A method and system for lco guided electric carbon black

Abstract

The present application relates to a method and system for guiding electric carbon black by LCO, by reasonable utilization of components in LCO, LCO is cracked at different reaction zones according to the properties of the fractions, which improves the yield of carbon black and the effective utilization rate of LCO. The method for producing carbon black can simply and efficiently prepare electrically conductive carbon black, and the yield of carbon black is high.

Description

Technical Field

[0001] This invention relates to the field of petrochemicals, specifically to a method and system for producing conductive carbon black from LCO. Background Technology

[0002] In my country, due to declining crude oil reserves and increasing environmental awareness, the availability of low-quality oil and increased processing profits have led to a decrease in the market share of low-quality gasoline and diesel. Simultaneously, the demand for high-quality gasoline is gradually increasing. Meanwhile, slower economic growth has resulted in a structural surplus of diesel, causing its market share to gradually decline. The shortage of chemical feedstocks such as low-carbon olefins and aromatics still needs to be addressed to achieve refining transformation and further development. Therefore, it is necessary to develop high-temperature cracking technology for producing chemical feedstocks from low-quality heavy oil, thereby achieving a successful transformation from oil to chemicals.

[0003] Carbon black is an important chemical raw material, widely used in the rubber industry as a reinforcing filler, colorant, or toner, and also in inks, coatings, leather making, chemical fibers, metallurgy, electronics, photosensitive materials, black agricultural films, and packaging materials. Existing carbon black production technologies include furnace black, channel black, pyrolysis black, and lampblack production processes. Chinese patent (ZL89104111) provides a carbon black production method using natural gas as fuel and oxygen-enriched gas as a combustion aid. This method improves furnace temperature stability and ensures heat supply, but it does not effectively address the issues of carbon black yield and quality.

[0004] Conductive carbon black is generally obtained as a byproduct of acetylene production from natural gas. The main reaction process involves heating the raw materials, natural gas and oxygen, to specific temperatures in gas preheaters before mixing and entering the reactor. Part of the natural gas is burned to provide heat for the reaction, while the remaining natural gas undergoes a cracking reaction at around 1500°C to produce acetylene. Acetylene readily decomposes into carbon black and hydrogen at high temperatures, so the optimal reaction time at high temperatures is only a few milliseconds. The reaction is terminated by water quenching. Although the reaction time is extremely short, carbon black is still produced. In this process, carbon black is a byproduct.

[0005] CN110204930B discloses a production method and conveying equipment for controlling the specific surface area of ​​conductive carbon black, belonging to the field of conductive carbon black preparation technology. The production method for controlling the specific surface area of ​​conductive carbon black includes subjecting a mixture of acetylene and hydrocarbon raw materials to a cracking reaction at 1300–1500°C; the hydrocarbon raw materials include one or more combinations of hydrocarbon compounds. The conductive carbon black obtained by introducing acetylene for cracking reaction at 1800°C generally has a specific surface area of ​​over 80 m² / g. CN112210233A relates to a method for preparing conductive carbon black, mainly addressing the lack of effective regeneration methods for carbon black byproducts from acetylene production from natural gas. This invention provides a method for preparing conductive carbon black, comprising the following steps: (a) acid treatment: treating the raw carbon black with an acid solution to obtain conductive carbon black intermediate product I; (b) alkali treatment: treating conductive carbon black intermediate product I with an alkali solution to obtain conductive carbon black intermediate product II; (c) salt loading: mixing conductive carbon black intermediate product II with a salt-containing aqueous solution to obtain conductive carbon black intermediate product III; (d) calcination: calcining conductive carbon black intermediate product III to obtain the finished conductive carbon black product. This technical solution effectively solves the problem and can be used in the recovery and utilization of carbon black by-products from natural gas-to-acetylene production in industrial plants. CN112210233A describes a granular conductive carbon black and its preparation method, belonging to the field of conductive carbon black technology. The preparation method of granular conductive carbon black includes sequentially wetting the conductive carbon black raw material with water at a temperature ≥80℃, wet granulation, and drying. By using water at a temperature ≥80℃ to wet the conductive carbon black raw material, the hydrophilicity of the conductive carbon black raw material is enhanced. The water at a temperature ≥80℃ enters the microporous structure of the conductive carbon black raw material, achieving a good wetting effect. Then, granular conductive acetylene carbon black with uniform particle size distribution is obtained by wet granulation and drying. Summary of the Invention

[0006] The purpose of this invention is to provide a method for producing conductive carbon black from catalytic diesel fuel.

