Method for preparing carbon black by using high-temperature petroleum-based composite raw material

Abstract

The invention discloses a method for preparing carbon black by using a high-temperature petroleum-based composite raw material, and relates to a production and manufacturing process of carbon black. The method mainly comprises the five steps that preheated air and preheated combustion oil form high-temperature combustion airflow in a combustion chamber, light-component raw oil and heavy-component raw oil are added through a characteristic distributor to be preheated, then the raw oil is injected into a throat pipe to produce carbon black smoke, and quenching water is adopted in a cooling section to terminate the carbon black reaction. The carbon black flue gas sequentially enters an air preheater and an oil preheater after leaving from the cooling section; and the carbon black flue gas sequentially enters a carbon black grading device, a granulating device and a drying device after leaving from the oil preheater to be recycled. Compared with the prior art, scaling of high-temperature oil in the pipeline can be controlled by controlling the composition of the raw oil, the mode of the raw oil entering the heater and parameters such as the retention time and the flow speed of the raw oil, and long-period continuous industrial production of carbon black is achieved when the preheating temperature of the raw oil is higher than 300 DEG C.

Description

Technical Field

[0001] The present invention relates to a production process for carbon black, and in particular to a method for preparing carbon black using high-temperature petroleum-based composite raw materials. Background Art

[0002] Carbon black is a product of the incomplete combustion or cracking of hydrocarbons. It is primarily composed of elemental carbon. Its crystallites have a quasi-graphitic structure and are concentrically oriented. Its particles are nearly spherical colloidal particles, most of which are fused into aggregates. Carbon black is primarily used as a reinforcing agent in the rubber industry. It is also used as a colorant, UV shielding agent, antistatic agent, or conductive agent in a wide range of industries, including plastics, chemical fibers, inks, coatings, electronics, and batteries.

[0003] The basic process flow for furnace carbon black production is well-known. Fuel and oxidant combust fully, generating a high-temperature combustion gas stream. This high-temperature combustion gas stream flows into a reactor at high speed, mixing with preheated feedstock and reacting. The stream is then cooled, separated, and the carbon black is recovered. The fuel is typically natural gas or liquid hydrocarbons, the oxidant is often air or oxygen-enriched air, and the feedstock can be either gaseous or liquid hydrocarbons. Gaseous hydrocarbons are typically natural gas, while liquid hydrocarbons are typically ethylene tar, catalytic cracking slurry, coal tar, and distillates thereof, or a mixture thereof. However, fouling is a major technical obstacle to the use of high-temperature feedstocks in carbon black production. Fouling with high-temperature feedstocks can be attributed to two fouling mechanisms: film boiling and asphaltene-induced coking. In film boiling fouling, the feedstock evaporates and forms a vapor film that blocks heat transfer. This vapor film overheats and causes coke formation during gas-phase pyrolysis reactions. Furthermore, asphaltene, often present in raw oil, can undergo liquid-phase pyrolysis when used at high temperatures (e.g., above 300°C), resulting in coke formation. Regarding the preheating temperature of the crude oil, when the preheating temperature of the crude oil is high, such as exceeding 300°C, the crude oil is prone to coking in the heater or transportation pipeline.

[0004] Regarding the production of carbon black, Chinese invention patent publication number CN 116462995 A discloses a method and apparatus for online preparation of carbon black. The method utilizes a double-tube heating electric furnace. One tube uses a hydrocarbon material such as liquefied petroleum gas or natural gas as a feed gas, and uses nitrogen, argon, or other gases as an inert diluent. The feed gas is introduced into a volatile product of ferrocene n-hexane, which has a coking retarder, through a volatilization barrel of a coking retarder. The feed gas is then rapidly delivered to the high-temperature zone of the furnace tube for cracking, producing a mixed gas containing nano-scale carbon black, thereby achieving the first step of carbon black production. The other tube passes compressed air containing water as a coking retarder to burn deposited carbon black and decompose coke on the furnace tube. The two tubes operate alternately, and the gases from the two tubes are then cooled and mixed. After the mixture, the feed gas and compressed air are added, and the mixture is incompletely burned. The carbon black layer is then sprayed onto the metal surface to form a carbon black layer, thereby achieving the second step of carbon black production. This carbon black layer has larger carbon black particles and excellent metal-to-metal lubrication properties at high temperatures, thereby improving the utilization efficiency of the raw materials and achieving energy conservation and emission reduction. This technical solution uses a double-tube heating electric furnace, which requires alternating operation, involves a large number of devices, and is complex to operate, and cannot guarantee the safety and efficiency of the carbon black manufacturing process.

