxidative crosslinking and cracking reactions in the upper reactor, and then transferring the intermediate products to the lower reactor for nitrogen stripping. After each reactor completes its corresponding operation, it is cleaned with high-pressure water using a cleaning component located in the upper part of the reactor's inner cavity. Then, the reactor in the upper reactor is dried with hot air, and the reactor in the lower reactor is dried with hot stripped nitrogen, thereby achieving a circulating operation between the reactors.

[0030] 4. This invention uses ethylene heavy tar as raw material and achieves continuous production of high softening point lithium-ion battery anode coating asphalt through switching operations between four reaction vessels. Furthermore, this invention employs a designed apparatus that, through a combined process of oxidative cross-linking followed by nitrogen stripping, can flexibly control the softening point and quinoline insoluble content of the anode coating asphalt, thereby improving the quality stability of the anode coating asphalt.

[0031] 5. This invention uses high-pressure water continuous rinsing to replace manual removal of adhering substances from the reactor, which significantly improves the cleaning speed of the reactor, shortens the cooling and cleaning time, reduces labor intensity, and improves production efficiency. Attached Figure Description

[0032] Figure 1 This is a schematic diagram of an apparatus and method for continuously producing lithium-ion battery negative electrode coated with asphalt, provided in Embodiment 1 of the present invention.

[0033] In the picture:

[0034] RA, First high-pressure reactor; RB, Second high-pressure reactor; RC, Third high-pressure reactor; RD, Fourth high-pressure reactor;

[0035] PA, first pressure detection component; PB, second pressure detection component; PC, third pressure detection component; PD, fourth pressure detection component;

[0036] TA, First Temperature Monitoring Component; TB, Second Temperature Monitoring Component; TC, Third Temperature Monitoring Component; TD, Fourth Temperature Monitoring Component;

[0037] FNA, First High-Pressure Water Cleaner; FNB, Second High-Pressure Water Cleaner; FNC, Third High-Pressure Water Cleaner; FND, Fourth High-Pressure Water Cleaner;

[0038] DA, First gas distributor; DB, Second gas distributor; DC, Third gas distributor; DD, Fourth gas distributor;

[0039] F1, Nitrogen preheating furnace; F2, Air preheating furnace; HE1, Waste gas heat exchanger; HE2, Gas phase product heat exchanger; GLS, Gas-liquid separator.

[0040] VX (X=1A~8A, 1B~8B, 1C~8C, 1D~8D, 9, 10, 11, 12), valve;

[0041] L1A, First high-pressure cleaning water line; L1B, Second high-pressure cleaning water line; L1C, Third high-pressure cleaning water line; L1D, Fourth high-pressure cleaning water line;

[0042] L2A, First liquid phase feed line; L2B, Second liquid phase feed line; L2C, Third liquid phase feed line; L2D, Fourth liquid phase feed line;

[0043] L3A, First pressurized nitrogen line; L3B, Second pressurized nitrogen line; L3C, Third pressurized nitrogen line; L3D, Fourth pressurized nitrogen line;

[0044] L4A, First gas phase product line; L4B, Second gas phase product line; L4C, Third gas phase product line; L4D, Fourth gas phase product line;

[0045] L5A, First Drying Exhaust Gas Line; L5B, Second Drying Exhaust Gas Line; L5C, Third Drying Exhaust Gas Line; L5D, Fourth Drying Exhaust Gas Line;

[0046] L6A, First liquid phase product line; L6B, Second liquid phase product line; L6C, Third liquid phase product line; L6D, Fourth liquid phase product line;

[0047] L7A, First gas feed line; L7B, Second gas feed line; L7C, Third gas feed line; L7D, Fourth gas feed line;

[0048] L8A, First cleaning wastewater line; L8B, Second cleaning wastewater line; L8C, Third cleaning wastewater line; L8D, Fourth cleaning wastewater line;

[0049] HET, Ethylene Heavy Tar; FW, High Pressure Cleaning Water Main; NP, Pressurized Nitrogen Main; AIR, Air; N2, Stripped Nitrogen.

[0050] TG1, drying exhaust gas; TG2, reaction tail gas; HO, light chemical oil; PC, coated asphalt; SW, cleaning wastewater main pipe. Detailed Implementation

[0051] like Figure 1 As shown in the diagram, this invention provides an apparatus for the continuous production of lithium-ion battery anode coating asphalt, comprising four high-pressure reactors: a first high-pressure reactor (RA), a second high-pressure reactor (RB), a third high-pressure reactor (RC), and a fourth high-pressure reactor (RD). These four high-pressure reactors are arranged symmetrically in upper and lower layers. The first and second high-pressure reactors (RA and RB) are arranged in the upper layer, while the third and fourth high-pressure reactors (RC and RD) are symmetrically arranged in the lower layer. The liquid phase product lines and liquid phase feed lines of the symmetrically arranged first and third high-pressure reactors (RC), as well as the second and fourth high-pressure reactors (RB and RD), are connected in series to form two identical reaction units. By connecting the two reaction units in parallel and switching them, continuous production of lithium-ion battery anode coating asphalt can be achieved. To improve the operational flexibility of the apparatus, the connection methods also include connecting the first and fourth high-pressure reactors (RA) in series, and connecting the second and third high-pressure reactors (RB) in series.

