Continuous hydrogenation apparatus and method

Abstract

This invention relates to the field of hydrogenation reaction technology, specifically to a continuous hydrogenation reaction apparatus and method, comprising a reactor shell, a feed tank, and a supplementary hydrogen compressor. A distribution system is installed within the reactor shell, including a distribution plate and an opening adjustment mechanism within the plate. Multiple catalyst modules are concentrically arranged within the reactor shell, dividing the reactor into a central reaction zone and an outer reaction zone. After purification by a high-pressure feed filter, the feed enters the reactor shell. Based on real-time feedback, the distribution system within the reactor shell distributes the mixed gas-liquid feed stream to the central and outer reaction zones in a specific ratio. Products from the central and outer reaction zones are combined and output. The entire system prioritizes light components and readily reactants in the central vertical tube zone for rapid, mass-transfer-controlled reactions, while guiding heavy components and less reactive substances to the outer annular gradient bed for deep, long-residence-time hydrogenation reactions.

Description

Technical Field

[0001] This invention relates to the field of hydrogenation reaction technology, and in particular to a continuous hydrogenation reaction apparatus and method. Background Technology

[0002] Hydrogenation reactors are core devices in industries such as chemical, petroleum refining, pharmaceutical, and food processing, enabling hydrogen to react with organic compounds in the presence of a catalyst. The core equipment, the hydrogenation reactor, typically operates under extremely harsh conditions of high temperature, high pressure, and proximity to hydrogen. Solid impurities carried in the raw materials, as well as polymers and salt deposits generated during the reaction, can easily clog the pores at the top of the catalyst bed, causing a rapid increase in reactor pressure drop and making continuous hydrogenation impossible.

[0003] In the prior art, patent CN116422244B discloses a high-efficiency and safe continuous hydrogenation reaction device, including an outer casing. Inside the outer casing, a diaphragm pump, a heat exchanger, a jet mixer, a tubular reactor, a cooler, a gas-liquid separator, and a buffer tank are installed. The outlet of the diaphragm pump is connected to the inlet of the heat exchanger, the outlet of the heat exchanger is connected to the inlet of the jet mixer, the outlet of the jet mixer is connected to the inlet of the tubular reactor, the outlet of the tubular reactor is connected to the inlet of the cooler, the outlet of the cooler is connected to the inlet of the gas-liquid separator, and the gas-liquid separator is connected to the buffer tank. The top of the jet mixer is a nozzle, the bottom of the nozzle is connected to an intake chamber, the bottom of the intake chamber is connected to a mixing section, and the bottom of the mixing section is connected to a diffuser section.

[0004] The above structure avoids the problem of separating liquid products from solid catalysts. However, in practical applications, it is not possible to carry out different hydrogenation reactions between light components and easily reactive substances, or between heavy components and difficult-to-react substances, which can easily increase the total pressure drop of the system. Summary of the Invention

[0005] In view of this, the purpose of this invention is to provide a continuous hydrogenation reaction apparatus and method to solve the problem that it is impossible to carry out different hydrogenation reactions of light components and easily reactive substances, and heavy components and difficult-to-react substances, and the total pressure drop of the system is easy to increase.

[0006] To achieve the above objectives, the present invention provides a continuous hydrogenation reaction apparatus, comprising a reactor shell, a feed tank, and a supplementary hydrogen compressor, wherein the reactor shell, the feed tank, and the supplementary hydrogen compressor are all connected by pipelines, and the outlets of the feed tank and the supplementary hydrogen compressor are both connected to a heating furnace. The reactor shell is equipped with a high-pressure raw material filter at the top for filtering raw materials, and the high-pressure raw material filter is connected to the outlet of the heating furnace. A gas-liquid separator is connected to the end of the reactor shell, and a circulating hydrogen compressor is connected to the top of the gas-liquid separator. The circulating hydrogen compressor is connected to the supplementary hydrogen compressor. The reactor shell is equipped with a distribution system, which includes a distribution plate and an opening adjustment mechanism inside the distribution plate. Multiple catalyst modules are concentrically arranged inside the reactor shell, which are divided into a central reaction zone and a peripheral reaction zone. A granular catalyst bed is arranged between the central reaction zone and the peripheral reaction zone, and the granular catalyst bed is gradient-filled. The opening adjustment mechanism can controllably distribute the raw material flow from the high-pressure raw material filter to the central reaction zone and the peripheral reaction zone.