[0005] In view of this, in order to solve the above technical problems, the present application aims to make improvements in aspects such as raw oil and preheating and feeding of raw oil, solve the above technical problems and increase the yield of carbon black. Summary of the Invention

[0006] The object of the present invention is to provide a method for preparing carbon black using a high-temperature petroleum-based composite raw material. By controlling the composition of the raw oil and the way the raw oil enters the heater, as well as controlling parameters such as the residence time and flow rate of the raw oil, the scaling of the high-temperature oil in the pipeline can be controlled. When the raw oil preheating temperature is higher than 300°C, continuous industrial production of carbon black can be achieved over a long period of time, thereby increasing the yield of carbon black and reducing the emission rate of sulfur and nitrogen oxides.

[0007] To achieve the above object, the present invention provides a method for preparing carbon black using a high-temperature petroleum-based composite raw material, comprising the following steps:

[0008] S1: The air required for carbon black production and combustion is pressurized by the main air supply fan, enters the air preheater for preheating, and then enters the reactor combustion chamber. The fuel oil is heated by the fuel oil heater and sprayed into the reactor through the fuel oil gun. It mixes with the preheated air in the combustion chamber and burns fully to form a high-temperature combustion airflow.

[0009] S2: Perform steps S2.1 and S2.2 simultaneously:

[0010] Step S2.1: A first pump is used to introduce the light component feedstock oil through the center hole of the distributor into the heater. After heating to the desired temperature, the light component feedstock oil is sprayed into the throat of the reactor through the ejector. In the reactor, the light component feedstock oil mixes with the high-temperature combustion airflow and rapidly cracks to produce carbon black flue gas.

[0011] Step S2.2: A second pump swirls the heavy component feedstock oil through a distributor into the heater. After heating to the desired temperature, the oil is sprayed into the throat of the reactor through an ejector. The heavy component feedstock oil mixes with the high-temperature combustion airflow in the reactor, rapidly cracking to produce carbon black flue gas.

[0012] S3: After the carbon black flue gas enters the cooling section, quenching water is sprayed in the cooling section. After quenching, the temperature of the carbon black flue gas drops to 950°C. At this time, potassium carbonate solution is sprayed into the cooling section. If the temperature of the carbon black flue gas in the cooling section drops to 700°C, the spraying is stopped;

[0013] S4: After leaving the cooling section, the carbon black flue gas goes to the air preheater and the oil preheater in sequence;

[0014] S5: After leaving the oil preheater, the carbon black flue gas enters the carbon black classification device, granulation device and drying device in sequence.

[0015] According to the embodiments of the present application, the density of the light component feedstock oil is not greater than 1.05 g / cm³, the density of the heavy component feedstock oil is greater than 1.10 g / cm³, and the ratio of the light component feedstock oil to the heavy component feedstock oil in the feedstock oil is 2:8~8:2.

[0016] According to an embodiment of the present application, the distributor is a circular body as a whole, which includes a central hole and at least one annular slit arranged with the central hole as the center of the circle. The inlet pipe of the heavy component feedstock is tangent to the outer circumference of the distributor, so that the heavy component feedstock is introduced into the heater in a vortex along the annular slit; the inlet pipe of the light component feedstock is connected to the central hole, so that the light component feedstock is introduced into the heater from the central hole.