[0052] As a preferred technical solution, the first high-pressure reactor (RA) is equipped with a first pressure detection component (PA) and a first temperature monitoring component (TA), the second high-pressure reactor (RB) is equipped with a second pressure detection component (PB) and a second temperature monitoring component (TB), the third high-pressure reactor (RC) is equipped with a third pressure detection component (PC) and a third temperature monitoring component (TC), and the fourth high-pressure reactor (RD) is equipped with a fourth pressure detection component (PD) and a fourth temperature monitoring component (TD), for controlling the pressure and temperature of the corresponding reactors. Each reactor is equipped with a high-pressure cleaning water inlet, a reaction raw material inlet, a pressurized nitrogen inlet, a gaseous product outlet, and a drying exhaust gas outlet on its top cover. The gaseous product outlet and the drying exhaust gas outlet are the same outlet. Each outlet is connected to the first to fourth high-pressure cleaning water lines, the first to fourth liquid raw material lines, the first to fourth pressurized nitrogen lines, the first to fourth gaseous product lines, and the first to fourth drying exhaust gas lines, respectively. Valves (V1X), (V2X), (V3X), (V4X), and (V5X) [X=A, B, C, D] are installed near each connecting pipeline to isolate different connecting pipelines from the reactor. The first to fourth high-pressure cleaning water lines are all connected to the high-pressure cleaning water main (FW); the first to fourth liquid-phase feedstock lines are all connected to ethylene heavy tar (HET); the first to fourth pressurized nitrogen lines are all connected to the pressurized nitrogen main (NP); the first to fourth gas-phase product lines are all connected to the inlet of the gas-phase product heat exchanger (HE2), the outlet of the gas-phase product heat exchanger (HE2) is connected to the inlet of the gas-liquid separator (GLS), the upper outlet of the gas-liquid separator (GLS) is connected to the reaction tail gas (TG2), and the lower outlet is connected to the light chemical oil (HO); the first to fourth drying exhaust gas lines are all connected to the inlet of the exhaust gas heat exchanger (HE1), and the outlet of the exhaust gas heat exchanger (HE1) is connected to the drying exhaust gas (TG1).

[0053] As a preferred technical solution, the bottom cover of the first to fourth high-pressure reactors is provided with a liquid product outlet, a gas feed inlet, and a cleaning wastewater outlet, which are respectively connected to the first to fourth liquid product lines, the first to fourth gas feed lines, and the first to fourth cleaning wastewater lines. Valves (V6X), (V7X), and (V8X) [X=A, B, C, D] are provided near the bottom of each connecting pipeline to achieve isolation between different connecting pipelines and the high-pressure reactor. The first liquid phase product line (L6A) and the second liquid phase product line (L6B) are both connected to the third liquid phase feed line (L2C) of the third high-pressure reactor (RC) and the fourth liquid phase feed line (L2D) of the fourth high-pressure reactor (RD). The third liquid phase product line (L6C) and the fourth liquid phase product line (L6D) are both connected to the asphalt coating product line (PC). The first to fourth gas feed lines are all connected to stripped nitrogen (N2) through a nitrogen preheating furnace (F1), while the first gas feed line (L7A) and the second gas feed line (L7B) are also connected to air (AIR) through an air preheating furnace (F2). The first to fourth cleaning wastewater lines are all connected to the cleaning wastewater main pipe (SW).

[0054] As a preferred technical solution, a first high-pressure water cleaner (FNA) that can move up and down and rotate is provided in the upper part of the inner cavity of the first high-pressure reactor (RA), a second high-pressure water cleaner (FNB) that can move up and down and rotate is provided in the upper part of the inner cavity of the second high-pressure reactor (RB), a third high-pressure water cleaner (FNC) that can move up and down and rotate is provided in the upper part of the inner cavity of the third high-pressure reactor (RC), and a fourth high-pressure water cleaner (FND) that can move up and down and rotate is provided in the upper part of the inner cavity of the fourth high-pressure reactor (RD), which are respectively connected to the first to fourth high-pressure cleaning water lines provided on the upper cover of the corresponding high-pressure reactor.