[0007] Preferably, the opening adjustment mechanism includes multiple sets of risers slidably installed at the bottom of the distribution plate. The multiple sets of risers are arranged in a circumferential array. Gears are rotatably installed at the bottom of the multiple sets of risers. A nozzle is fixedly installed on one side of the gear. The nozzle is fixedly connected to the distribution plate through a hose. The riser has a toothed plate corresponding to the gear slidingly installed inside, and an inclined plate seat is fixedly installed on the top of the toothed plate. A drive mechanism is provided on one side of the toothed plate.

[0008] Preferably, a slide rail is fixedly installed at the bottom of the distribution plate, and multiple sets of fixing blocks are fixedly installed inside the slide rail. A telescopic rod is hinged between each pair of adjacent fixing blocks and the riser.

[0009] Preferably, the driving mechanism includes a drive motor fixedly positioned at the center of the bottom end of the distribution plate, the output end of the drive motor being fixedly connected to a disc, the disc having an arc-shaped groove inside, a push rod slidably mounted on the bottom of the distribution plate, and a protrusion corresponding to the arc-shaped groove being fixedly mounted on the bottom of the push rod.

[0010] Preferably, a sleeve is fixedly installed at the bottom of the distribution plate, a long rod is slidably installed inside the sleeve, and an electromagnet corresponding to the long rod is provided inside the sleeve. The electromagnet is connected to an external control system.

[0011] Preferably, the catalyst module includes multiple parallel central vertical DC channels and side vertical DC channels, and the interior of the central vertical DC channels and side vertical DC channels is filled with catalyst packing.

[0012] Preferably, the diameter of the central vertical DC channel is larger than the diameter of the side vertical DC channels, and the catalyst packing in the central and side vertical DC channels is functionally gradient distributed along the flow direction.

[0013] Preferably, the size of the catalyst particles in the peripheral reaction zone is smaller than the size of the catalyst packing material in the central reaction zone.

[0014] A continuous hydrogenation reaction method, applied to the aforementioned continuous hydrogenation reaction equipment, includes the following steps: S1. The raw materials are mixed with hydrogen through the raw material tank and then enter the heating furnace. After passing through the heating furnace, the raw materials enter the high-pressure raw material filter. After being purified by the high-pressure raw material filter, the raw materials enter the reactor shell. S2. The distribution system inside the reactor shell distributes the mixed gas-liquid feedstock flow to the central reaction zone and the peripheral reaction zone in a specific ratio based on real-time feedback. S3, light components and easily reacted substances mainly undergo rapid hydrogenation reactions in the vertical direct current channel of the central reaction zone, while heavy components and difficult-to-react substances mainly undergo deep hydrogenation reactions in the particulate catalyst bed of the peripheral reaction zone. S4. After the products from the central reaction zone and the peripheral reaction zone are combined, they are output. After output, the high-temperature and high-pressure products from the reactor are classified by a gas-liquid separator. The gas is repressurized by a circulating hydrogen compressor, mixed with fresh hydrogen, and returned to the reaction system to maintain the high hydrogen partial pressure of the system. Other reactants are discharged through the separator.

[0015] Preferably, in step S2, the real-time feedback includes at least one parameter based on the distillation range distribution, density, and aromatic content of the raw material; A heat extraction pipe is installed in the central reaction zone, and a quench hydrogen injection device is installed between the outer reaction zones. The heat extraction pipe integrated in the central reaction zone and the quench hydrogen injection device installed in the outer reaction zone enable independent and precise temperature control of the two reaction zones.

[0016] The beneficial effects of this invention are: The raw materials are mixed in the raw material tank and hydrogen is mixed in the supplementary hydrogen compressor and then enter the heating furnace. After passing through the heating furnace, the raw material enters the high-pressure raw material filter. After being purified by the high-pressure raw material filter, it enters the reactor shell. The distribution system in the reactor shell distributes the mixed gas-liquid raw material flow to the central reaction zone and the peripheral reaction zone in a specific ratio according to real-time feedback. The catalyst module in the reaction zone provides a large number of parallel straight and regular flow channels. The products from the central and peripheral reaction zones are combined and output. The high-temperature and high-pressure products from the reactor are sorted by a gas-liquid separator. The gas is repressurized by a circulating hydrogen compressor, mixed with fresh hydrogen, and returned to the reaction system. The system can preferentially guide light components and easily reactive substances to the central vertical pipe zone for rapid, mass-transfer-controlled reactions, while guiding heavy components and difficult-to-react substances to the peripheral annular gradient bed for deep, long-residence-time hydrogenation reactions. The total pressure drop of the system is significantly reduced, and the operating cycle is greatly extended. Attached Figure Description