[0017] According to an embodiment of the present application, the distributor is a circular body as a whole, which includes a central hole and multiple injection holes evenly arranged on the central body. The inlet pipe of the heavy component feedstock is tangent to the outer circumference of the distributor, so that the heavy component feedstock is vortex-wise introduced into the heater from the multiple injection holes; the inlet pipe of the light component feedstock is connected to the central hole, so that the light component feedstock is introduced into the heater from the central hole.

[0018] According to an embodiment of the present application, ethylene tar is used as the fuel oil.

[0019] According to an embodiment of the present application, the preheating temperature of the feedstock oil is not less than 300°C.

[0020] According to an embodiment of the present application, in step S2, the residence time of the raw oil in the heater is not higher than 1 minute, the residence time of the raw oil from the heater outlet to the reactor inlet is not higher than 1 minute, and the running speed of the raw oil in the heater and the flow rate in the throat from the heater to the reactor are not lower than 0.3 m / s.

[0021] According to an embodiment of the present application, the flow rate of the heavy component feedstock oil entering the heater is higher than the flow rate of the light component feedstock oil, and the flow rate difference is 0.2-1 m / s.

[0022] According to an embodiment of the present application, the raw oil is catalytic cracking slurry, and the asphaltene content of the catalytic cracking slurry is less than 1%.

[0023] According to an embodiment of the present application, the cooling section is provided with 1-4 quench coolers, and the quenching water in the quench cooler is directly sprayed into the high-temperature air flow containing carbon black through a nozzle to cool it and terminate the carbon black reaction.

[0024] The beneficial effects of the technical solution of the present invention compared with the prior art are:

[0025] 1. The present invention uses catalytic cracking slurry or treated catalytic cracking slurry as feedstock oil and controls its asphaltene content, which can effectively reduce the coking problem of feedstock oil caused by asphaltene at high temperatures.

[0026] 2. The present invention controls the manner in which the feedstock oil enters the heater, dividing the feedstock oil into heavy-component feedstock oil and light-component feedstock oil. A distributor is provided on the heater, so that the heavy-component feedstock oil enters the heater in a vortex-like manner along the periphery of the distributor, and the light-component feedstock oil is introduced from the center of the distributor. At the same time, a speed difference between the introduction of the two feedstock oils is set, which increases the disturbance in the conveying pipeline and the heater, facilitates heat transfer, hinders the formation of a vapor film, and avoids the problem of overheating of the vapor film and causing coking formation in the gas-phase pyrolysis reaction.

[0027] 3. The method of the present invention can realize continuous production for a longer period at a higher raw oil preheating temperature, and can realize continuous industrial production of carbon black for a longer period, such as continuous production for more than 72 hours, when the raw oil preheating temperature is higher than 300°C. BRIEF DESCRIPTION OF THE DRAWINGS

[0028] Figure 1 This is a flowchart of a method for preparing carbon black using a high-temperature petroleum-based composite raw material in an example of the present invention;

[0029] Figure 2 This is a schematic diagram of the reactor structure for preparing carbon black structure in an example of the present invention.

[0030] The following are the descriptions of the reference numerals:

[0031] 11. Combustion chamber, 12. Throat, 13. Cooling section, 14. Heater. DETAILED DESCRIPTION

[0032] The present invention will be further described below in conjunction with the accompanying drawings and specific examples. The following examples are used to illustrate the present invention, but are not intended to limit the scope of the present invention.

[0033] See Figure 1 and Figure 2 , a method for preparing carbon black using a high-temperature petroleum-based composite raw material is shown, comprising the following steps:

[0034] S1: The air required for carbon black production and combustion is pressurized by the main air supply fan, enters the air preheater for preheating, and then enters the reactor combustion chamber 11. The fuel oil is heated by the fuel oil heater 14 and sprayed into the reactor through the fuel oil gun. It mixes with the preheated air in the combustion chamber 11 and is fully burned to form a high-temperature combustion airflow.