[0007] A first aspect of the present invention provides a method for producing conductive carbon black using LCO, comprising:

[0008] (1) The LCO is cut into aromatic components and non-aromatic components, wherein the LCO cutting temperature is 210-260℃, the non-aromatic components are fractions with a distillation range less than the cutting temperature, and the aromatic components are fractions with a distillation range greater than the cutting temperature.

[0009] (2) Non-aromatic components are introduced into the first cracking reactor to undergo cracking reaction. The first cracking product is then introduced into the second cracking reactor under the action of carrier gas and merged with aromatic components to continue cracking reaction, resulting in a second cracking product containing conductive carbon black and cracking gas.

[0010] (3) The second pyrolysis product enters the carbon black collector, and is separated by quenching and cooling to obtain the solid product conductive carbon black. The gaseous product is further washed and filtered before entering the pyrolysis gas collector for collection.

[0011] According to the method of the first aspect, the reaction temperature of the first pyrolysis reactor is 1800-2000℃;

[0012] The reaction time of the first pyrolysis reactor is 2 milliseconds to 30 milliseconds;

[0013] The reaction temperature of the second pyrolysis reactor is 1100-1800℃, preferably 1200-1500℃; and / or

[0014] The reaction time of the second pyrolysis reactor is 2 milliseconds to 5 seconds, preferably 40 milliseconds to 2 seconds.

[0015] According to the method of the first aspect, the carrier gas is selected from one or more of the following: methane, nitrogen, dry gas, helium, argon, and C2-C4 light hydrocarbons;

[0016] Preferably, the carrier gas is preheated before entering the first pyrolysis reactor, and the preheating temperature is 800-2500℃, more preferably 1500-2300℃.

[0017] According to the method of the first aspect, the aromatic component and the non-aromatic component are introduced into the first cracking reactor and the second cracking reactor respectively after preheating, and the preheating temperature is 200-600℃, preferably 230-250℃.

[0018] According to the method of the first aspect, the feed ratio of carrier gas to LCO per unit time is 0.5-200 liters / gram, preferably 1-40 liters / gram.

[0019] According to the method of the first aspect, the cooling rate of the quenching is 50-1000℃ / ms, preferably 50-500℃ / ms; and / or

[0020] The temperature of the product after rapid cooling is 100-900℃, preferably 200-500℃;

[0021] Preferably, a quenching medium is used to quench and cool the second pyrolysis product, wherein the quenching medium is selected from one or more of the following: water, nitrogen, argon, and more preferably liquid nitrogen.

[0022] A second aspect of the present invention provides a system for producing conductive carbon black using LCO, comprising:

[0023] The raw material cutting device is equipped with an LCO inlet, an aromatic component outlet, and a non-aromatic component outlet, and is used to cut LCO into aromatic components and non-aromatic components.

[0024] The carrier gas preheating unit includes one or more carrier gas preheating furnaces connected in series. Preferably, the carrier gas preheating unit includes two carrier gas preheating furnaces.

[0025] The reaction unit includes:

[0026] The first pyrolysis reactor is used to pyrolyze non-aromatic components. The first pyrolysis reactor is connected to the non-aromatic component outlet of the raw material cutting device and the carrier gas outlet of the carrier gas preheating unit, respectively.

[0027] The second cracking reactor is used to crack the aromatic components and the first cracking product obtained from the first cracking reactor. The second cracking reactor is connected to the aromatic component outlet of the raw material cutting device and the first cracking product outlet of the first cracking reactor, respectively.

[0028] Product collection unit, including

[0029] A carbon black collector is provided with a quench medium inlet and a gas product outlet, which is used to cool the second pyrolysis product obtained from the second pyrolysis reactor and collect conductive carbon black. The carbon black collector is connected to the second pyrolysis product outlet of the second pyrolysis reactor.