[0055] As a preferred technical solution, a first gas distributor (DA), a second gas distributor (DB), a third gas distributor (DC), and a fourth gas distributor (DD) are respectively provided at the bottom of the inner cavity of the first high-pressure reactor (RA), the second high-pressure reactor (RB), the third high-pressure reactor (RC), and the fourth high-pressure reactor (RD), which are respectively connected to the first to fourth gas feed lines.

[0056] As a preferred technical solution, the third liquid phase product line (L6C) of the third high-pressure reactor (RC) and the fourth liquid phase product line (L6D) of the fourth high-pressure reactor (RD) are both connected to the coated asphalt product (PC).

[0057] Another aspect of the present invention provides a method for continuously producing lithium-ion battery negative electrode coated asphalt, the specific operation process of which is as follows:

[0058] Close all valves of the device. Open valve (V4A) and the cooling water of the gas phase product heat exchanger (HE2), then open valve (V2A) to quantitatively feed ethylene heavy tar (HET) feedstock into the first high-pressure reactor (RA). Close valve (V2A) and control the temperature and pressure of the first high-pressure reactor (RA) to reach predetermined values. Open valves (V10) and (V7A) to introduce hot air (AIR) preheated to a certain temperature by the air preheater (F2) into the first gas distributor (DA) located at the bottom of the inner cavity of the high-pressure reactor. While bubbling and stirring the feedstock in the high-pressure reactor, the feedstock undergoes oxidation cross-linking and cracking reactions. The air that does not participate in the reaction and the light components generated by the cracking reaction are condensed and cooled by valve (V4A) and the gas phase product heat exchanger (HE2), and then enter the gas-liquid separator (GLS) for gas-liquid separation. The non-condensable gas enters the reaction tail gas (TG2) system, and the separated liquid phase component flows out through valve (V11) as light chemical oil (HO).

[0059] After the oxidative crosslinking reaction reaches the predetermined time, valve (V4A) is closed, and valves (V4C) and (V7C) are opened to introduce stripped nitrogen (N2) preheated by the nitrogen preheating furnace (F1) into the third high-pressure reactor (RC). Then, valves (V2C), (V6A), and (V3A) are opened sequentially to pressurize the intermediate product from the first high-pressure reactor (RA) into the third high-pressure reactor (RC) using pressurized nitrogen from the pressurized nitrogen main pipe (NP). When all the intermediate product in the first high-pressure reactor (RA) has been pressed into the third high-pressure reactor... After entering the reactor (RC), close valves (V3A), (V6A), (V7A), (V10), and (V2C); control the temperature and pressure of the third high-pressure reactor (RC), and use hot stripped nitrogen to stir and strip the material in the reactor. The stripped nitrogen and light components enter the gas phase product heat exchanger (HE2) through valve (V4C) for condensation and cooling, and then enter the gas-liquid separator (GLS) for gas-liquid separation. The non-condensable gas enters the reaction tail gas (TG2) system, and the separated liquid phase component flows out through valve (V11) as light chemical oil (HO).

[0060] When the nitrogen stripping operation begins in the third high-pressure reactor (RC), the first high-pressure reactor (RA) enters the cleaning operation. Valves (V1A) and (V8A) are opened to allow high-pressure cleaning water from the high-pressure cleaning water main (FW) to pass through the first high-pressure water cleaner (FNA) to clean the inner wall of the first high-pressure reactor (RA) and the outer surfaces such as the first gas distributor (DA). The wastewater enters the cleaning wastewater main (SW) system through valve (V8A).

[0061] After cleaning, valves (V1A) and (V8A) are closed, and the first high-pressure reactor (RA) enters the drying operation. Valve (V5A), (V7A), (V10), and the cooling water of the waste gas heat exchanger (HE1) are opened sequentially. Air (AIR), preheated by the air preheating furnace (F2), is introduced into the reactor through the first gas distributor (DA) to dry the high-pressure reactor. The drying waste gas is cooled by the waste gas heat exchanger (HE1) and then vented. The drying waste gas is sampled and analyzed before the waste gas heat exchanger (HE1). When the water content meets the requirements, valves (V5A), (V7A), and (V10) are closed, and the drying operation is stopped. The first high-pressure reactor (RA) can then enter the next cycle.

[0062] After the third high-pressure reactor (RC) completes the nitrogen stripping operation, close valves (V4C) and (V7C), and open valves (V3C) and (V6C) to inject the liquid phase product in the high-pressure reactor into the coated asphalt (PC) product system using pressurized nitrogen from the pressurized nitrogen main pipe (NP).

[0063] After all the liquid products in the third high-pressure reactor (RC) have been discharged, close valves (V3C) and (V6C), open valves (V1C) and (V8C), and complete the cleaning of the third high-pressure reactor (RC) according to the cleaning plan of the first high-pressure reactor (RA).