[0035] Specifically, the fuel oil can be ethylene tar or an oil product with similar properties, or light oil can be used as the combustion oil. The lower calorific value of the fuel oil is greater than 8000Kcal / kg, preferably greater than 9000Kcal / kg.

[0036] S2: Perform steps S2.1 and S2.2 simultaneously:

[0037] Step S2.1: A first pump is used to introduce the light component feedstock oil through the center hole of the distributor into the heater 14. After heating to the desired temperature, the light component feedstock oil is sprayed into the throat 12 of the reactor by the ejector. In the reactor, the light component feedstock oil mixes with the high-temperature combustion airflow and is rapidly cracked to produce carbon black flue gas.

[0038] Step S2.2: A second pump is used to introduce the heavy component feedstock oil into the heater 14 in a vortex manner through a distributor. After heating to the required temperature, the heavy component feedstock oil is sprayed into the throat 12 of the reactor through an ejector. In the reactor, the heavy component feedstock oil mixes with the high-temperature combustion airflow and is rapidly cracked to produce carbon black flue gas.

[0039] Specifically, the density of the light component feedstock oil is not greater than 1.05 g / cm³, the density of the heavy component feedstock oil is greater than 1.10 g / cm³, and the ratio of the light component feedstock oil to the heavy component feedstock oil in the feedstock oil is 2:8~8:2, preferably in the range of 4:6~6:4.

[0040] Specifically, the distributor as a whole can be a circular body, which includes a central hole and at least one annular slit arranged with the central hole as the center of the circle. The inlet pipe of the heavy component feedstock is tangent to the outer circumference of the distributor, so that the heavy component feedstock is vortex-wise introduced into the heater 14 along the annular slit; the inlet pipe of the light component feedstock is connected to the central hole, so that the light component feedstock is introduced into the heater from the central hole.

[0041] Specifically, the distributor as a whole can be a circular body, which can also include a center hole and multiple injection holes evenly arranged on the center body. The inlet pipe of the heavy component feedstock is tangent to the outer circumference of the distributor, so that the heavy component feedstock is vortex-wise introduced into the heater 14 from the multiple injection holes; the inlet pipe of the light component feedstock is connected to the center hole, so that the light component feedstock is introduced into the heater 14 from the center hole.

[0042] Specifically, the flow rate of the heavy component feedstock at the outer periphery of the distributor is higher than the flow rate of the light component feedstock at the inner periphery, with the flow rate difference being no less than 0.1 m / s, and preferably being 0.2-1 m / s. That is, the flow rate of the heavy component feedstock entering the heater 14 is higher than the flow rate of the light component feedstock, with the flow rate difference being 0.2-1 m / s.

[0043] Specifically, the preheating temperature of the feedstock oil is not less than 300° C. The beneficial effects of increasing the preheating temperature of the feedstock oil to 300° C. include improved energy recovery, savings in raw material costs, increased carbon black yield, reduced carbon dioxide emissions, and reduced sulfur and nitrogen oxide emissions. At the same time, using a high preheating temperature feedstock oil can effectively reduce the polycyclic aromatic hydrocarbon content of the carbon black.

[0044] Specifically, the residence time of the raw oil in the heater 14 is not longer than 1 minute, preferably not longer than 30 seconds.

[0045] Specifically, in step S2, the residence time of the raw oil in the heater 14 is not higher than 1 minute, and the residence time of the raw oil from the outlet of the heater 14 to the inlet of the reactor is not higher than 1 minute, preferably not higher than 30 seconds; the running speed of the raw oil in the heater 14 and the flow rate in the throat 12 from the heater 14 to the reactor are not lower than 0.3 m / s, and the flow rate is preferably not lower than 0.5 m / s.