[0017] To more clearly illustrate the technical solutions in this invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only for this invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0018] Figure 1 This is a three-dimensional structural diagram of the entire invention; Figure 2 This is a schematic diagram of the overall planar structure of the present invention; Figure 3 This is a schematic diagram of the internal structure of the reactor shell of the present invention; Figure 4 This is a three-dimensional structural diagram of the distribution disk of the present invention; Figure 5 This is a schematic diagram of the internal structure of the opening adjustment mechanism of the present invention; Figure 6 This is a schematic diagram of the internal structure of the drive mechanism of the present invention.

[0019] The components in the diagram are labeled as follows: 1. Reactor shell; 2. Circulating hydrogen compressor; 3. Heating furnace; 4. Raw material tank; 5. Gas-liquid separator; 6. Catalyst module; 61. Central vertical direct current channel; 62. Side vertical direct current channel; 7. Opening adjustment mechanism; 71. Riser; 72. Nozzle; 73. Fixing block; 74. Telescopic rod; 75. Gear; 76. Toothed plate; 77. Inclined seat; 78. Slide rail; 8. Inlet diffuser; 81. Drive motor; 82. Disc; 83. Top rod; 84. Arc groove; 85. Protruding column; 9. High-pressure raw material filter; 10. Distribution plate; 11. Supplementary hydrogen compressor; 12. Particulate catalyst bed; 13. Sleeve; 14. Long rod; 15. Electromagnet. Detailed Implementation

[0020] To make the objectives, technical solutions, and advantages of this invention clearer, the invention will be further described in detail below with reference to specific embodiments.

[0021] like Figure 1 , Figure 2 , Figure 3 , Figure 4 , Figure 5 and Figure 6 As shown, a continuous hydrogenation reaction device includes a reactor shell 1, a raw material tank 4, and a supplementary hydrogen compressor 11. The reactor shell 1, the raw material tank 4, and the supplementary hydrogen compressor 11 are all connected by pipelines. The outlets of the raw material tank 4 and the supplementary hydrogen compressor 11 are all connected to a heating furnace 4. A high-pressure raw material filter 9 for filtering raw materials is provided at the top of the reactor shell 1, and the high-pressure raw material filter 9 is connected to the outlet of the heating furnace 4. A gas-liquid separator 5 is connected to the end of the reactor shell 1, and a circulating hydrogen compressor 2 is connected to the top of the gas-liquid separator 5. The circulating hydrogen compressor 2 is connected to the supplementary hydrogen compressor 11. A distribution system is provided inside the reactor shell 1. The distribution system includes a distribution disk 10 and an opening adjustment mechanism 7 provided inside the distribution disk 10. Multiple catalyst modules 6 are concentrically arranged inside the reactor shell 1. The catalyst modules 6 are divided into a central reaction zone and an outer reaction zone. A granular catalyst bed 12 is provided between the central reaction zone and the outer reaction zone. The granular catalyst bed 12 is gradient-filled. The opening adjustment mechanism 7 can controllably distribute the raw material flow from the high-pressure raw material filter 9 to the central reaction zone and the peripheral reaction zone respectively.

[0022] In this embodiment, the raw materials are mixed through the raw material tank 4 and hydrogen is mixed through the supplementary hydrogen compressor 11 and then enter the heating furnace 3. After passing through the heating furnace 3, the raw materials enter the high-pressure raw material filter 9. After being purified by the high-pressure raw material filter 9, the raw materials enter the reactor shell 1. The distribution system inside the reactor shell 1 distributes the mixed gas-liquid raw material flow to the central reaction zone and the peripheral reaction zone in a specific ratio according to real-time feedback. The catalyst module 6 in the reaction zone provides a large number of parallel straight and regular flow channels. The products from the central and peripheral reaction zones are combined and output. The high-temperature and high-pressure products from the reactor are classified by the gas-liquid separator 5. The gas is repressurized by the circulating hydrogen compressor 2, mixed with fresh hydrogen, and returned to the reaction system. The system can preferentially guide light components and easily reactive substances to the central vertical pipe zone for rapid and mass-transfer controlled reactions, while guiding heavy components and difficult-to-react substances to the peripheral annular gradient bed for deep and long-term hydrogenation reactions. The total pressure drop of the system is significantly reduced and the operating cycle is greatly extended.