[0064] After the third high-pressure reactor (RC) completes its cleaning operation, valves (V1C) and (V8C) are closed, and valves (V5C) and (V7C) are opened. Preheated nitrogen gas from the nitrogen preheating furnace (F1) is used to dry the third high-pressure reactor (RC). The drying exhaust gas is cooled by the exhaust gas heat exchanger (HE1) and then vented. A sample of the drying exhaust gas is taken and analyzed before the exhaust gas heat exchanger (HE1). Once the water content meets the requirements, valves (V5C) and (V7C) are closed, and the drying operation is stopped. The third high-pressure reactor (RC) can then enter the next cycle.

[0065] As a preferred technical solution, the operation process and conditions of the second reaction unit are exactly the same as those of the first reaction unit, except that the operation of the second reaction unit is delayed by one step compared to the first reaction unit. Specifically: after the first high-pressure reactor (RA) of the first reaction unit completes the oxidative crosslinking reaction, the second high-pressure reactor (RB) of the second reaction unit begins the oxidative crosslinking reaction according to the exact same operation process and conditions; after the third high-pressure reactor (RC) of the first reaction unit completes the nitrogen stripping operation, the fourth high-pressure reactor (RD) of the second reaction unit begins the nitrogen stripping operation according to the exact same operation process and conditions. The cleaning and drying operations of each high-pressure reactor in the second reaction unit are also delayed by one step compared to the first reaction unit, and their methods are completely consistent with those of the first reaction unit. Through the above operations, continuous production of lithium-ion battery negative electrode coated asphalt can be achieved.

[0066] As a preferred technical solution, after the first high-pressure reactor (RA) completes the oxidative crosslinking reaction, the intermediate product can also be injected into the fourth high-pressure reactor (RD) by opening valves (V3A), (V6A), (V12) and (V2D) with pressurized nitrogen to complete the subsequent nitrogen stripping operation; similarly, after the second high-pressure reactor (RB) completes the oxidative crosslinking reaction, the intermediate product can also be injected into the third high-pressure reactor (RC) by opening valves (V3B), (V6B), (V12) and (V2C) with pressurized nitrogen to complete the subsequent nitrogen stripping operation, thereby improving the flexibility of the production apparatus and process described in this invention.

[0067] Example 1

[0068] Reference Figure 1 Embodiment 1 of the present invention provides an apparatus and method for continuous production of lithium-ion battery negative electrode coated asphalt, wherein a first reaction unit consisting of a first high-pressure reactor (RA) and a third high-pressure reactor (RC) connected in series is used to produce lithium-ion battery negative electrode coating material.

[0069] Close all valves in the first high-pressure reactor (RA) and the third high-pressure reactor (RC). Open valve (V4A) and the cooling water of the gas-phase product heat exchanger (HE2), then open valve (V2A) to feed approximately 2 / 3 of the volume of ethylene heavy tar (HET) feedstock into the first high-pressure reactor (RA), and close valve (V2A). Preheat the material in the first high-pressure reactor (RA) to 340°C and control the pressure at 0.6 MPa (gauge pressure); open valves (V10) and (V7A) at a rate of 1 L / (kg ethylene heavy tar)... Hot air (AIR) preheated to 150°C is introduced into the reactor at a flow rate of min to bubble and stir the raw materials in the reactor and cause them to undergo oxidative crosslinking and cracking reactions.

[0070] After the air has been introduced for 5 hours, close valves (V4A), (V10) and (V7A), and open valves (V3A), (V6A), (V2C) and (V4C). Use pressurized nitrogen from the 0.5MPa (gauge pressure) pressurized nitrogen main pipe (NP) to force all the intermediate products in the first high-pressure reactor (RA) into the third high-pressure reactor (RC). Then close valves (V3A), (V6A) and (V2C).

[0071] While the nitrogen stripping operation begins in the third high-pressure reactor (RC), the first high-pressure reactor (RA) enters the cleaning operation. Valves (V1A) and (V8A) are opened, and high-pressure cleaning water (3.0 MPa gauge pressure) from the high-pressure cleaning water main (FW) is used to clean the inner wall of the first high-pressure reactor (RA) and the outer surfaces, including the first gas distributor (DA), for 12 minutes. The cleaning wastewater enters the cleaning wastewater main (SW) system through valve (V8A). After cleaning, valves (V1A) and (V8A) are closed, and the first high-pressure reactor (RA) enters the drying operation. Valves (V5A), (V7A), (V10), and the cooling water of the waste gas heat exchanger (HE1) are opened sequentially to introduce air (AIR) preheated to 170°C by the air preheating furnace (F2) into the first high-pressure reactor (RA) for drying. The dried waste gas is cooled by the waste gas heat exchanger (HE1) and then vented. After drying for 25 minutes, the water content of the dried waste gas is less than 100µg / g, meeting the drying requirements. Valves (V5A), (V7A), and (V10) are then closed to stop the drying operation. The first high-pressure reactor (RA) then proceeds to the next round of operation.