[0046] Specifically, if Figure 1 As shown in FIG, at least two pumps are required to introduce the light component feedstock oil and the heavy component feedstock oil into the heater 14 respectively. The pumps can pressurize the feedstock oil to ensure that it has a sufficient flow rate.

[0047] It is understood that when the pressure leaving the heater 14 has a rapid pressure drop compared to the pressure at the inlet of the heater 14, it can be considered a coking signal. Generally, when comparing the inlet pressure of the heater 14 and the pressure leaving the heater 14, there will be a normal pressure drop, which is caused by the friction of the raw materials in the pipeline. However, during steady-state operation of the device, when a rapid or uncontrolled pressure drop change occurs at the outlet of the heater 14, it will be considered a signal that coking may or will occur. For example, when the general pressure drop change exceeds 2%, it is considered that coking may have occurred in the raw oil in the heater 14. Therefore, the pressure drop change at the outlet of the heater 14 or the pressure drop change at the inlet of the raw oil in the reactor can be used as a reference indicator of whether coking has occurred.

[0048] S3: After the carbon black flue gas enters the cooling section 13, quenching water is sprayed in the cooling section 13. After quenching, the temperature of the carbon black flue gas drops to 950°C. At this time, nitrogen reducing agent is sprayed into the cooling section 13. If the temperature of the carbon black flue gas in the cooling section 13 drops to 700°C, the spraying is stopped.

[0049] Specifically, the cooling section 13 may be provided with 1-4 quench coolers, and the quenching water in the quench cooler is directly sprayed into the high-temperature air flow containing carbon black through a nozzle to cool the air and terminate the carbon black reaction.

[0050] Specifically, the raw oil is catalytic cracking slurry, and the asphaltene content of the catalytic cracking slurry is less than 1%.

[0051] S4: After leaving the cooling section 13, the carbon black flue gas goes to the air preheater and the oil preheater in sequence.

[0052] S5: After leaving the oil preheater, the carbon black flue gas enters the carbon black classification device, granulation device and drying device in sequence.

[0053] Overall embodiment

[0054] The preheated high-temperature air, reaching a temperature of approximately 850°C, reacts, mixes, and combusts with the preheated combustion oil, heated to approximately 120°C, in the reactor combustion chamber 11, generating a high-temperature combustion airflow at a temperature of approximately 2000°C. This high-temperature combustion airflow flows into the reactor throat 12, where it is sprayed with feedstock oil, preheated to a temperature exceeding 300°C. The feedstock oil mixes with the high-temperature combustion airflow in the reactor chamber and rapidly cracks, producing carbon black flue gas. After entering the cooling section 13, the carbon black flue gas is sprayed with quenching water, rapidly cooling it to 950°C. At this point, potassium carbonate solution is sprayed into the cooling section 13. After exiting the cooling section 13, the carbon black flue gas is sequentially directed to the air preheater and the oil preheater. After exiting the oil preheater, the carbon black flue gas sequentially enters the carbon black classification device, the granulation device, and the drying device, where the carbon black is finally recovered.

[0055] In this embodiment, the combustion oil used is ethylene tar, and its properties are shown in Table 1; the properties of the raw material oil are shown in Table 2.

[0056] Table 1

[0057]

[0058] Table 2

[0059]

[0060] The operating steps of Example 1 and Example 2 are consistent with the general example. The raw material oil and operating parameters used in Examples 1 and 2 are shown in Table 3.

[0061] The operating steps of Comparative Examples 1, 2, 3 and 4 are consistent with those of the general embodiment. The raw material oils and operating parameters used in Comparative Examples 1 to 4 are shown in Table 3.