[0023] As one implementation method, such as Figure 4 , Figure 5 and Figure 6 As shown, the opening adjustment mechanism 7 includes multiple sets of risers 71 that are slidably installed at the bottom of the distribution plate 10. The multiple sets of risers 71 are arranged in a circumferential array. Gears 75 are rotatably installed at the bottom of the multiple sets of risers 71. A nozzle 72 is fixedly installed on one side of the gear 75. The nozzle 72 is fixedly connected to the distribution plate 10 through a hose. Inside the riser 71, a toothed plate 76 corresponding to the gear 75 is slidably installed. A sloping seat 77 is fixedly installed on the top of the toothed plate 76, and a drive mechanism is provided on one side of the toothed plate 76.

[0024] In this embodiment, when the drive mechanism drives the inclined seat 77 to move, the inclined seat 77 and the toothed plate 76 pull the riser 71 to move at the bottom of the distribution plate 10. By adjusting the extension and retraction of the nozzle 72 of the distribution plate 10, the processing load of the central reaction zone and the peripheral reaction zone can be dynamically adjusted. When the raw material becomes heavier, the feed ratio of the annular gap zone can be automatically increased without significantly adjusting the overall temperature, thereby maintaining stable product specifications and extending catalyst life.

[0025] As one implementation method, such as Figure 4 As shown, a slide rail 78 is fixedly installed at the bottom of the distribution plate 10. Multiple sets of fixing blocks 73 are fixedly installed inside the slide rail 78. Telescopic rods 74 are hinged between adjacent sets of fixing blocks 73 and the riser 71.

[0026] In this embodiment, when the drive mechanism drives the riser 71 to move at the bottom of the distribution plate 10, the telescopic rod 74 outside the riser 71 extends and retracts, and at the same time, with the connection of the fixing block 73, the stability of the nozzle 72 at the bottom of the riser 71 is improved.

[0027] As one implementation method, such as Figure 4 , Figure 5 and Figure 6 As shown, the driving mechanism includes a drive motor 81 fixedly positioned at the center of the bottom end of the distribution disk 10. The output end of the drive motor 81 is fixedly connected to a disc 82. An arc-shaped groove 84 is provided inside the disc 82. A push rod 83 is slidably mounted on the bottom of the distribution disk 10. A protrusion 85 corresponding to the arc-shaped groove 84 is fixedly mounted on the bottom of the push rod 83.

[0028] In this embodiment, when the drive motor 81 drives the disc 82 to rotate, the arc groove 84 inside the disc 82 rotates, which in turn drives the protrusion 85 and the push rod 83 to move telescopically at the bottom of the distribution disc 10. The push rod 83 drives the inclined seat 77 and the riser 71 outside the toothed plate 76 to move, thereby realizing the adjustable movement of the nozzle 72 and guiding the reactants to different areas, the central reaction area or the peripheral reaction area.

[0029] As one implementation method, such as Figure 4 , Figure 5 As shown, a sleeve 13 is fixedly installed at the bottom of the distribution plate 10. A long rod 14 is slidably installed inside the sleeve 13, and an electromagnet 15 corresponding to the long rod 14 is provided inside the sleeve 13. The electromagnet 15 is connected to an external control system.

[0030] In this embodiment, the magnetic poles generated by the electromagnet 15, connected to the external control system, drive the long rod 14. Since one side of the inclined seat 77 is restricted by the top rod 83, after the long rod 14 contacts the inclined surface of the inclined seat 77, it drives the toothed plate 76 to move downward. After the toothed plate 76 meshes with the gear 75, it changes the tilt angle of the nozzle 72. During the process of increasing or decreasing the flow rate of the entire reaction, the opening angle of all nozzles 72 is adjusted synchronously according to the proportion to contact the catalyst module 6, so as to maintain the optimal flow distribution at each point and maintain the distribution efficiency.

[0031] As one implementation method, such as Figure 2 , Figure 3 As shown, the catalyst module 6 includes multiple parallel central vertical DC channels 61 and side vertical DC channels 62, and the interior of the central vertical DC channels 61 and side vertical DC channels 62 is filled with catalyst packing.