[0030] One or more gas scrubbing and carbon black filters for scrubbing and filtering gaseous products exiting from a carbon black collector;

[0031] A pyrolysis gas collector is used to collect pyrolysis gas products that have been washed and filtered by a gas scrubbing and carbon black filter.

[0032] According to the system of the second aspect, the first pyrolysis reactor and / or the second pyrolysis reactor are tubular reactors;

[0033] Preferably, the material of the tubular reactor is selected from one or more of the following: tungsten, molybdenum, tantalum, niobium, vanadium, chromium, titanium, zirconium, rare earth metal borides, rare earth metal carbides, rare earth metal nitrides, rare earth metal silicides, rare earth metal phosphides, and rare earth metal sulfides, wherein the rare earth metal is selected from one or more of lanthanum, cerium, praseodymium, and neodymium.

[0034] According to the system of the second aspect, an electromagnetic induction coil for heating is provided around the periphery of the first pyrolysis reactor and / or the second pyrolysis reactor.

[0035] According to the system of the second aspect, the first pyrolysis reactor is arranged vertically or horizontally, preferably vertically; and / or

[0036] The second pyrolysis reactor is set horizontally.

[0037] The advantages of the present invention through the above technical solution are as follows:

[0038] (1) The electromagnetic induction coil heating of the pyrolysis reactor can achieve rapid heating of the pyrolysis reactor, and the reaction temperature control is simple and the operation is stable.

[0039] (2) By making reasonable use of the components in catalytic cracking diesel (LCO), the catalytic cracking diesel (LCO) is subjected to high-temperature cracking in different reaction zones according to the composition of the fractions, which not only improves the yield of carbon black, but also improves the effective utilization rate of catalytic cracking diesel (LCO).

[0040] (3) The method for producing carbon black of the present invention can prepare conductive carbon black in a simple and efficient manner, and the yield of carbon black is high. Attached Figure Description

[0041] Figure 1 The diagram shows a flow chart and structural schematic of a specific embodiment of the method for producing conductive carbon black according to the present invention.

[0042] Figure 2 The test results of the battery capacity of the conductive carbon black prepared in Example 1 of the present invention as a conductive agent for lithium batteries are shown.

[0043] Figure 3 The charge-discharge curves of the conductive carbon black material prepared in Example 1 at different rates are shown.

[0044] Figure 4 A TEM image of the conductive carbon black prepared in Example 1 is shown.

[0045] Explanation of reference numerals in the attached figures:

[0046] 1. LCO injection line; 2. Carrier gas injection line; 3-7, 9, 11-13, lines; 8. Quenching medium inlet line; 14. LCO raw material cutting device; 15. Carrier gas preheating furnace I; 16. Carrier gas preheating furnace II; 17. Pyrolysis reactor I; 18. Pyrolysis reactor II; 19. Carbon black collector; 20. Gas scrubbing and carbon black filter I; 21. Gas scrubbing and carbon black filter II; 22. Gas collector. Detailed Implementation

[0047] The present application will now be described in further detail with reference to the accompanying drawings and embodiments. Through these descriptions, the features and advantages of the present application will become clearer and more apparent.

[0048] The term “exemplary” as used herein means “serving as an example, embodiment, or illustration.” Any embodiment illustrated herein as “exemplary” is not necessarily to be construed as superior to or better than other embodiments. Although various aspects of embodiments are shown in the accompanying drawings, the drawings are not necessarily drawn to scale unless specifically indicated otherwise.

[0049] Furthermore, the technical features involved in the different embodiments of this application described below can be combined with each other as long as they do not conflict with each other.

[0050] Before describing the technical solution of this invention, the terms used herein are defined as follows:

[0051] The term "LCO" refers to light cycle oil, which is catalytic cracked diesel.

[0052] The term "aromatic fraction" refers to the heavy fraction of LCO that is rich in aromatics after being cut.

[0053] The term "non-aromatic fraction" refers to the light fraction of LCO that is not rich in aromatics after cleavage.