[0062] Table 3

[0063]

[0064] As shown in Table 3, ① Under steady-state operating conditions, a rapid pressure drop occurred after 6 hours of operation, indicating that coking occurred. To protect the equipment, the test was stopped. ② Under steady-state operating conditions, a rapid pressure drop occurred after 5 hours of operation, indicating that coking occurred. To protect the equipment, the test was stopped. ③ Under steady-state operating conditions, a rapid pressure drop occurred after 6 hours of operation, indicating that coking occurred. To protect the equipment, the test was stopped. Under steady-state operating conditions, a rapid pressure drop occurred after 6 hours of operation, indicating the occurrence of coking. To protect the equipment, the test was stopped. Table 3 shows that the method of the present invention can achieve long-term continuous production at a higher feedstock oil preheating temperature. Examples 1 and 2 can achieve continuous production for more than 72 hours without coking.

[0065] The properties and yield (by weight) of carbon black produced at a conventional crude oil preheating temperature (e.g., 200°C) were compared with those of the carbon black produced in Examples 1 and 2. The carbon black properties were characterized as follows: iodine absorption value: measured according to the method specified in GB / T 380.1-2015; DBP (dibutyl phthalate) absorption: measured according to the method specified in GB / T 380.2-2017; specific surface area: measured according to the method specified in GB / T 10722-2014; and polycyclic aromatic hydrocarbon content in carbon black: measured according to the method specified in GB / T 3780.28-2020. Specific results are shown in Table 4.

[0066] Table 4

[0067]

[0068] As can be seen from Table 4, the carbon black obtained using the present invention exhibits significantly lower polycyclic aromatic hydrocarbon (PAH) content compared to conventional carbon black with the same morphology produced at conventional crude oil preheating temperatures (e.g., 200°C), with PAH content reduced by 28% and 36% in Examples 1 and 2, respectively. Furthermore, the carbon black yield can be increased by the present invention compared to conventional carbon black with the same morphology produced at conventional crude oil preheating temperatures (e.g., 200°C), with carbon black yields increased by 6% and 10% in Examples 1 and 2, respectively.

[0069] In summary, the technical solution of this application has the following beneficial effects:

[0070] 1. The present invention uses catalytic cracking slurry or treated catalytic cracking slurry as feedstock oil and controls its asphaltene content, which can effectively reduce the coking problem of feedstock oil caused by asphaltene at high temperatures.

[0071] 2. The present invention controls the manner in which the feedstock oil enters the heater, dividing the feedstock oil into heavy-component feedstock oil and light-component feedstock oil. A distributor is provided on the heater, so that the heavy-component feedstock oil enters the heater in a vortex-like manner along the periphery of the distributor, and the light-component feedstock oil is introduced from the center of the distributor. At the same time, a speed difference between the introduction of the two feedstock oils is set, which increases the disturbance in the conveying pipeline and the heater, facilitates heat transfer, hinders the formation of a vapor film, and avoids the problem of overheating of the vapor film and causing coking formation in the gas-phase pyrolysis reaction.

[0072] 3. The method of the present invention can realize continuous production for a longer period at a higher raw oil preheating temperature, and can realize continuous industrial production of carbon black for a longer period, such as continuous production for more than 72 hours, when the raw oil preheating temperature is higher than 300°C.

[0073] The above are only preferred embodiments of the present invention and do not limit the implementation mode and protection scope of the present invention. For those skilled in the art, it should be aware that all solutions obtained by equivalent substitutions and obvious changes made using the description and illustrations of the present invention should be included in the protection scope of the present invention.

