Reaction furnace for producing carbon black based on de-crystallized anthracene oil

Abstract

The present application relates to the technical field of reaction furnace, in particular to a reaction furnace for producing carbon black based on de-crystallized anthracene oil, which comprises a combustion section, a throat pipe, a reaction section, a quenching section and a residence section fixed and communicated in sequence along the axial direction, and a plurality of pre-vaporization assemblies for vaporizing raw material oil by using the waste heat of flue gas from the residence section. The pre-vaporization assembly comprises a flue gas main pipe, a vaporizer and a raw material oil injection pipe, the gas inlet end of the flue gas main pipe is communicated with the residence section, and the discharge end of the raw material oil injection pipe is communicated with the throat pipe. The vaporizer comprises a tubular heat exchanger, a feed pipe, a discharge pipe, an air inlet pipe and an air outlet pipe. The feed pipe is used for feeding de-crystallized anthracene oil, the feed end of the raw material oil injection pipe is communicated with the discharge pipe, the air inlet pipe is communicated with the gas outlet end of the flue gas main pipe, and the air outlet pipe is used for feeding the heat-exchanged flue gas into a waste heat boiler. The reaction furnace can avoid coking on the outlet end face of the raw material oil injection gun, improve the production efficiency, and improve the structural uniformity of the carbon black product and reduce the impurity content.

Description

Technical Field

[0001] This invention relates to the field of reactor technology, and in particular to a reactor for producing carbon black based on decrystalline anthracene oil. Background Technology

[0002] The oil furnace method is the mainstream process for carbon black production. Its basic principle is to first fully combust fuels such as natural gas with air in the combustion section of the reactor to generate high-temperature flue gas with a temperature greater than 1400℃; then, the feed oil is radially injected into the high-temperature flue gas zone of the reaction section of the reactor from the throat pipe. The feed oil undergoes atomization, vaporization, cracking and other reaction processes in sequence to generate carbon black, and is discharged from the reactor after the reaction is quickly terminated by rapid cooling.

[0003] The oil-fired furnace process for producing carbon black utilizes a wide variety of feedstock oils, including coal tar, ethylene tar, and catalytic cracking clarified oil. Among these, anthracene oil, as an important fraction of coal tar, is one of the main raw materials for carbon black production. In recent years, with the increasing demands for purity and structural uniformity in carbon black from downstream industries such as rubber products, decrystalline anthracene oil has gradually gained industry attention. Decrystalline anthracene oil is a high-quality feedstock oil obtained by removing solid crystalline components such as anthracene, phenanthrene, and carbazole from ordinary anthracene oil through methods such as cooling crystallization and centrifugal separation. It has high aromatic content, low asphaltene and ash content, and advantages such as good fluidity, high reactivity, and low coking tendency, making it a preferred feedstock oil for high-end carbon black.

[0004] Existing reactors using decrystalline anthracene oil for carbon black production employ an oil furnace method. The feed oil lance is inserted radially into the reactor through a throat, with liquid oil droplets entering the throat from the lance outlet. However, the lance outlet is directly exposed to intense heat radiation and a highly reactive free radical environment exceeding 1400°C. The liquid oil droplets undergo thermal decomposition at the lance outlet face, gradually forming solid coke that blocks the outlet face. This prevents the feed oil from entering the throat normally, forcing frequent reactor shutdowns to clean the lance, severely limiting carbon black production efficiency. Furthermore, the atomization, vaporization, and decomposition processes all occur in the narrow throat region at high temperatures, with a high degree of spatial overlap. This can lead to some oil droplets solidifying into coke particles before complete vaporization, or a non-uniform reaction state where the surface is decomposed while the center remains liquid. Ultimately, this results in carbon black products with poor structural uniformity and high impurity content. Summary of the Invention

[0005] Therefore, it is necessary to provide a reactor for producing carbon black based on decrystalline anthracene oil to address the above-mentioned technical problems. This reactor can avoid coking at the outlet end face of the raw material oil spray gun, thereby improving production efficiency and enhancing the structural uniformity of the carbon black product while reducing impurity content.

[0006] This invention provides a reactor for producing carbon black based on decrystalline anthracene oil, comprising a combustion section, a throat, a reaction section, a quenching section, and a residence section that are fixedly connected along the axial direction. And multiple pre-vaporization components that utilize the waste heat of flue gas in the residence section to vaporize the feedstock oil; The pre-vaporization components include the flue gas main, vaporizer, and feed oil injection pipe; The inlet end of the flue gas main is connected to the residence section, the outlet end of the raw material oil spray pipe is connected to the throat pipe, and the outlet direction of the raw material oil spray pipe is perpendicular to the axis of the throat pipe. The vaporizer is used to heat the feed oil entering the vaporizer by using the waste heat of the flue gas in the residence section, and vaporize the feed oil into gaseous hydrocarbons. The vaporizer includes a shell-and-tube heat exchanger, a feed pipe, a discharge pipe, an inlet pipe, and an outlet pipe. The feed pipe and the discharge pipe are connected to both ends of the tube side of the shell-and-tube heat exchanger, and the inlet pipe and the outlet pipe are connected to both ends of the shell side of the shell-and-tube heat exchanger. The feed pipe is used to introduce decrystalline anthracene oil. The feed end of the raw material oil spray pipe is connected to the discharge pipe. The air inlet pipe is connected to the air outlet end of the flue gas main pipe. The air outlet pipe is used to introduce the heat-exchanged flue gas into the waste heat boiler.