[0032] The diameter of the central vertical DC channel 61 is larger than that of the side vertical DC channel 62, and the catalyst packing in the central vertical DC channel 61 and the side vertical DC channel 62 is distributed in a functional gradient along the flow direction.

[0033] In this embodiment, through adjustable distribution, readily reactive substances can be guided to the central vertical direct current channel 61 of the central tube bundle for rapid reaction; while difficult-to-react substances can be introduced into multiple side vertical direct current channels 62 for deep hydrogenation or long residence time reaction.

[0034] As one implementation method, such as Figure 1 , Figure 2 , Figure 3 As shown, the size of the catalyst particles in the outer reaction zone is smaller than the size of the catalyst packing material in the central reaction zone.

[0035] In this embodiment, the catalyst particles in the outer reaction zone can significantly reduce internal diffusion resistance and improve the volumetric efficiency of the catalyst. With the inclined distribution system guiding heavy components and difficult reactants to this area, the small particle catalyst can react more powerfully.

[0036] This specification also provides a continuous hydrogenation reaction method, including the following steps: S1. The raw materials are mixed through the raw material tank 4 and hydrogen is mixed through the supplementary hydrogen compressor 11 and then enter the heating furnace 3. After passing through the heating furnace 3, the raw materials enter the high-pressure raw material filter 9. After being purified by the high-pressure raw material filter 9, the raw materials enter the reactor shell 1. S2. The distribution system inside reactor shell 1 distributes the mixed gas-liquid raw material flow to the central reaction zone and the peripheral reaction zone in a specific ratio according to real-time feedback. S3, light components and easily reacted substances mainly undergo rapid hydrogenation reactions in the vertical direct current channel of the central reaction zone, while heavy components and difficult-to-react substances mainly undergo deep hydrogenation reactions in the particulate catalyst bed of the peripheral reaction zone. S4. The products from the central reaction zone and the peripheral reaction zone are combined and output. The high-temperature and high-pressure products from the reactor are classified by the gas-liquid separator 5. The gas is repressurized by the circulating hydrogen compressor 2, mixed with fresh hydrogen and returned to the reaction system to maintain the high hydrogen partial pressure of the system. Other reactants are discharged through the separator.

[0037] In step S2, the real-time feedback includes at least one parameter based on the distillation range distribution, density, and aromatic content of the raw material. A heat exchanger is installed in the central reaction zone, and a quench hydrogen injection device is installed between the outer reaction zones. The heat exchanger integrated in the central reaction zone and the quench hydrogen injection device installed in the outer reaction zone enable independent and precise temperature control of the two reaction zones.

[0038] Those skilled in the art should understand that the discussion of any of the above embodiments is merely exemplary and is not intended to imply that the scope of the invention (including the claims) is limited to these examples; within the framework of the invention, the technical features of the above embodiments or different embodiments can also be combined, the steps can be implemented in any order, and there are many other variations of the different aspects of the invention as described above, which are not provided in the details for the sake of brevity.

[0039] This invention is intended to cover all such substitutions, modifications, and variations that fall within the broad scope of the appended claims. Therefore, any omissions, modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of this invention should be included within the scope of protection of this invention.

Claims

1. A continuous hydrogenation reaction apparatus comprising a reactor housing (1), a raw material tank (4), and a make-up hydrogen compressor (11), which are connected by piping, characterized in that, The outlets of the raw material tank (4) and the supplementary hydrogen compressor (11) are both connected to a heating furnace (4). The reactor shell (1) is provided with a high-pressure raw material filter (9) for filtering raw materials at the top, and the high-pressure raw material filter (9) is connected to the outlet of the heating furnace (4). A gas-liquid separator (5) is connected to the end of the reactor shell (1), and a circulating hydrogen compressor (2) is connected to the top of the gas-liquid separator (5). The circulating hydrogen compressor (2) is connected to the supplementary hydrogen compressor (11). The reactor shell (1) is provided with a distribution system, which includes a distribution plate (10) and an opening adjustment mechanism (7) provided inside the distribution plate (10). Multiple catalyst modules (6) are concentrically arranged inside the reactor shell (1), which are divided into a central reaction zone and an outer reaction zone by the catalyst modules (6). A granular catalyst bed (12) is provided between the central reaction zone and the outer reaction zone. The granular catalyst bed (12) is gradient-filled. The opening adjustment mechanism (7) can controllably distribute the raw material flow from the high-pressure raw material filter (9) to the central reaction zone and the peripheral reaction zone respectively.