[0072] The material in the third high-pressure reactor (RC) is preheated to 340°C at a temperature adjustment rate of 3°C / min, and the pressure is controlled at 0.6 MPa (gauge pressure); valve (V7C) is opened, and 2 L / (kg ethylene heavy tar) is introduced. At a flow rate of (min), stripping nitrogen (N2), preheated to 120°C by a nitrogen preheating furnace (F1), is introduced into the third high-pressure reactor (RC). The stripping nitrogen is used to stir and strip the material in the reactor, with the stripping time controlled at 1 hour. After the stripping operation is completed, valves (V4C) and (V7C) are closed, and valves (V3C) and (V6C) are opened. Pressurized nitrogen from the 0.5 MPa (gauge pressure) main nitrogen pipe (NP) is used to force out the liquid phase product in the third high-pressure reactor (RC), which is denoted as coated asphalt product PC1.

[0073] After all the liquid products in the third high-pressure reactor (RC) have been discharged, close valves (V3C) and (V6C), open valves (V1C) and (V8C), and complete the cleaning of the third high-pressure reactor (RC) according to the cleaning plan of the first high-pressure reactor (RA).

[0074] After the third high-pressure reactor (RC) completes its cleaning operation, valves (V1C) and (V8C) are closed, and valves (V5C) and (V7C) are opened. The reactor is then dried using stripped nitrogen gas preheated to 170°C in a nitrogen preheating furnace (F1). After 25 minutes of drying, the water content in the waste gas is less than 100 µg / g, meeting the drying requirements. Valve (V5C) and (V7C) are then closed, and the drying operation is stopped. The third high-pressure reactor (RC) then proceeds to the next stage of operation.

[0075] Example 2

[0076] Reference Figure 1 Embodiment 2 of the present invention provides an apparatus and method for continuous production of lithium-ion battery negative electrode coated asphalt, wherein the production of the lithium-ion battery negative electrode coating material is carried out by a second reaction unit consisting of a second high-pressure reactor (RB) and a fourth high-pressure reactor (RD) connected in series.

[0077] The operating procedure in this embodiment is exactly the same as that in Embodiment 1. The corresponding operating conditions are as follows:

[0078] The ethylene heavy tar (HET) feedstock is fed into the second high-pressure reactor (RB) to fill half its volume; the feedstock in the second high-pressure reactor (RB) is preheated to 380°C, and the pressure is controlled at 0.2 MPa (gauge pressure); the air is preheated to 200°C, and the flow rate is 2 L / (kg ethylene heavy tar). The ventilation time was 3.5 hours.

[0079] After all the liquid products in the second high-pressure reactor (RB) are discharged, the subsequent cleaning and drying conditions are as follows: high-pressure cleaning water pressure is 4.0 MPa (gauge pressure), cleaning time is 8 min; air preheating temperature is 200℃, drying time is 18 min.

[0080] The material in the fourth high-pressure reactor (RD) was kept at a constant temperature of 360°C at a rate of 5°C / min, while the pressure remained at atmospheric pressure. The preheating temperature of the stripping nitrogen was 180°C, and the flow rate was 1.5 L / (kg ethylene heavy tar). The air extraction time is 3 hours.

[0081] The coated asphalt product produced in this embodiment is designated as PC2.

[0082] After all the liquid products in the fourth high-pressure reactor (RD) are discharged, the subsequent cleaning and drying conditions are as follows: the high-pressure cleaning water pressure is 3.5 MPa (gauge pressure), the cleaning time is 10 min; the nitrogen gas preheating temperature is 180℃, and the drying time is 20 min.

[0083] Example 3

[0084] Reference Figure 1 Embodiment 3 of the present invention provides an apparatus and method for continuous production of lithium-ion battery negative electrode coated asphalt. The oxidation crosslinking operation is carried out in a first high-pressure reactor (RA), and the nitrogen stripping operation is carried out in a fourth high-pressure reactor (RD).

[0085] In this embodiment, the oxidative crosslinking procedure is exactly the same as that of the first high-pressure reactor (RA) in Example 1, and the nitrogen stripping procedure is exactly the same as that of the fourth high-pressure reactor (RD) in Example 2. The corresponding operating conditions are as follows:

[0086] The ethylene heavy tar (HET) feedstock fed into the first high-pressure reactor (RA) occupies 1 / 2 of its volume; the material preheating temperature in the first high-pressure reactor (RA) is 360℃, and the pressure is controlled at 0.4MPa (gauge pressure); the air preheating temperature is 180℃, and the flow rate is 1.5L / (kg ethylene heavy tar) The ventilation time is 4 hours. After the oxidative crosslinking reaction in the first high-pressure reactor (RA) is completed, valves (V4A) and (V7A) are closed, and valves (V4D), (V3A), (V6A), (V12) and (V2D) are opened to force all the liquid phase product in the first high-pressure reactor (RA) into the fourth high-pressure reactor (RD). Then, valves (V3A), (V6A), (V12) and (V2D) are closed.