[0007] In one embodiment, the feed oil spray pipe includes an inner pipe and an outer pipe of equal length, the outer pipe is sleeved outside the inner pipe, and the axes of the inner pipe and the outer pipe are collinear. The inner pipe is used to transport gaseous hydrocarbons, and the outer pipe is used to heat and insulate the inner pipe. The inner diameter of the inner tube is 2 to 3 times the difference between the inner and outer tube diameters, and the outer wall of the inner tube is coated with a heat insulation layer. At the feed end of the raw oil spray pipe, the inner and outer pipes are fixedly connected by an annular end cap; The outer diameter of the annular end cap is equal to the inner diameter of the outer tube, and the inner diameter of the annular end cap is equal to the outer diameter of the inner tube; the annular end cap is fitted onto the inner tube, and the outer tube is fitted onto the annular end cap. The inner pipe is connected to the discharge pipe. The pre-vaporization component also includes a first flue gas branch pipe and a second flue gas branch pipe. The inlet ends of the first flue gas branch pipe and the second flue gas branch pipe are both connected to the outlet end of the main flue gas pipe. The outlet end of the first flue gas branch pipe is connected to the inlet pipe. The outlet end of the second flue gas branch pipe is connected to the feed end of the raw material oil spray pipe and is connected to the outer pipe.

[0008] In one embodiment, the feed pipe is connected to a mixer, and the outlet of the mixer is connected to the feed pipe; The mixer is equipped with two feed pipes, which are used to feed preheated raw oil and high-pressure steam into the mixer respectively. The temperature of the preheated raw oil is 250℃~280℃, and the pressure of the high-pressure steam is 3Mpa~4Mpa.

[0009] In one embodiment, the main flue gas pipe is provided with a first flow regulating valve, the first flue gas branch pipe is provided with a second flow regulating valve, the second flue gas branch pipe is provided with a third flow regulating valve, and the discharge pipe is provided with a fourth flow regulating valve. The first, second, third, and fourth flow control valves can work together to control the real-time flow in their respective pipelines to maintain the temperature of the gaseous hydrocarbons at the outlet pipe at 390℃~450℃.

[0010] In one embodiment, the combustion section, reaction section, quenching section, and residence section are all cylindrical, and the axial diameter of the combustion section, reaction section, quenching section, and residence section is equal to the end face diameter of the throat. The end of the combustion section away from the throat pipe has a sealing cap with N natural gas passages, where N is greater than or equal to 3. The centers of the radial cross-sections of the N natural gas passages are located on the same circle, and the N natural gas passages are evenly distributed around the axis of the combustion section. A ring-shaped natural gas pipe is installed on the side of the sealing cap away from the throat pipe, and each natural gas through hole is connected to the ring-shaped natural gas pipe through a pipeline.

[0011] In one embodiment, the sidewall of the combustion section is provided with an air passage equal to the number of natural gas passages, and all air passages are evenly distributed circumferentially around the axis of the combustion section. Each air vent is connected to an air delivery pipe for supplying preheated air at the end furthest from the combustion section axis.

[0012] In one embodiment, the main flue gas pipe, the first flue gas branch pipe, and the second flue gas branch pipe are connected by a three-way valve.

[0013] In one embodiment, a feed pipe for conveying preheated feed oil into the mixer is defined as a first feed pipe, and a feed pipe for conveying high-pressure steam into the mixer is defined as a second feed pipe. The diameter ratio of the first feed pipe to the second feed pipe is 3:5 to 3:8. The feed oil flow velocity inside the first feed pipe is 1 m / s to 2 m / s, and the high-pressure steam flow velocity inside the second feed pipe is 20 m / s to 40 m / s.

[0014] In one embodiment, the quench section is provided with at least one quench assembly for spraying cooling water into the quench section. The quench assembly includes a quench pipe and a nozzle. The quench pipe is inserted into the quench section radially, and the nozzle is assembled at one end of the quench pipe located inside the quench section. The nozzle is located at the center of the radial cross-section of the quench section, and the nozzle sprays water towards the residence section.