[0054] This invention provides a method for producing conductive carbon black using LCO, comprising:

[0055] (1) The LCO is cut into aromatic components and non-aromatic components, wherein the LCO cutting temperature is 210-260℃, the non-aromatic components are fractions with a distillation range less than the cutting temperature, and the aromatic components are fractions with a distillation range greater than the cutting temperature.

[0056] (2) Non-aromatic components are introduced into the first cracking reactor to undergo cracking reaction. The first cracking product is then introduced into the second cracking reactor under the action of carrier gas and merged with aromatic components to continue cracking reaction, resulting in a second cracking product containing conductive carbon black and cracking gas.

[0057] (3) The second pyrolysis product enters the carbon black collector, and is separated by quenching and cooling to obtain the solid product conductive carbon black. The gaseous product is further washed and filtered before entering the pyrolysis gas collector for collection.

[0058] Analysis of the properties of catalytic cracked diesel (LCO) reveals that most aromatic compounds are concentrated in the heavy fraction. Studies have shown that aromatic compounds are precursors for carbon black production, which is beneficial for increasing carbon black yield. Furthermore, research on the formation mechanism of acetylene shows that straight-chain hydrocarbons are more conducive to acetylene formation. Therefore, this invention utilizes the components of catalytic cracked diesel (LCO) rationally, conducting high-temperature cracking reactions in different reaction zones based on the fractional composition to obtain acetylene and carbon black products respectively. This improves both the yield of acetylene and carbon black, and also enhances the effective utilization rate of catalytic cracked diesel (LCO).

[0059] The present invention will be further described below with reference to the accompanying drawings and specific embodiments, but the present invention is not limited thereto.

[0060] like Figure 1As shown, LCO is cut into aromatic and non-aromatic components in LCO raw material cutting device 14 according to its properties. Carrier gas is introduced into carrier gas preheating furnace I15 and carrier gas preheating furnace II 16 through carrier gas injection line 2 for heating. Non-aromatic components are introduced into cracking reactor I17 from top to bottom through pipeline 5, and aromatic components are introduced into cracking reactor II 18 through pipeline 6. The gaseous products of cracking reactor I17 and the raw materials of cracking reactor II 18 are combined to form the raw materials of cracking reactor II 18 and cracked together in cracking reactor II 18. The cracking products enter carbon black collector 19 and enter the quench water of carbon black collector 19 through quench medium inlet pipeline 8 to quench the products and terminate the reaction. Then, they enter gas washing and carbon black filter I 20 and gas washing and carbon black filter II 21 in sequence, and enter the subsequent separation system to obtain conductive carbon black. The gaseous products are collected in gas collector 22.

[0061] This invention employs an electromagnetic induction heating pyrolysis reactor, enabling rapid heating and stable temperature control. Compared to plasma reactors, this equipment is simpler, smaller, and easier to implement and operate. By combining the pyrolysis reaction in the electromagnetic induction heating pyrolysis reactor with a controlled rapid cooling rate within a specific range, this invention can produce higher yields of high-quality conductive carbon black.

[0062] According to the present invention, the pyrolysis reaction is completed at ultra-high temperature and in a very short time. Compared with plasma reactors, the pyrolysis reactor of the present invention has a simple structure, the pyrolysis process is easy to control, and the energy consumption is low.

[0063] In one embodiment, the reaction temperature of the first pyrolysis reactor is 1800-2000°C;

[0064] The reaction time of the first pyrolysis reactor is 2 milliseconds to 30 milliseconds;

[0065] The reaction temperature of the second pyrolysis reactor is 1100-1800℃, preferably 1200-1500℃; and / or

[0066] The reaction time of the second pyrolysis reactor is 2 milliseconds to 5 seconds, preferably 40 milliseconds to 2 seconds, and more preferably 40 milliseconds to 1 second.

[0067] According to the present invention, the method may further include: preheating the pyrolysis feedstock and carrier gas before feeding them into the pyrolysis reactor, so that the pyrolysis feedstock and carrier gas rapidly reach the reaction temperature in the pyrolysis reactor. The temperatures of the preheated pyrolysis feedstock and carrier gas can vary within a wide range. The carrier gas serves two purposes: firstly, to control the reaction time, allowing the pyrolysis feedstock to pass through the pyrolysis reactor rapidly; and secondly, to provide a high-temperature reaction gas environment for the pyrolysis of the feedstock.