Claims

1. A method for preparing carbon black using a high-temperature petroleum-based composite raw material, characterized in that: The following steps are involved: S1: The air required for carbon black production and combustion is pressurized by the main air supply fan, enters the air preheater for preheating, and then enters the reactor combustion chamber. The fuel oil is heated by the fuel oil heater and sprayed into the reactor through the fuel oil gun. It mixes with the preheated air in the combustion chamber and burns fully to form a high-temperature combustion airflow. S2: Perform steps S2.1 and S2.2 simultaneously: Step S2.1: A first pump is used to introduce the light component feedstock oil through the center hole of the distributor into the heater. After heating to the desired temperature, the light component feedstock oil is sprayed into the throat of the reactor through the ejector. In the reactor, the light component feedstock oil mixes with the high-temperature combustion airflow and rapidly cracks to produce carbon black flue gas. Step S2.2: A second pump swirls the heavy component feedstock oil through a distributor into the heater. After heating to the desired temperature, the oil is sprayed into the throat of the reactor through an ejector. The heavy component feedstock oil mixes with the high-temperature combustion airflow in the reactor, rapidly cracking to produce carbon black flue gas. S3: After the carbon black flue gas enters the cooling section, quenching water is sprayed in the cooling section. After quenching, the temperature of the carbon black flue gas drops to 950°C. At this time, potassium carbonate solution is sprayed into the cooling section. If the temperature of the carbon black flue gas in the cooling section drops to 700°C, the spraying is stopped; S4: After leaving the cooling section, the carbon black flue gas goes to the air preheater and the oil preheater in sequence; S5: After leaving the oil preheater, the carbon black flue gas enters the carbon black classification device, granulation device and drying device in sequence, and finally the carbon black is recovered.

2. The method for preparing carbon black using high-temperature petroleum-based composite raw materials according to claim 1, characterized in that: The density of the light component feedstock oil is not greater than 1.05 g / cm³, the density of the heavy component feedstock oil is greater than 1.10 g / cm³, and the ratio of the light component feedstock oil to the heavy component feedstock oil in the feedstock oil is 2:8 to 8:

2.

3. The method for preparing carbon black using high-temperature petroleum-based composite raw materials according to claim 1, characterized in that: The distributor is a circular body as a whole, which includes a central hole and at least one annular slit arranged with the central hole as the center. The inlet pipe of the heavy component feedstock is tangent to the outer circumference of the distributor, so that the heavy component feedstock is introduced into the heater in a vortex along the annular slit; the inlet pipe of the light component feedstock is connected to the central hole, so that the light component feedstock is introduced into the heater from the central hole.

4. The method for preparing carbon black using high-temperature petroleum-based composite raw materials according to claim 1, characterized in that: The distributor is a circular body as a whole, which includes a central hole and multiple injection holes evenly arranged on the central body. The inlet pipe of the heavy component feedstock is tangent to the outer circumference of the distributor, so that the heavy component feedstock is vortex-wise introduced into the heater from the multiple injection holes; the inlet pipe of the light component feedstock is connected to the central hole, so that the light component feedstock is introduced into the heater from the central hole.

5. The method for preparing carbon black using high-temperature petroleum-based composite raw materials according to claim 1, characterized in that: The fuel oil is ethylene tar.

6. The method for preparing carbon black using high-temperature petroleum-based composite raw materials according to claim 1, characterized in that: The preheating temperature of the raw oil shall not be less than 300℃.

7. The method for preparing carbon black using high-temperature petroleum-based composite raw materials according to claim 1, characterized in that: In step S2, the residence time of the raw oil in the heater is not more than 1 minute, the residence time of the raw oil from the outlet of the heater to the inlet of the reactor is not more than 1 minute, and the running speed of the raw oil in the heater and the flow rate in the throat from the heater to the reactor are not less than 0.3 m / s.

8. The method for preparing carbon black using high-temperature petroleum-based composite raw materials according to claim 1, characterized in that: The flow rate of the heavy component feedstock oil entering the heater is higher than the flow rate of the light component feedstock oil, and the flow rate difference is 0.2-1 m / s.

9. The method for preparing carbon black using high-temperature petroleum-based composite raw materials according to claim 1, characterized in that: The raw oil is catalytic cracking slurry, and the asphaltene content of the catalytic cracking slurry is less than 1%.

10. The method for preparing carbon black using high-temperature petroleum-based composite raw materials according to claim 1, characterized in that: The cooling section is provided with 1-4 quenchers, and the quenching water in the quencher is directly sprayed into the high-temperature air flow containing carbon black through a nozzle to cool the air and terminate the carbon black reaction.

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