[0015] The beneficial effects of this invention are: (1) By setting up a pre-vaporization component, the waste heat of the high-temperature flue gas in the residence section is recovered and used to indirectly heat and vaporize the decrystalline anthracene oil feedstock. The decrystalline anthracene oil is then radially injected into the throat in the form of gaseous hydrocarbons through the feedstock oil nozzle, eliminating the problem of high-temperature coking of liquid oil droplets at the nozzle outlet end face and avoiding frequent shutdowns due to blockage at the nozzle outlet end face, thus improving the carbon black production efficiency. At the same time, after the gaseous hydrocarbon form of the decrystalline anthracene oil is injected into the throat, it mixes rapidly with the high-temperature combustion flue gas. The vaporization and pyrolysis processes no longer overlap in the narrow throat area. The gaseous hydrocarbon form of the decrystalline anthracene oil is uniformly pyrolyzed in the reaction section, and the generated carbon black particles have high uniformity of structure and low impurity content. (2) The raw material oil spray pipe of the present invention adopts a double-layer structure with the inner pipe conveying gaseous hydrocarbon form decrystalline anthracene oil and the outer pipe passing in high-temperature flue gas for heating. Furthermore, the outer wall of the inner pipe is coated with a heat insulation layer, which effectively prevents the gaseous hydrocarbon from condensing prematurely due to heat dissipation during the conveying process, and also avoids the gaseous hydrocarbon form decrystalline anthracene oil from being further heated and spontaneously combusted. Attached Figure Description

[0016] Figure 1 This is a schematic diagram of the overall structure of the reactor for producing carbon black based on decrystalline anthracene oil, provided in an embodiment of the present invention. Figure 2 This is a schematic diagram of the vaporizer provided in an embodiment of the present invention; Figure 3 A schematic diagram of the radial cross-section of the raw oil spray pipe near the feed end provided in an embodiment of the present invention; Figure 4 A schematic diagram of the overall structure of a reactor for producing carbon black based on decrystalline anthracene oil is provided for another embodiment of the present invention; Figure 5 This is a schematic diagram showing the connection relationship between the vaporizer and the mixer provided in an embodiment of the present invention; Figure 6 A schematic diagram showing the distribution of natural gas holes and air pipes on the combustion section according to an embodiment of the present invention; Figure 7 This is a schematic diagram illustrating the assembly relationship between the quenching component and the quenching section provided in an embodiment of the present invention.

[0017] Explanation of reference numerals in the attached drawings: 10. Combustion section; 11. Sealing cap; 111. Natural gas through-hole; 12. Annular natural gas pipe; 13. Air delivery pipe; 20. Throat pipe; 30. Reaction section; 40. Quenching section; 41. Quenching assembly; 411. Quenching pipe; 412. Nozzle; 50. Residence section; 60. Main flue gas pipe; 61. First flue gas branch pipe; 62. Second flue gas branch pipe; 63. First flow regulating valve; 64. Second flow regulating valve; 65. Third flow regulating valve; 66. Fourth flow regulating valve; 70. Vaporizer; 71. Shell-and-tube heat exchanger; 72. Feed pipe; 73. Discharge pipe; 74. Air inlet pipe; 75. Air outlet pipe; 80. Raw material oil spray pipe; 81. Inner pipe; 82. Outer pipe; 83. Insulation layer; 84. Annular end cap; 90. Mixer; 91. First feed pipe; 92. Second feed pipe. Detailed Implementation

[0018] To make the above-mentioned objects, features and advantages of the present invention more apparent and understandable, the specific embodiments of the present invention will be described in detail below with reference to the accompanying drawings.

[0019] It should be noted that in the description of this invention, "upper," "lower," "top," "bottom," and orientation or positional relationship are based on the appendix. Figure 1 The orientations or positional relationships shown are for the convenience of describing the present invention and simplifying the description, and are not intended to indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as limiting the present invention.

[0020] In one embodiment, such as Figure 1 As shown, the reactor for producing carbon black based on decrystalline anthracene oil in this embodiment includes a combustion section 10, a throat 20, a reaction section 30, a quench section 40, and a residence section 50, which are fixedly connected along the axial direction. The combustion section 10, reaction section 30, quench section 40, and residence section 50 are all cylindrical, and the axial diameter of each section is equal to the end diameter of the throat 20, thus forming a smooth flow channel within the reactor, which is beneficial for the stable flow of high-temperature flue gas and reactants.

[0021] The reactor in this embodiment also includes multiple sets of pre-vaporization components that utilize the waste heat of flue gas in the residence section 50 to vaporize the feedstock oil. Two symmetrical pre-vaporization components are shown in the figure as an example. In practice, multiple sets of pre-vaporization components can be evenly arranged around the circumference of the reactor.

[0022] Specifically, the pre-vaporization assembly includes a main flue gas pipe 60, a vaporizer 70, and a feed oil spray pipe 80. The inlet end of the main flue gas pipe 60 is connected to the residence section 50, which is used to extract a portion of high-temperature flue gas from the residence section 50. The flue gas temperature in the residence section 50 is typically above 700°C.