[0068] In one embodiment, the carrier gas is selected from one or more of the following: methane, nitrogen, dry gas, helium, argon, and C2-C4 light hydrocarbons;

[0069] Preferably, the carrier gas is preheated before entering the first pyrolysis reactor, and the preheating temperature is 800-2500℃, more preferably 1500-2300℃.

[0070] In one embodiment, the aromatic and non-aromatic components are preheated and then introduced into a first cracking reactor and a second cracking reactor, respectively. The preheating temperature is 200-600°C, preferably 230-250°C.

[0071] In one embodiment, the feed ratio of carrier gas to LCO per unit time is 0.5-200 liters / gram, preferably 1-40 liters / gram.

[0072] In one embodiment, the feed ratio of carrier gas to non-aromatic component feedstock is 0.5-200 liters / gram, preferably 1-40 liters / gram; and / or

[0073] The feed ratio of carrier gas to aromatic component feedstock per unit time is 0.1-50 liters / gram, preferably 0.5-10 liters / gram.

[0074] According to the present invention, rapid cooling is used to rapidly cool the reaction products to terminate the reaction and generate products with a specific composition. The quenching medium used for rapid cooling is a medium well known to those skilled in the art.

[0075] In one embodiment, the cooling rate of the rapid cooling is 50-1000°C / ms, preferably 50-500°C / ms; and / or

[0076] The temperature of the product after rapid cooling is 100-900℃, preferably 200-500℃;

[0077] Preferably, a quenching medium is used to quench and cool the second pyrolysis product, wherein the quenching medium is selected from one or more of the following: water, nitrogen, argon, and more preferably liquid nitrogen.

[0078] The present invention also provides a system for producing conductive carbon black using LCO, comprising:

[0079] The raw material cutting device is equipped with an LCO inlet, an aromatic component outlet, and a non-aromatic component outlet, and is used to cut LCO into aromatic components and non-aromatic components.

[0080] The carrier gas preheating unit includes one or more carrier gas preheating furnaces connected in series. Preferably, the carrier gas preheating unit includes two carrier gas preheating furnaces.

[0081] The reaction unit includes:

[0082] The first pyrolysis reactor is used to pyrolyze non-aromatic components. The first pyrolysis reactor is connected to the non-aromatic component outlet of the raw material cutting device and the carrier gas outlet of the carrier gas preheating unit, respectively.

[0083] The second cracking reactor is used to crack the aromatic components and the first cracking product obtained from the first cracking reactor. The second cracking reactor is connected to the aromatic component outlet of the raw material cutting device and the first cracking product outlet of the first cracking reactor, respectively.

[0084] Product collection unit, including

[0085] A carbon black collector is provided with a quench medium inlet and a gas product outlet, which is used to cool the second pyrolysis product obtained from the second pyrolysis reactor and collect conductive carbon black. The carbon black collector is connected to the second pyrolysis product outlet of the second pyrolysis reactor.

[0086] One or more gas scrubbing and carbon black filters for scrubbing and filtering gaseous products exiting from a carbon black collector;

[0087] A pyrolysis gas collector is used to collect pyrolysis gas products that have been washed and filtered by a gas scrubbing and carbon black filter.

[0088] In one embodiment, the first pyrolysis reactor and / or the second pyrolysis reactor are tubular reactors;

[0089] Preferably, the material of the tubular reactor is selected from one or more of the following: tungsten, molybdenum, tantalum, niobium, vanadium, chromium, titanium, zirconium, rare earth metal borides, rare earth metal carbides, rare earth metal nitrides, rare earth metal silicides, rare earth metal phosphides, and rare earth metal sulfides, wherein the rare earth metal is selected from one or more of lanthanum, cerium, praseodymium, and neodymium.

[0090] In one embodiment, an electromagnetic induction coil for heating is provided around the periphery of the first pyrolysis reactor and / or the second pyrolysis reactor.

