Internal circulation hydrogenation reactor and hydrogenation method for producing hydrogen peroxide by anthraquinone process

Abstract

The present invention provides an internal circulation hydrogenation reactor and a hydrogenation method for producing hydrogen peroxide by an anthraquinone process. The reactor comprises an outer cylinder and a middle cylinder arranged coaxially, and at least one inner cylinder arranged in the middle cylinder. Catalyst particles are filled in the inner cylinder. Anthraquinone working liquid and hydrogen enter the reactor from the bottom, contact and react in the inner cylinder. Driven by the working liquid and hydrogen, the catalyst and working liquid ascend to the top of the inner cylinder, then descend through the gap between the inner cylinder and the middle cylinder, and continue to undergo hydrogenation reaction under hydrogen supplementation. After reaching the bottom, part of the working liquid and catalyst flows back into the inner cylinder, and part of the working liquid ascends through the gap between the middle cylinder and the outer cylinder. Solid particles remaining in the working liquid precipitate during the upward movement of the liquid and flow back to the bottom of the inner cylinder, completing preliminary separation of solid and liquid. The separated working liquid is discharged through a liquid outlet at the top of the outer cylinder to form hydrogenated liquid. The reactor of the present invention adopts the form of an internal circulating fluidized bed to realize the anthraquinone hydrogenation reaction, which is conducive to the uniform mixing of the reaction materials and the catalyst, has good mass and heat transfer effects in the system, has few side reactions, and has high product quality. It can well solve the hot spot problem generated in the production process of the fixed bed hydrogenator.

Description

Technical Field

[0001] The present invention relates to a hydrogenation reactor, in particular to a reactor for realizing a hydrogenation reaction of anthraquinone to produce hydrogen peroxide through internal circulation, and a corresponding hydrogenation method. Background Art

[0002] Hydrogen peroxide is an important chemical widely used in fields such as medicine and environmental protection. The anthraquinone process is currently widely used for hydrogen peroxide production both domestically and internationally. This process uses anthraquinone derivatives as the working carrier. In the presence of a catalyst, the anthraquinone derivatives are hydrogenated to produce hydroanthraquinone, which is then oxidized to produce hydrogen peroxide and anthraquinone derivatives. Finally, hydrogen peroxide is extracted with water to obtain a desired concentration, and the anthraquinone derivatives are recycled as the working fluid. The efficiency of anthraquinone hydrogenation directly determines the yield and concentration of hydrogen peroxide and is a crucial step in the production process. Fluidized bed reactors are highly efficient chemical reactors, offering advantages such as fast reaction speed, uniform reaction, and excellent heat and mass transfer. Within a fluidized bed reactor, the working fluid, catalyst, and hydrogen gas are in full contact, increasing anthraquinone conversion and addressing uneven bed temperature distribution. This effectively improves reaction efficiency and yield, while reducing production costs. Newly built large-scale hydrogen peroxide production facilities abroad typically utilize fluidized beds for the hydrogenation reaction, achieving hydrogen efficiencies typically exceeding 12 g / L.

[0003] Patent US3423176A discloses a tubular suspended bed reactor for producing hydrogen peroxide by an anthraquinone process. The reactor consists of horizontal and vertical reaction tubes connected by elbows. A slit channel is formed in the reaction tube. In a venturi mixer, hydrogen and a material containing a catalyst are pre-mixed and then enter the slit channel from the bottom of the reaction tube for suspension hydrogenation. The hydrogenation efficiency can reach 12g / L. Patent CN104549059A discloses a slurry bed reactor for producing hydrogen peroxide by an anthraquinone process and its application. It adopts a slurry bed reactor with an upper diameter expansion. The reaction effluent is filtered through a post-filter, the filtrate is discharged, and the catalyst is recycled. The hydrogen efficiency reaches 10g / L. The fluidized bed reactor has a uniform flow state inside, which can fully mix the catalyst with the working fluid, reduce the catalyst dosage, and has good mass and heat transfer performance. However, catalyst separation is difficult, and a filter device needs to be added later, which greatly increases the burden of the filtering equipment.

[0004] The reactor design that realizes online separation of catalysts and maintains good mass and heat transfer performance will greatly reduce the pressure of subsequent filtration, extend the operating cycle, and improve the stability of the reaction. Summary of the Invention

[0005] To address the shortcomings of the existing technology, the present invention provides an internal circulation hydrogenation reactor and hydrogenation method for producing hydrogen peroxide using the anthraquinone process. The reactor design allows for efficient catalyst precipitation and separation within the reactor, significantly reducing pressure on subsequent filtration equipment and catalyst filtration losses. The reactor allows for online catalyst unloading and addition, and exhibits excellent mass and heat transfer properties, improving hydrogenation efficiency and enabling long-term stable operation.