[0023] The vaporizer 70 utilizes the waste heat of the high-temperature flue gas from the residence section 50 as a heat source to heat the decrystalline anthracene oil, which is used as feedstock, through heat exchange, vaporizing the decrystalline anthracene oil into gaseous hydrocarbons. For example... Figure 2 As shown, the vaporizer 70 specifically includes a shell-and-tube heat exchanger 71, a feed pipe 72, a discharge pipe 73, an air inlet pipe 74, and an air outlet pipe 75. The feed pipe 72 and the discharge pipe 73 are respectively connected to both ends of the tube side of the shell-and-tube heat exchanger 71, and the air inlet pipe 74 and the air outlet pipe 75 are respectively connected to both ends of the shell side of the shell-and-tube heat exchanger 71.

[0024] Feed pipe 72 is used to introduce decrystalline anthracene oil, which flows in the tube side and is heated to gaseous hydrocarbon form by the high-temperature flue gas in the shell side. The feed end of feed oil nozzle 80 is connected to discharge pipe 73. Inlet pipe 74 is connected to outlet end of flue gas main 60. High-temperature flue gas flows through the shell side of shell-and-tube heat exchanger 71. Outlet pipe 75 is used to introduce the heat-exchanged flue gas into waste heat boiler for further waste heat recovery. The discharge end of feed oil nozzle 80 is connected to throat 20. The discharge direction of feed oil nozzle 80 is perpendicular to the axis of throat 20, thereby ensuring that gaseous hydrocarbons are uniformly injected radially into the high-temperature flue gas mainstream of throat 20.

[0025] The reactor for producing carbon black from decrystalline anthracene oil in this embodiment employs a pre-vaporization component to indirectly heat and vaporize the decrystalline anthracene oil feedstock. This allows the decrystalline anthracene oil to be radially injected into the throat 20 in the form of gaseous hydrocarbons, eliminating the problem of high-temperature coking of liquid oil droplets at the nozzle outlet end face and improving carbon black production efficiency. Furthermore, by injecting the feedstock oil into the throat 20 in the form of gaseous hydrocarbons, the vaporization and cracking processes of the feedstock oil no longer overlap within the narrow throat 20. The gaseous hydrocarbon feedstock can be uniformly cracked within the reaction section 30, improving the uniformity of carbon black particle structure and reducing impurity content.

[0026] In one embodiment, such as Figure 3 As shown, the feedstock oil nozzle 80 includes an inner pipe 81 and an outer pipe 82 of equal length. The outer pipe 82 is sleeved outside the inner pipe 81, and the axes of the inner pipe 81 and the outer pipe 82 are collinear. The inner pipe 81 is used to transport gaseous hydrocarbons, and the outer pipe 82 is used to heat and insulate the inner pipe 81. The internal flow channel of the inner pipe 81 is used to transport gaseous hydrocarbons, and the annular interlayer between the outer pipe 82 and the inner pipe 81 is used to introduce high-temperature flue gas as a heat tracing medium to heat and insulate the inner pipe 81, preventing the gaseous hydrocarbons from partially condensing due to heat dissipation before being injected into the throat pipe 20.

[0027] The inner diameter of the inner tube 81 is 2 to 3 times the difference between the inner tube 81 and the outer tube 82, to ensure sufficient flow area in the inner tube 81 and maintain a suitable gaseous hydrocarbon flow rate without wasting the heat tracing medium. The outer wall of the inner tube 81 is coated with a heat insulation layer 83 to prevent the high-temperature flue gas, used as the heat tracing medium, from exchanging heat with the gaseous hydrocarbons flowing in the inner tube 81, which could further heat the gaseous hydrocarbons into decrystalline anthracene oil, causing it to spontaneously combust. The thickness of the heat insulation layer 83 includes, but is not limited to, 0.5 mm.

[0028] At the feed end of the raw material oil spray pipe 80, the inner pipe 81 and the outer pipe 82 are fixedly connected by an annular end cap 84. The outer diameter of the annular end cap 84 is equal to the inner diameter of the outer pipe 82, and the inner diameter of the annular end cap 84 is equal to the outer diameter of the inner pipe 81. The annular end cap 84 is fitted onto the inner pipe 81, and the outer pipe 82 is fitted onto the annular end cap 84. The three are tightly fixed together to form a seal and prevent leakage between the internal and external media.