[0091] In one embodiment, the first pyrolysis reactor is arranged vertically or horizontally, preferably vertically; and / or

[0092] The second pyrolysis reactor is set horizontally.

[0093] According to the present invention, the pyrolysis reactor is a reactor capable of electromagnetic induction heating, for example, a horizontally arranged metal tubular reactor. There are no specific limitations on the manner in which the pyrolysis feedstock and carrier gas are introduced into the metal tubular reactor. In one specific embodiment, the pyrolysis feedstock and carrier gas are introduced into the metal tubular reactor from the front, and the reaction products are led out of the metal tubular reactor from the rear. A quenching medium is introduced from pipeline 8 through a nozzle into a carbon black collector to quench and cool the reaction products exiting the reactor. An electromagnetic induction coil may be fitted around the outer periphery of the metal tubular reactor to heat the reactor through the alternating magnetic field generated by the electromagnetic induction coil.

[0094] The present invention will be further illustrated by the following examples, but the present invention is not limited thereto.

[0095] like Figure 1 As shown, LCO is cut into non-aromatic and aromatic components in LCO feedstock cutting device 14. The non-aromatic components are preheated to 500-2000°C via pipeline 5, carrier gas preheating furnace I15, and carrier gas preheating furnace II16, and then enter cracking reactor I17 via pipeline 4 for cracking reaction. The aromatic components obtained from LCO feedstock cutting device 14 and the products from cracking reactor I17 enter cracking reactor II18 via pipelines 6 and 7 for cracking reaction. The products enter carbon black collector 19 and are quenched by quenching medium via pipeline 8. The products are then rapidly cooled to 200-500°C (the cooling rate of the reaction products is 100°C / ms during rapid cooling). The quenching medium from pipeline 8 is injected into the bottom of carbon black collector 19 through the quenching medium inlet at the bottom of carbon black collector 19 to further cool and separate the gaseous products. Among them, the gaseous products containing acetylene enter the gas washing and carbon black filter I20 and the gas washing and carbon black filter II21 through the gas outlet of carbon black collector 19. The resulting product gas enters the gas collector 22 through pipeline 13.

[0096] Example 1

[0097] This embodiment is in Figure 1In the system shown, LCO with properties as described in Table 1 is used as the cracking feedstock. The cutting temperature is 260℃, with fractions below 260℃ being non-aromatic components and fractions above 260℃ being aromatic components. Nitrogen is used as the carrier gas. The first preheating temperature of carrier gas preheating furnace I is 500℃, and the second preheating temperature of carrier gas preheating furnace II is 1500℃. A quartz tube serves as the reactor, and a graphite tube is used as the heating medium. The quartz tube in the first cracking reactor is vertically arranged along its length, with an inner diameter of 10mm and a length of 38mm. An electromagnetic induction coil is fitted around the outer circumference of the quartz tube. The quartz tube in the second cracking reactor is horizontally arranged along its axial direction, with an inner diameter of 20mm and a length of 50mm. An electromagnetic induction coil is also fitted around the outer circumference of the quartz tube. Water is introduced into the carbon black collector 19 from the quench medium inlet at the bottom as the quench medium, with a flow rate of 4 liters / minute. The cooling rate of the reaction products is controlled at 100℃ / millisecond, reducing their temperature to approximately 250℃. The acetylene-containing gaseous product enters through the gas outlet of carbon black collector 19, and is sequentially washed and filtered through carbon black filters I20 and II21. The resulting product gas enters gas collector 22 through pipeline 13. The carbon black product is separated and dried to obtain conductive carbon black product. The quality of catalytic cracking diesel is shown in Table 1.

[0098] Table 1 Properties of Catalytic Cracking Diesel

[0099]

[0100]

[0101] The specific conditions for Example 1 are as follows: the first reaction temperature is 1800℃, the second reaction temperature is 1500℃, nitrogen is used as the carrier gas with a flow rate of 4 L / min, the LCO feed rate is 1.0 g / min, the oil feeding time is 4 minutes, the first reaction time is 25 ms, the second reaction time is 50 ms, the cooling rate is 100℃ / ms, and the product temperature is 200℃. The composition of the gaseous product is as follows: gas yield 10.58%, carbon black yield 89.42%, of which hydrogen accounts for 0.73%, methane 4.86%, and acetylene 1.71%. This demonstrates that staged feeding can better convert the raw material into carbon black and improve the carbon black yield. The property analysis of carbon black is shown in the appendix. Figure 2-4 As shown.