[0087] After all the liquid products in the first high-pressure reactor (RA) are discharged, the subsequent cleaning and drying conditions are as follows: high-pressure cleaning water pressure is 4.0 MPa (gauge pressure), cleaning time is 8 min; air preheating temperature is 180℃, and drying time is 20 min.

[0088] The material in the fourth high-pressure reactor (RD) was kept at a constant temperature of 360°C at a rate of 6°C / min, with a pressure of 0.2 MPa (gauge pressure); the preheating temperature of the stripping nitrogen was 170°C, and the flow rate was 2 L / (kg ethylene heavy tar). The air extraction time is 2 hours.

[0089] The coated asphalt product produced in this embodiment is designated as PC3.

[0090] The cleaning and drying conditions for the fourth high-pressure reactor (RD) are as follows: the high-pressure cleaning water pressure is 3.0 MPa (gauge pressure), the cleaning time is 15 min; the nitrogen preheating temperature is 170℃, and the drying time is 25 min.

[0091] Example 4

[0092] Reference Figure 1 Embodiment 4 of the present invention provides an apparatus and method for continuous production of lithium-ion battery negative electrode coated asphalt, wherein the oxidation crosslinking operation is carried out in a second high-pressure reactor (RB) and the nitrogen stripping operation is carried out in a third high-pressure reactor (RC).

[0093] In this embodiment, the oxidative crosslinking procedure is exactly the same as that of the second high-pressure reactor (RB) in Example 2, and the nitrogen stripping procedure is exactly the same as that of the third high-pressure reactor (RC) in Example 1. The corresponding operating conditions are as follows:

[0094] The ethylene heavy tar (HET) feedstock is fed into the second high-pressure reactor (RB) to fill 2 / 3 of its volume; the material in the second high-pressure reactor (RB) is preheated to 350°C, and the pressure is controlled at 0.5 MPa (gauge pressure); the air is preheated to 190°C, and the flow rate is 1 L / (kg ethylene heavy tar). The ventilation time is 5 hours. After the oxidative crosslinking reaction in the second high-pressure reactor (RB) is completed, valves (V4B) and (V7B) are closed, and valves (V4C), (V3B), (V6B), (V12) and (V2C) are opened to force all the liquid phase product in the second high-pressure reactor (RB) into the third high-pressure reactor (RC). Then, valves (V3B), (V6B), (V12) and (V2C) are closed.

[0095] After all the liquid products in the second high-pressure reactor (RB) are discharged, the subsequent cleaning and drying conditions are as follows: high-pressure cleaning water pressure is 4.5 MPa (gauge pressure), cleaning time is 6 min; air preheating temperature is 190℃, and drying time is 19 min.

[0096] The material in the third high-pressure reactor (RC) is preheated to 360°C at a temperature adjustment rate of 4°C / min, and the pressure is controlled at 0.1 MPa (gauge pressure); the preheating temperature of the stripping nitrogen is 160°C, and the flow rate is 1.5 L / (kg ethylene heavy tar). The air extraction time is 3 hours.

[0097] The coated asphalt product produced in this embodiment is designated as PC4.

[0098] The cleaning and drying conditions for the third high-pressure reactor (RC) are as follows: the high-pressure cleaning water pressure is 3.0 MPa (gauge pressure), the cleaning time is 15 min; the nitrogen preheating temperature is 160℃, and the drying time is 28 min.

[0099] Performance testing methods

[0100] 1. The softening point, coking value, residual carbon value and quinoline insoluble content of the coated asphalt products prepared in the examples and comparative examples were determined. The results are shown in Table 1.

[0101] (1) Softening point: Refer to standard GB / T2294-2019 to test the softening point of the coated asphalt products prepared in the examples and comparative examples.

[0102] (2) Coking value: The coking value of the coated asphalt products prepared in the examples and comparative examples was tested in accordance with standard GB / T8728-2008;

[0103] (3) Carbon residue value: The carbon residue value of the coated asphalt products prepared in the examples and comparative examples was tested in accordance with standard SH / T0170-1992;

[0104] (4) Quinoline insoluble matter: Refer to standard GB / T2293-2019 to test the quinoline insoluble matter of the coated asphalt products prepared in the examples and comparative examples.