[0029] In this embodiment, an inner pipe 81 is used to transport gaseous hydrocarbons, while an outer pipe 82 transports high-temperature flue gas with heat tracing. This effectively prevents the gaseous hydrocarbons from condensing prematurely due to heat dissipation during transport. The outer wall of the inner pipe 81 is coated with a heat insulation layer 83 to prevent the heat tracing medium from further heating the gaseous hydrocarbons into anthracene oil, causing them to decrystalline. For example, the heat insulation layer 83 can be made of ZS-855 anti-scorching, fire-resistant, and corrosion-resistant coating, applied to the outer wall of the inner pipe 81 using an endoscopic spraying method. This coating is non-stick, anti-scorching, and has good high-temperature oxidation resistance.

[0030] like Figure 4 As shown, in one embodiment, the inner tube 81 is connected to the discharge pipe 73. The pre-vaporization component also includes a first flue gas branch pipe 61 and a second flue gas branch pipe 62. The inlet ends of both the first flue gas branch pipe 61 and the second flue gas branch pipe 62 are connected to the outlet end of the main flue gas pipe 60. The outlet end of the first flue gas branch pipe 61 is connected to the inlet pipe 74, which is used to provide high-temperature flue gas for heating the shell-and-tube heat exchanger 71. The outlet end of the second flue gas branch pipe 62 is connected to the feed end of the raw material oil spray pipe 80 and is connected to the outer tube 82, thereby introducing a portion of the high-temperature flue gas into the annular jacket of the outer tube 82 to provide full-process heating for the inner tube 81. Specifically, the main flue gas pipe 60, the first flue gas branch pipe 61, and the second flue gas branch pipe 62 are connected by a three-way valve to achieve high-temperature flue gas diversion.

[0031] To further improve vaporization efficiency and suppress coking in the tube side, in one embodiment, the feed pipe 72 is connected to a mixer 90, and the outlet of the mixer 90 is connected to the feed pipe 72. Figure 5 As shown, the mixer 90 is equipped with two feed pipes, which are used to feed preheated raw oil and high-pressure steam into the mixer 90, respectively. In this embodiment, the temperature of the preheated raw oil is 250℃~280℃, and the pressure of the high-pressure steam is 3MPa~4MPa.

[0032] Specifically, the feed pipe for conveying preheated raw material oil into the mixer 90 is defined as the first feed pipe 91, and the feed pipe for conveying high-pressure steam into the mixer 90 is defined as the second feed pipe 92. The pipe diameter ratio of the first feed pipe 91 to the second feed pipe 92 is 3:5 to 3:8. The flow velocity of the raw material oil inside the first feed pipe 91 is 1 m / s to 2 m / s, and the flow velocity of the high-pressure steam inside the second feed pipe 92 is 20 m / s to 40 m / s.

[0033] It should be noted that the temperature of the preheated feed oil, the pressure of the high-pressure steam, the pipe diameter ratio of the first feed pipe 91 and the second feed pipe 92, the feed oil flow rate inside the first feed pipe 91, and the high-pressure steam flow rate inside the second feed pipe 92 can be specifically set according to the actual carbon black production requirements and the overall specifications of the reactor. The feed oil can be preheated through a feed oil preheater, which uses the waste heat generated by the waste heat boiler in the carbon black production system as a heat source.

[0034] In this embodiment, by setting up a mixer 90 to mix the preheated decrystalline anthracene oil with high-pressure steam before sending it into the tube side of the vaporizer 70, the dispersion and carrying effect of steam can not only reduce the partial pressure of the feed oil in the heat exchange tube and promote low-temperature vaporization, but also suppress the coking tendency of the decrystalline anthracene oil on the heated walls of the shell-and-tube heat exchanger 71 and the feed oil nozzle 80. At the same time, the steam, as a diluent, is beneficial to adjust the carbon black structure after entering the throat reaction area.

[0035] In one embodiment, to achieve precise control of the fluids in each pipe of the pre-vaporization component and to regulate the outlet temperature of the feed oil nozzle 80, this embodiment is equipped with a first flow regulating valve 63 in the main flue gas pipe 60, a second flow regulating valve 64 in the first flue gas branch pipe 61, a third flow regulating valve 65 in the second flue gas branch pipe 62, and a fourth flow regulating valve 66 in the discharge pipe 73. The first flow regulating valve 63, the second flow regulating valve 64, the third flow regulating valve 65, and the fourth flow regulating valve 66 can cooperate to control the real-time flow in their respective pipes to control the temperature of the gaseous hydrocarbons at the outlet of the discharge pipe 73 to be 390℃~450℃. At this temperature, the decrystalline anthracene oil is completely vaporized into gaseous hydrocarbons below its auto-ignition point.