[0102] Electrochemical performance testing

[0103] The conductive carbon black prepared in Example 1 was assembled into a battery with lithium iron phosphate. The assembled battery was first allowed to stand at 25°C for 5 hours before electrochemical performance testing. The charge-discharge performance of the battery was tested on a blue electric system, with a test voltage of 2.0–3.9 V. The test items included the battery's charge-discharge specific capacity, cycle performance, and rate performance. Cyclic voltammetry (CV) testing of the battery was performed on an electrochemical analyzer.

[0104] (1) Charge and discharge performance test

[0105] The purpose of this test is to obtain data on the battery's initial charge-discharge cycle stability and rate performance. The test system used is the Blue Battery test system, and the test conditions are 25℃, 2.0~3.9V, and a current density of 160mAh / g. Before the test, the assembled battery is placed at 25℃ for 5 hours before subsequent tests.

[0106] (2) Cyclic Voltmeter-Ampere Test (CV)

[0107] Cyclic voltammetry analyzes the electrochemical performance of a battery by studying the redox processes occurring at the electrodes. The instrument used was a Shanghai Chenhua CHI electrochemical analyzer, and the test conditions were: room temperature, test voltage 2.5–4 V, and scan rate 0.2 mV / s.

[0108] from Figure 2 The battery capacity test curve shows that as the rate increases, the discharge specific capacity decreases slightly; however, when the rate returns to its initial value, the discharge specific capacity returns to its original state, indicating that the battery has good and relatively stable capacity. Figure 3 The results show that the prepared conductive carbon black has a very good stability of the charge and discharge voltage plateau and has good charge and discharge performance.

[0109] from Figure 4 TEM images show that the carbon black produced by this invention consists of approximately spherical particles, some of which are connected end-to-end to form chain-like aggregates, while others overlap; the particle size is generally less than 100 nm; and the connected end-to-end aggregates form chain-like aggregates. Therefore, the method and system of this invention can be used to prepare conductive carbon black, and the prepared conductive carbon black has good electrical conductivity.

[0110] In the description of this application, it should be noted that, unless otherwise expressly specified and limited, the terms "installation," "connection," and "linking" should be interpreted broadly. Those skilled in the art can understand the specific meaning of these terms in this application based on the specific circumstances.

[0111] The present application has been described above with reference to preferred embodiments; however, these embodiments are merely exemplary and illustrative. Various substitutions and modifications can be made to the present application based on these embodiments, all of which fall within the protection scope of the present application.

Claims

1. A method for producing conductive carbon black using LCO, comprising: (1) The LCO is cut into aromatic components and non-aromatic components, wherein the LCO cutting temperature is 210-260℃, the non-aromatic components are fractions with a distillation range less than the cutting temperature, and the aromatic components are fractions with a distillation range greater than the cutting temperature. (2) Non-aromatic components are introduced into the first cracking reactor to undergo cracking reaction. The first cracking product is then introduced into the second cracking reactor under the action of carrier gas and merged with the aromatic components to continue cracking reaction, resulting in a second cracking product containing conductive carbon black and cracking gas. (3) The second pyrolysis product enters the carbon black collector, and is separated by quenching and cooling to obtain the solid product conductive carbon black. The gaseous product is further washed and filtered before entering the pyrolysis gas collector for collection. Wherein, the reaction temperature of the first pyrolysis reactor is 1800-2000℃; and / or The reaction temperature of the second pyrolysis reactor is 1100-1800℃.

2. The method according to claim 1, characterized in that, The reaction temperature of the second pyrolysis reactor is 1200-1500℃.

3. The method according to claim 1 or 2, characterized in that, The reaction time of the first pyrolysis reactor is 2 milliseconds to 30 milliseconds; and / or The reaction time of the second pyrolysis reactor is 2 milliseconds to 5 seconds.