2. The continuous hydroprocessing apparatus of claim 1, wherein, The opening adjustment mechanism (7) includes multiple sets of risers (71) slidably installed at the bottom of the distribution plate (10). The multiple sets of risers (71) are arranged in a circular array. Gears (75) are rotatably installed at the bottom of the multiple sets of risers (71). A nozzle (72) is fixedly installed on one side of the gear (75). The nozzle (72) is fixedly connected to the distribution plate (10) through a hose. The riser (71) has a toothed plate (76) corresponding to the gear (75) slidably installed inside. A sloping seat (77) is fixedly installed on the top of the toothed plate (76), and a drive mechanism is provided on one side of the toothed plate (76).

3. The continuous hydrogenation reaction apparatus according to claim 2, characterized in that, The bottom of the distribution plate (10) is fixedly installed with a slide rail (78). Multiple sets of fixing blocks (73) are fixedly installed inside the slide rail (78). A telescopic rod (74) is hinged between each pair of adjacent fixing blocks (73) and the riser (71).

4. A continuous hydrogenation reaction apparatus according to claim 2, characterized in that, The driving mechanism includes a drive motor (81) fixedly positioned at the center of the bottom of the distribution plate (10). The output end of the drive motor (81) is fixedly connected to a disc (82). An arc groove (84) is provided inside the disc (82). A push rod (83) is slidably installed at the bottom of the distribution plate (10). A protrusion (85) corresponding to the arc groove (84) is fixedly installed at the bottom of the push rod (83).

5. A continuous hydrogenation reaction apparatus according to claim 1, characterized in that, A sleeve (13) is fixedly installed at the bottom of the distribution plate (10). A long rod (14) is slidably installed inside the sleeve (13), and an electromagnet (15) corresponding to the long rod (14) is provided inside the sleeve (13). The electromagnet (15) is connected to the external control system.

6. A continuous hydrogenation reaction apparatus according to claim 1, characterized in that, The catalyst module (6) includes multiple parallel central vertical DC channels (61) and side vertical DC channels (62), and the interior of the central vertical DC channels (61) and side vertical DC channels (62) is filled with catalyst packing.

7. A continuous hydrogenation reaction apparatus according to claim 6, characterized in that, The diameter of the central vertical DC channel (61) is larger than the diameter of the side vertical DC channel (62), and the catalyst packing in the central vertical DC channel (61) and the side vertical DC channel (62) is distributed in a functional gradient along the flow direction.

8. A continuous hydrogenation reaction apparatus according to claim 1, characterized in that, The size of the catalyst particles in the outer reaction zone is smaller than the size of the catalyst packing material in the central reaction zone.

9. A continuous hydrogenation reaction method, applied to the continuous hydrogenation reaction apparatus as described in any one of claims 1-8, characterized in that, Includes the following steps: S1. The raw material is mixed with the raw material tank (4) and the hydrogen is mixed with the supplementary hydrogen compressor (11) and then enters the heating furnace (3). After passing through the heating furnace (3), it enters the high-pressure raw material filter (9). After being purified by the high-pressure raw material filter (9), it enters the reactor shell (1). S2, The distribution system inside the reactor shell (1) distributes the mixed gas-liquid raw material flow to the central reaction zone and the peripheral reaction zone in a specific ratio according to real-time feedback; S3, light components and easily reacted substances mainly undergo rapid hydrogenation reactions in the vertical direct current channel of the central reaction zone, while heavy components and difficult-to-react substances mainly undergo deep hydrogenation reactions in the particulate catalyst bed of the peripheral reaction zone. S4. The products from the central reaction zone and the peripheral reaction zone are combined and output. After output, the high temperature and high pressure products from the reactor are classified by the gas-liquid separator (5). The gas is repressurized by the circulating hydrogen compressor (2), mixed with new hydrogen and returned to the reaction system to maintain the high hydrogen partial pressure of the system. Other reactants are discharged through the separator.

10. A continuous hydrogenation reaction method according to claim 1, characterized in that, In step S2, the real-time feedback includes at least one parameter based on the distillation range distribution, density, and aromatic content of the raw material. A heat extraction pipe is installed in the central reaction zone, and a quench hydrogen injection device is installed between the outer reaction zones. The heat extraction pipe integrated in the central reaction zone and the quench hydrogen injection device installed in the outer reaction zone enable independent and precise temperature control of the two reaction zones.

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