[0036] In this embodiment, a temperature sensor is also installed between the fourth flow regulating valve 66 and the feed end of the feed oil nozzle 80 to detect the temperature of the gaseous hydrocarbons at the outlet of the discharge pipe 73. Simultaneously, the first flow regulating valve 63, the second flow regulating valve 64, the third flow regulating valve 65, and the fourth flow regulating valve 66 are all electrically controlled valves. They can be controlled by a PLC based on real-time data from the temperature sensor to adjust the opening of each valve, thereby regulating the flow rate of heating flue gas entering the shell side of the vaporizer 70, the flow rate of heating flue gas entering the outer pipe 82, and the supply flow rate of the gaseous hydrocarbon-form decrystalline anthracene oil. This ensures that the temperature of the gaseous hydrocarbon-form decrystalline anthracene oil at the outlet of the discharge pipe 73, and also at the outlet of the inner pipe 81 of the feed oil nozzle 80, is precisely controlled within the optimal pyrolysis preparation temperature range of 390℃ to 450℃. Furthermore, electrically controlled flow regulating valves can also be installed in the first feed pipe 91 and the second feed pipe 92, controlled by the same controller as the four flow regulating valves mentioned above.

[0037] Flow regulating valves are installed on the main flue gas pipe 60, the first flue gas branch pipe 61, the second flue gas branch pipe 62, and the discharge pipe 73, respectively, to achieve independent and coordinated control of the heating flue gas volume, the heat-tracing flue gas volume, and the gaseous hydrocarbon delivery volume of the vaporizer 70. This can accurately regulate the gaseous hydrocarbon temperature at the outlet of the raw material oil spray pipe 80 to 390℃~450℃, preventing the gaseous hydrocarbon from undergoing premature oxidation and spontaneous combustion with trace amounts of oxygen inside the raw material oil spray pipe 80 or at the outlet.

[0038] In one embodiment, such as Figure 6 As shown, the end of the combustion section 10 away from the throat 20 has a sealing cap 11, which has N natural gas through holes 111, where N is greater than or equal to 3, for example... Figure 6 Four are shown in the image. The centers of the radial cross-sections of the N natural gas through holes 111 are located on the same circle, and the N natural gas through holes 111 are evenly distributed circumferentially around the axis of the combustion section 10. An annular natural gas pipe 12 is provided on the side of the sealing cap 11 away from the throat pipe 20, and each natural gas through hole 111 is connected to the annular natural gas pipe 12 through a pipe.

[0039] Correspondingly, the sidewall of the combustion section 10 has an equal number of air passages as the natural gas passages 111, and all air passages are evenly distributed circumferentially around the axis of the combustion section 10. Each air passage is connected to an air delivery pipe 13 for delivering preheated air at the end furthest from the axis of the combustion section 10.

[0040] The combustion section 10 end face is equipped with multiple natural gas through holes 111 evenly distributed in the circumference, and is combined with preheated air through holes evenly arranged in the circumference of the side wall. This allows the natural gas and preheated air to form a uniform and stable swirling combustion flame in the combustion section 10, with a uniform combustion temperature field distribution. This makes the velocity field and temperature field of the generated high-temperature flue gas more consistent at the throat 20, providing good conditions for the rapid and uniform cracking of gaseous hydrocarbons, which is beneficial to improving the yield and quality of carbon black products.

[0041] like Figure 7 As shown, in one embodiment, the quench section 40 is provided with at least one quenching component 41 for injecting cooling water into the quench section 40 to quickly terminate the cracking reaction. Figure 7 The example shows two quenching components 41, but the actual number is determined based on the length of the quenching section. Each quenching component 41 includes a quenching pipe 411 and a nozzle 412. The quenching pipe 411 is inserted radially into the quenching section 40, and the nozzle 412 is fitted to one end of the quenching pipe 411 located inside the quenching section 40. The nozzle 412 is located at the center of the radial cross-section of the quenching section 40, and the spray direction of the nozzle 412 is towards the residence section 50. This allows the cooling water to mix and cool rapidly with the high-temperature reaction gas flow, while preventing cooling water backflow from affecting the high-temperature environment of the throat 20 and the reaction section 30.