[0006] To achieve the above technical objectives, the first aspect of the present invention provides an internal circulation hydrogenation reactor for producing hydrogen peroxide by the anthraquinone process, comprising a coaxially arranged outer cylinder and a middle cylinder, and at least one inner cylinder arranged in the middle cylinder, the bottoms of the inner cylinder, the middle cylinder and the outer cylinder are connected, the tops of the outer cylinder and the middle cylinder are sealed together, at least one gas-liquid distribution plate is provided at the bottom of each inner cylinder, the gas-liquid distribution plate is connected to the mixed gas-liquid inlet, the upper end of the inner cylinder extends to the middle or upper part of the middle cylinder, the upper end opening is connected to the interior of the middle cylinder, several gas distribution plates are provided at the bottom between the inner cylinder and the middle cylinder, and are connected to the gas inlet; at least one exhaust port is provided at the top of the middle cylinder and the top between the middle cylinder and the outer cylinder, the top of the middle cylinder is provided with a solid feed port, the bottom between the middle cylinder and the outer cylinder is provided with a solid discharge port, and the upper part of the outer cylinder is provided with a liquid outlet.

[0007] Furthermore, the bottom end of the inner tube is lower than the bottom end of the middle tube.

[0008] Furthermore, the liquid outlet is also connected to a filtering device.

[0009] Furthermore, the ratio of the distance between the bottom end of the inner cylinder and the bottom end of the outer cylinder to the diameter of the inner cylinder is 1:0.3-2.

[0010] Furthermore, the gas distribution plates are symmetrically distributed, or an annular gas distribution plate is provided.

[0011] Furthermore, a baffle with holes is provided on the upper portion of the middle tube and above the reaction zone of the inner tube to prevent solids in the inner tube from entering the upper outlet. Preferably, the baffle is an inverted V-shaped baffle.

[0012] Furthermore, a deflection baffle is provided at the front end of the liquid outlet so that the liquid material passes through the deflection baffle and is discharged from the liquid outlet.

[0013] Furthermore, the ratio of the distance from the deflection baffle to the inner wall of the outer cylinder to the distance from the outer wall of the middle cylinder to the inner wall of the outer cylinder is 1:1.5-10, and the ratio of the distance from the deflection baffle to the inner wall of the outer cylinder to the height of the deflection baffle is 1:2-15.

[0014] Furthermore, the bottoms of both the middle and inner tubes are provided with outward-facing flared baffles, with the angle between the flared baffles and the horizontal plane being 10°-80°, preferably 25°-70°. The ratio of the inner tube baffle length to the distance from the inner wall of the middle tube to the outer wall of the inner tube is 1:1.5-8, preferably 1:2-4. The ratio of the middle tube baffle length to the distance from the inner wall of the outer tube to the inner wall of the middle tube is 1:1.5-8, preferably 1:2-4.

[0015] Furthermore, the ratio of the outer cylinder diameter to the reactor height of the hydrogenation reactor is 1:1-30, preferably 1:3-12; the ratio of the cross-sectional area of ​​the outer cylinder to the cross-sectional area of ​​the middle cylinder is 100:20-90, preferably 100:30-70; the ratio of the cross-sectional area of ​​the middle cylinder to the cross-sectional area of ​​the inner cylinder is 100:9-64, preferably 100:16-50; and the ratio of the length of the middle cylinder to the length of the inner cylinder is 100:20-90, preferably 100:30-60.

[0016] The technical objective of the second aspect of the present invention is to provide a hydrogenation method for producing hydrogen peroxide by the anthraquinone method, using the above-mentioned reactor, with catalyst particles filled in the inner tube. The anthraquinone working liquid and hydrogen enter the reactor from the mixed gas-liquid inlet at the bottom, pass through the gas-liquid distribution plate, and enter the inner tube. The working liquid, hydrogen, and catalyst contact and react. Driven by the working liquid and hydrogen, the catalyst and working liquid ascend to the top of the inner tube, then descend through the gap between the inner tube and the middle tube, and continue the hydrogenation reaction under the hydrogen supplemented by the gas distribution plate between the middle tube and the outer tube. After reaching the bottom, part of the working liquid and catalyst flows back to the inner tube, and part of the working liquid ascends through the gap between the middle tube and the outer tube. The solid particles remaining in the working liquid precipitate during the liquid's upward movement and flow back to the bottom of the inner tube, completing the initial separation of solid and liquid. The separated working liquid is discharged through the liquid outlet at the top of the outer tube, i.e., the hydrogenated liquid.

[0017] Furthermore, based on the total volume of the middle cylinder, the loading amount of the catalyst particles is 20%-90%, preferably 30%-70%, and most preferably 35%-65%.

[0018] Furthermore, the catalyst used in the above method is a catalyst known in the art capable of achieving anthraquinone hydrogenation, and has an average particle size of 0.01 mm to 3.0 mm, preferably 0.1 mm to 1.5 mm, and most preferably 0.3 mm to 1.0 mm. Specifically, the above catalyst is generally a Group VIII metal supported on an inorganic refractory oxide.