[0105] Table 1

[0106]

Claims

1. A method for continuous production of lithium-ion battery negative electrode coated asphalt, characterized in that, This is achieved through a device that continuously produces asphalt-coated negative electrodes for lithium-ion batteries. The apparatus for continuously producing lithium-ion battery negative electrode coated asphalt comprises at least four high-pressure reactors with temperature control functions: a first high-pressure reactor (RA), a second high-pressure reactor (RB), a third high-pressure reactor (RC), and a fourth high-pressure reactor (RD). The first high-pressure reactor (RA) is equipped with a first pressure detection component (PA) and a first temperature monitoring component (TA); the second high-pressure reactor (RB) is equipped with a second pressure detection component (PB) and a second temperature monitoring component (TB); the third high-pressure reactor (RC) is equipped with a third pressure detection component (PC) and a third temperature monitoring component (TC); and the fourth high-pressure reactor (RD) is equipped with a fourth pressure detection component. The first high-pressure reactor (RA) has a first liquid feed line (L2A), a first gaseous product line (L4A), and a first drying exhaust gas line (L5A) on its upper cover; the second high-pressure reactor (RB) has a second liquid feed line (L2B), a second gaseous product line (L4B), and a second drying exhaust gas line (L5B) on its upper cover; the third high-pressure reactor (RC) has a third liquid feed line (L2C), a third gaseous product line (L4C), and a third drying exhaust gas line (L5C) on its upper cover; and the fourth high-pressure reactor (RD) has a fourth liquid feed line (L2A). The reactor comprises a first gaseous product line (L2D), a fourth gaseous product line (L4D), and a fourth dry waste gas line (L5D). All four gaseous product lines are connected to the inlet of the gaseous product heat exchanger (HE2), and all four dry waste gas lines are connected to the inlet of the dry waste gas heat exchanger (HE1). A first gas distributor (DA) is located at the bottom of the inner cavity of the first high-pressure reactor (RA), a second gas distributor (DB) is located at the bottom of the inner cavity of the second high-pressure reactor (RB), a third gas distributor (DC) is located at the bottom of the inner cavity of the third high-pressure reactor (RC), and a fourth gas distributor (DD) is located at the bottom of the inner cavity of the fourth high-pressure reactor (RD). The first gas distributor (DA) in the first high-pressure reactor (RA) located in the upper layer is connected to the first air feed line (L7A) and the total nitrogen stripping line (L9); the second gas distributor (DB) in the second high-pressure reactor (RB) located in the upper layer is connected to the second air feed line (L7B) and the total nitrogen stripping line (L9); the third gas distributor (DC) in the third high-pressure reactor (RC) located in the lower layer is only connected to the third nitrogen stripping line (L7C); and the fourth gas distributor (DD) in the fourth high-pressure reactor (RD) located in the lower layer is only connected to the fourth nitrogen stripping line (L7D).The bottom cover of the third high-pressure reactor (RC) is equipped with a third liquid product line (L6C), and the bottom cover of the fourth high-pressure reactor (RD) is equipped with a fourth liquid product line (L6D). Both the third liquid product line (L6C) and the fourth liquid product line (L6D) are connected to the coated asphalt product line (PC). The first high-pressure reactor (RA), the second high-pressure reactor (RB), the third high-pressure reactor (RC), and the fourth high-pressure reactor (RD) are arranged in two layers, with the first high-pressure reactor (RA) and the second high-pressure reactor (RB) arranged on the upper layer, and the third high-pressure reactor (RC) and the fourth high-pressure reactor (RD) correspondingly arranged on the upper layer of the first high-pressure reactor (RA) and the second high-pressure reactor (RB). Directly below the first high-pressure reactor (RB); the first liquid phase product line (L6A) located on the bottom cover of the first high-pressure reactor (RA) and the third liquid phase feed line (L2C) located on the top cover of the third high-pressure reactor (RC) are connected in series to form a first reaction unit; the second liquid phase product line (L6B) located on the bottom cover of the second high-pressure reactor (RB) and the fourth liquid phase feed line (L2D) located on the top cover of the fourth high-pressure reactor (RD) are connected in series to form a second reaction unit; the first reaction unit and the second reaction unit are connected in parallel; the first liquid phase product line (L6A) on the bottom cover of the first high-pressure reactor (RA) and the fourth liquid phase feed line (L2D) on the top cover of the fourth high-pressure reactor (RD) are connected. The second liquid product line (L6B) on the bottom cover of the second high-pressure reactor (RB) is connected to the third liquid feed line (L2C) on the top cover of the third high-pressure reactor (RC); the upper part of the inner cavity of the first high-pressure reactor (RA) is provided with a first high-pressure water cleaner (FNA) that can move up and down and rotate, the upper part of the inner cavity of the second high-pressure