4. The method according to claim 3, characterized in that, The reaction time of the second pyrolysis reactor is 40 milliseconds to 2 seconds.

5. The method according to claim 1, characterized in that, The carrier gas is selected from one or more of the following: methane, nitrogen, dry gas, helium, argon, and C2-C4 light hydrocarbons.

6. The method according to claim 5, characterized in that, The carrier gas is preheated before entering the first pyrolysis reactor, and the preheating temperature is 800-2500℃.

7. The method according to claim 6, characterized in that, The preheating temperature is 1500-2300℃.

8. The method according to claim 1, characterized in that, The aromatic and non-aromatic components are preheated and then introduced into the first and second cracking reactors, respectively, at a preheating temperature of 200-600℃.

9. The method according to claim 8, characterized in that, The preheating temperature is 230-250℃.

10. The method according to claim 1, characterized in that, The feed ratio of carrier gas to LCO per unit time is 0.5-200 liters / gram.

11. The method according to claim 10, characterized in that, The feed ratio of carrier gas to LCO per unit time is 1-40 liters / gram.

12. The method according to claim 1, characterized in that, The cooling rate of the quenching is 50-1000℃ / ms; and / or The temperature of the product after rapid cooling is 100-900℃.

13. The method according to claim 1, characterized in that, The cooling rate of the quenching is 50-500℃ / millisecond; and / or The temperature of the product after rapid cooling is 200-500℃.

14. The method according to claim 1, characterized in that, The second pyrolysis product is cooled by a quenching medium selected from one or more of the following: water, nitrogen, and argon.

15. The method according to claim 1, characterized in that, The quenching medium is liquid nitrogen.

16. A system for producing conductive carbon black using LCO, comprising: The raw material cutting device is equipped with an LCO inlet, an aromatic component outlet, and a non-aromatic component outlet, and is used to cut LCO into aromatic components and non-aromatic components. A carrier gas preheating unit includes one or more carrier gas preheating furnaces connected in series, wherein the carrier gas preheating unit includes two carrier gas preheating furnaces; The reaction unit includes: The first pyrolysis reactor is used to pyrolyze non-aromatic components. The first pyrolysis reactor is connected to the non-aromatic component outlet of the raw material cutting device and the carrier gas outlet of the carrier gas preheating unit, respectively. The second cracking reactor is used to crack the aromatic components and the first cracking product obtained from the first cracking reactor. The second cracking reactor is connected to the aromatic component outlet of the raw material cutting device and the first cracking product outlet of the first cracking reactor, respectively. Product collection unit, including A carbon black collector is provided with a quench medium inlet and a gas product outlet, which is used to cool the second pyrolysis product obtained from the second pyrolysis reactor and collect conductive carbon black. The carbon black collector is connected to the second pyrolysis product outlet of the second pyrolysis reactor. One or more gas scrubbing and carbon black filters for scrubbing and filtering gaseous products exiting from a carbon black collector; A pyrolysis gas collector is used to collect pyrolysis gas products that have been washed and filtered by a gas scrubbing and carbon black filter.

17. The system according to claim 16, characterized in that, The first pyrolysis reactor and / or the second pyrolysis reactor are tubular reactors.

18. The system according to claim 17, characterized in that, The tubular reactor is made of one or more of the following materials: tungsten, molybdenum, tantalum, niobium, vanadium, chromium, titanium, zirconium, rare earth metal borides, rare earth metal carbides, rare earth metal nitrides, rare earth metal silicides, rare earth metal phosphides, and rare earth metal sulfides, wherein the rare earth metal is selected from one or more of lanthanum, cerium, praseodymium, and neodymium.

19. The system according to claim 16, characterized in that, The outer periphery of the first pyrolysis reactor and / or the second pyrolysis reactor is fitted with an electromagnetic induction coil for heating.

20. The system according to claim 16, characterized in that, The first pyrolysis reactor is arranged vertically or horizontally; and / or The second pyrolysis reactor is set horizontally.

21. The system according to claim 16, characterized in that, The first pyrolysis reactor is vertically positioned.

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