[0042] The working process of the reactor for producing carbon black based on decrystalline anthracene oil of the present invention is as follows: Natural gas is uniformly injected into the combustion section 10 through the annular natural gas pipe 12 and various natural gas through-holes 111. Preheated air is simultaneously sent into the combustion section 10 through the air conveying pipe 13 and various air through-holes. The two are rapidly combusted in the combustion section 10, generating high-temperature flue gas with a temperature above 1400℃. The high-temperature flue gas flows sequentially through the throat pipe 20 and enters the reaction section 30. At the same time, the decrystalline anthracene oil, after being preheated to 250℃~280℃, is mixed at high speed with high-pressure steam of 3Mpa~4Mpa in the mixer 90, and then enters the tube side of the vaporizer 70. A portion of the high-temperature flue gas drawn from the residence section 50 through the flue gas main pipe 60 enters the shell side of the shell-and-tube heat exchanger 71 through the first flue gas branch pipe 61, heating the mixed raw materials in the tube side and completely vaporizing them into gaseous hydrocarbons at 390℃~450℃. The flue gas after heat exchange and cooling is sent to the waste heat boiler through the exhaust pipe 75. Another portion of the high-temperature flue gas is led from the second flue gas branch pipe 62 to the outer pipe 82 of the raw material oil spray pipe 80, forming a heat tracing jacket to ensure that the temperature of the gaseous hydrocarbons in the inner pipe 81 remains stable at 390℃~450℃ during transportation and spraying. The gaseous hydrocarbons are injected radially at high speed from the outlet end of the inner pipe 81 along the throat pipe 20, rapidly and uniformly mixed with the high-temperature flue gas flowing through the throat pipe 20, and enter the reaction section 30, where they are fully decomposed to generate carbon black under high-temperature conditions. The carbon black-containing flue gas after the reaction enters the quench section 40, where cooling water is sprayed from the nozzle 412 of the quench component 41 to quickly reduce the flue gas temperature below the reaction termination temperature. Subsequently, the flue gas enters the residence section 50 for further cooling, while a portion of the flue gas is extracted for the waste heat utilization of the pre-vaporization component, and the remaining flue gas is discharged to subsequent equipment such as the air preheater. Throughout the process, since the feedstock oil is injected into the throat 20 in the form of gaseous hydrocarbons, the phenomenon of coking of liquid oil droplets on the high-temperature end face of the feedstock oil nozzle outlet is avoided, which significantly extends the continuous operation cycle of the unit. Furthermore, the pyrolysis reaction of the gaseous feedstock is more uniform, and the produced carbon black product has high structural uniformity and low impurity content, making it particularly suitable for preparing high-end carbon black products using decrystalline anthracene oil.

[0043] It should be noted that, generally, once a carbon black production reactor is started, it does not stop under normal production conditions. In the initial startup phase of the carbon black production reactor based on decrystalline anthracene oil of this invention, raw materials are not supplied to the first feed pipe 91 and the second feed pipe 92. After the high-temperature flue gas combustion conditions and the cooling conditions of the quench section 40 within the entire reactor stabilize, the pre-vaporization component is activated and raw materials are supplied.

[0044] The embodiments described above are merely illustrative of several implementations of the present invention, and while the descriptions are specific and detailed, they should not be construed as limiting the scope of the present invention. It should be noted that those skilled in the art can make various modifications and improvements without departing from the concept of the present invention, and these modifications and improvements all fall within the scope of protection of the present invention. Therefore, the scope of protection of the present invention should be determined by the appended claims.

Claims

1. A reactor for producing carbon black based on decrystalline anthracene oil, characterized in that, It includes a combustion section (10), a throat (20), a reaction section (30), a quenching section (40), and a residence section (50) that are fixedly connected along the axial direction. And multiple pre-vaporization components that utilize the waste heat of flue gas in the residence section (50) to vaporize the raw material oil; The prevaporization assembly includes a flue gas main (60), a vaporizer (70), and a feed oil spray pipe (80); The inlet end of the flue gas main pipe (60) is connected to the residence section (50), the outlet end of the raw material oil spray pipe (80) is connected to the throat pipe (20), and the outlet direction of the raw material oil spray pipe (80) is perpendicular to the axis of the throat pipe (20). The vaporizer (70) is used to heat the raw oil entering the vaporizer (70) by using the waste heat of the flue gas in the residence section (50) to vaporize the raw oil into gaseous hydrocarbons. The vaporizer (70) includes a shell-and-tube heat exchanger (71), a feed pipe (72), a discharge pipe (73), an air inlet pipe (74), and an air outlet pipe (75). The feed pipe (72) and the discharge pipe (73) are respectively connected to the two ends of the tube side of the shell-and-tube heat exchanger (71), and the air inlet pipe (74) and the air outlet pipe (75) are respectively connected to the two ends of the shell side of the shell-and-tube heat exchanger (71). The feed pipe (72) is used to introduce decrystalline anthracene oil. The feed end of the raw material oil spray pipe (80) is connected to the discharge pipe (73). The air inlet pipe (74) is connected to the air outlet end of the flue gas main pipe (60). The air outlet pipe (75) is used to introduce the heat-exchanged flue gas into the waste heat boiler.