reactor (RB) is provided with a second high-pressure water cleaner (FNB) that can move up and down and rotate, the upper part of the inner cavity of the third high-pressure reactor (RC) is provided with a third high-pressure water cleaner (FNC) that can move up and down and rotate, and the upper part of the inner cavity of the fourth high-pressure reactor (RD) is provided with a fourth high-pressure water cleaner (FND) that can move up and down and rotate; the first high-pressure water The first high-pressure water cleaner (FNA) is connected to one end of the first high-pressure cleaning water line (L1A) installed on the top cover of the first high-pressure reactor (RA); the second high-pressure water cleaner (FNB) is connected to one end of the second high-pressure cleaning water line (L1B) installed on the top cover of the second high-pressure reactor (RB); the third high-pressure water cleaner (FNC) is connected to one end of the third high-pressure cleaning water line (L1C) installed on the top cover of the third high-pressure reactor (RC); and the fourth high-pressure water cleaner (FND) is connected to one end of the fourth high-pressure cleaning water line (L1D) installed on the top cover of the fourth high-pressure reactor (RD). The other ends of the first to fourth high-pressure cleaning water lines are all connected to the high-pressure cleaning water main pipe (FW).The first high-pressure reactor (RA) has a first pressurized nitrogen line (L3A) on its top cover, the second high-pressure reactor (RB) has a second pressurized nitrogen line (L3B) on its top cover, the third high-pressure reactor (RC) has a third pressurized nitrogen line (L3C) on its top cover, and the fourth high-pressure reactor (RD) has a fourth pressurized nitrogen line (L3D) on its top cover; all the first to fourth pressurized nitrogen lines are connected to a main pressurized nitrogen pipe (NP); the first high-pressure reactor (RA) has a first cleaning wastewater line (L8A) on its bottom cover, the second high-pressure reactor (RB) has a second cleaning wastewater line (L8B) on its bottom cover, the third high-pressure reactor (RC) has a third cleaning wastewater line (L8C) on its bottom cover, and the fourth high-pressure reactor (RD) has a fourth cleaning wastewater line (L8D) on its bottom cover; all the first to fourth cleaning wastewater lines are connected to a main cleaning wastewater pipe (SW); The method for continuously producing lithium-ion battery negative electrode coated asphalt specifically includes the following steps: (1) An oxidative crosslinking reaction is carried out in the first reaction unit or the second reaction unit; (2) Perform nitrogen stripping operation; (3) Perform the reactor cleaning operation; (4) Perform the drying operation of the reaction vessel; The specific process of the oxidation-crosslinking reaction in the first reaction unit in step (1) is as follows: the ethylene heavy tar preheated to a certain temperature is fed into the first high-pressure reactor (RA) arranged on the upper layer through the first liquid phase feed line (L2A), and heated to the reaction temperature at a certain rate. Then, hot air is introduced into the first high-pressure reactor (RA) through the first air feed line (L7A) and the first gas distributor (DA) for stirring and oxidation-crosslinking reaction. The gas generated in the reaction process and the gas that did not participate in the reaction enter the gas phase product heat exchanger (HE2) along the first gas phase product line (L4A) on the cover of the first high-pressure reactor (RA) for condensation. The condensed gas-liquid mixture enters the gas-liquid separator (GLS) for gas-liquid separation. The gas phase component is used as reaction tail gas (TG2) for post-treatment, and the liquid phase component is collected as light chemical oil (HO). The nitrogen stripping operation in step (2) specifically involves: pressurized nitrogen supplied through the first pressurized nitrogen line (L3A) or the second pressurized nitrogen line (L3B) via the pressurized nitrogen main pipe (NP) to pressurize the liquid phase product in the first high-pressure reactor (RA) or the second high-pressure reactor (RB) into the third high-pressure reactor (RC) or the fourth high-pressure reactor (RD) located directly below it. Then, through the third stripping nitrogen line (L7C) and the third gas distributor (DC), or the fourth stripping nitrogen line (L7D) and the fourth gas distributor (DD), nitrogen is supplied to the third high-pressure reactor (RC) or the fourth high-pressure reactor respectively. In the (RD) reactor, hot stripping nitrogen (N2) is continuously introduced for stirring and stripping. The stripped light components and stripping nitrogen are fed together through the third gas phase product line (L4C) or the fourth gas phase product line (L4D) into the gas phase product heat exchanger (HE2) for condensation, and then gas-liquid separation is carried out in the gas-liquid separator (GLS). After the stripping process is completed, pressurized nitrogen supplied by the pressurized nitrogen manifold (NP) through the third pressurized nitrogen line (L3C) or the fourth pressurized nitrogen line (L3D) is used to pressurize the liquid phase product in the third high-pressure reactor (RC) or the fourth high-pressure reactor (RD), which is the lithium-ion battery negative electrode coated asphalt product (PC).

Images