2. The reactor for producing carbon black based on decrystalline anthracene oil according to claim 1, characterized in that, The raw material oil spray pipe (80) includes an inner pipe (81) and an outer pipe (82) of equal length. The outer pipe (82) is sleeved on the outside of the inner pipe (81), and the axes of the inner pipe (81) and the outer pipe (82) are collinear. The inner pipe (81) is used to transport gaseous hydrocarbons, and the outer pipe (82) is used to heat and insulate the inner pipe (81). The inner diameter of the inner tube (81) is 2 to 3 times the difference between the inner tube (81) and the outer tube (82), and the outer wall of the inner tube (81) is coated with a heat insulation layer (83). At the feed end of the raw material oil spray pipe (80), the inner pipe (81) and the outer pipe (82) are fixedly connected by an annular end cap (84); The outer diameter of the annular end cap (84) is equal to the inner diameter of the outer tube (82), and the inner diameter of the annular end cap (84) is equal to the outer diameter of the inner tube (81); the annular end cap (84) is sleeved on the inner tube (81), and the outer tube (82) is sleeved on the annular end cap (84). The inner pipe (81) is connected to the discharge pipe (73). The pre-vaporization component also includes a first flue gas branch pipe (61) and a second flue gas branch pipe (62). The inlet ends of the first flue gas branch pipe (61) and the second flue gas branch pipe (62) are both connected to the outlet end of the main flue gas pipe (60). The outlet end of the first flue gas branch pipe (61) is connected to the inlet pipe (74). The outlet end of the second flue gas branch pipe (62) is connected to the feed end of the raw material oil spray pipe (80) and is connected to the outer pipe (82).

3. The reactor for producing carbon black based on decrystalline anthracene oil according to claim 2, characterized in that, The feed pipe (72) is connected to a mixer (90), and the outlet of the mixer (90) is connected to the feed pipe (72); The mixer (90) is provided with two feed pipes, which are used to feed preheated raw material oil and high-pressure steam into the mixer (90) respectively. The temperature of the preheated raw material oil is 250℃~280℃, and the pressure of the high-pressure steam is 3Mpa~4Mpa.

4. The reactor for producing carbon black based on decrystalline anthracene oil according to claim 3, characterized in that, The main flue gas pipe (60) is equipped with a first flow regulating valve (63), the first flue gas branch pipe (61) is equipped with a second flow regulating valve (64), the second flue gas branch pipe (62) is equipped with a third flow regulating valve (65), and the discharge pipe (73) is equipped with a fourth flow regulating valve (66). The first flow regulating valve (63), the second flow regulating valve (64), the third flow regulating valve (65) and the fourth flow regulating valve (66) can cooperate with each other to control the real-time flow in their respective pipelines so as to control the temperature of the gaseous hydrocarbon at the outlet of the discharge pipe (73) to be 390℃~450℃.

5. The reactor for producing carbon black based on decrystalline anthracene oil according to claim 4, characterized in that, The combustion section (10), reaction section (30), quenching section (40) and residence section (50) are all cylindrical, and the shaft diameter of the combustion section (10), reaction section (30), quenching section (40) and residence section (50) is equal to the end face diameter of the throat (20); The combustion section (10) has a sealing cap (11) at one end away from the throat (20). The sealing cap (11) has N natural gas through holes (111), where N is greater than or equal to 3. The centers of the radial cross-section circles of the N natural gas through holes (111) are located on the same circle, and the N natural gas through holes (111) are evenly distributed circumferentially around the axis of the combustion section (10). An annular natural gas pipe (12) is provided on the side of the sealing cap (11) away from the throat pipe (20), and each of the natural gas through holes (111) is connected to the annular natural gas pipe (12) through a pipe.

6. The reactor for producing carbon black based on decrystalline anthracene oil according to claim 5, characterized in that, The sidewall of the combustion section (10) is provided with an air passage equal in number to the natural gas passage (111), and all the air passages are evenly distributed around the axis of the combustion section (10). Each air vent is connected to an air delivery pipe (13) at the end furthest from the axis of the combustion section (10).

7. The reactor for producing carbon black based on decrystalline anthracene oil according to claim 2, characterized in that, The main flue gas pipe (60), the first flue gas branch pipe (61), and the second flue gas branch pipe (62) are connected by a three-way valve.

8. The reactor for producing carbon black based on decrystalline anthracene oil according to claim 3, characterized in that, The feed pipe used to deliver preheated raw material oil into the mixer (90) is defined as the first feed pipe (91), and the feed pipe used to deliver high-pressure steam into the mixer (90) is defined as the second feed pipe (92). The pipe diameter ratio of the first feed pipe (91) and the second feed pipe (92) is 3:5 to 3:

8. The flow velocity of the raw material oil inside the first feed pipe (91) is 1 m / s to 2 m / s, and the flow velocity of the high-pressure steam inside the second feed pipe (92) is 20 m / s to 40 m / s.

9. The reactor for producing carbon black based on decrystalline anthracene oil according to claim 6, characterized in that, The quench section (40) is provided with at least one quench assembly (41) for spraying cooling water into the quench section (40). The quench assembly (41) includes a quench pipe (411) and a nozzle (412). The quench pipe (411) is inserted into the quench section (40) radially, and the nozzle (412) is assembled at one end of the quench pipe (411) located inside the quench section (40). The nozzle (412) is located at the center of the radial cross-section circle of the quench section (40), and the water spraying direction of the nozzle (412) is towards the residence section (50).

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