[0019] Furthermore, when the loading amount of catalyst particles is ≥30%, overly fine catalysts will clog due to clumping. Therefore, the average particle size of the catalyst is not less than 0.5 mm. The catalyst in the reactor exists in both fluidized and mobile states, and the catalyst forms a moving bed between the inner tube and the middle tube. In this state, the catalyst filling amount is large and the precipitation and separation effect is good. When the loading amount of catalyst particles is not more than 30%, the fluid in the reactor can more easily achieve a fluidized state. There are no strict requirements on the average particle size range of the catalyst as mentioned above. The reactor is in a fluidized state as a whole, and the mass and heat transfer effects are good. However, the precipitation effect is worse than the former in this method, and the overall reaction is sensitive to pressure and has higher operating requirements. Considering the overall reaction efficiency, the catalyst particle loading amount is generally kept at a slightly higher level.

[0020] Furthermore, in the above method, the catalyst can be replaced online through the solid feed port at the top and the solid discharge port at the bottom.

[0021] Furthermore, in the above method, the reaction temperature of the inner barrel of the reactor is 30-80°C, preferably 40-60°C, and the pressure in the inner barrel is 0.15-0.55 MPa, preferably 0.2-0.3 MPa.

[0022] Furthermore, the hydrogenated liquid obtained by the reaction is filtered and then enters the subsequent oxidation unit and extraction and separation unit to obtain the product hydrogen peroxide and anthraquinone working solution. It should be understood by those skilled in the art that the hydrogenated liquid must be finely filtered multiple times before entering the oxidation unit to ensure that the amount of catalyst residue in the hydrogenated liquid meets the liquid feed requirements of the oxidation reaction before entering the oxidation unit.

[0023] Furthermore, the anthraquinone working solution is prepared by dissolving alkyl anthraquinone in an organic solvent, and a solvent system disclosed in the prior art can be used, such as anthraquinone derivatives, heavy aromatics (C10), trioctyl phosphate, etc.

[0024] The technical solution of the present invention has the following advantages:

[0025] (1) The reactor of the present invention adopts the form of an internal circulating fluidized bed to realize the anthraquinone hydrogenation reaction, which is conducive to the uniform mixing of the reactants and the catalyst. The mass and heat transfer effects in the system are good, the side reactions are few, and the product quality is high. It can well solve the hot spot problem generated in the production process of the fixed bed hydrogenator.

[0026] (2) The internal circulation hydrogenation reactor of the present invention adopts the method of bottom catalyst separation and upper liquid discharge. The catalyst is precipitated and separated at the bottom of the reactor, and the working liquid is discharged at the top of the reactor. The solid-liquid separation effect is good, which greatly reduces the burden on subsequent filters.

[0027] (3) The internal circulation hydrogenation reactor of the present invention can realize online replacement of the catalyst and extend the operation cycle of the device.

[0028] Other features and advantages of the present invention will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0029] Figure 1 Schematic diagram of the internal circulation hydrogenation reactor device of the present invention;

[0030] Figure 2 Schematic diagram of the catalyst and liquid flow state in the internal circulation hydrogenation reactor when the catalyst loading amount is high;

[0031] Figure 3 Schematic diagram of the catalyst and liquid flow state when the catalyst loading amount in the internal circulation hydrogenation reactor is high. DETAILED DESCRIPTION

[0032] The following non-limiting examples may enable those skilled in the art to more fully understand the present invention, but are not intended to limit the present invention in any way. Example 1

[0033] This embodiment provides an internal circulation hydrogenation reactor for producing hydrogen peroxide by anthraquinone method, such as Figure 1 As shown, it includes an outer cylinder 3 and a middle cylinder 2 arranged coaxially and an inner cylinder 1. The bottoms of the inner cylinder 1, the middle cylinder 2 and the outer cylinder 3 are connected. The tops of the outer cylinder 3 and the middle cylinder 2 are sealed together. The bottom of the inner cylinder 1 is lower than the bottom of the middle cylinder 2. A gas-liquid distribution plate 4 is set at the bottom of the inner cylinder 1. The gas-liquid distribution plate 4 is connected to the mixed gas-liquid inlet 301 opened on the outer cylinder 3. The upper end of the inner cylinder 1 extends to the upper middle part of the middle cylinder 2. The upper end opening is connected to the interior of the middle cylinder 2. An inverted V-shaped baffle 5 with an opening is set above the upper part of the middle cylinder 2 and the reaction zone of the inner cylinder 1. The bottom between the inner cylinder 1 and the middle cylinder 2 is set Gas distribution plate I6 and gas distribution plate II7 are connected to the air inlet; an exhaust port I201 is set at the top of the middle cylinder 2, an exhaust port II302 is set at the top between the middle cylinder 2 and the outer cylinder 3, the top of the middle cylinder 2 is also provided with a solid feed port 202, and a solid discharge port I331 and a solid discharge port II332 are set at the bottom between the middle cylinder 2 and the outer cylinder 3. Liquid outlet I311 and liquid outlet II312 are symmetrically provided on the upper part of the outer cylinder, and a deflection baffle I341 and a deflection baffle II342 are respectively provided at the front end thereof, and a filter I321 and a filter II322 are respectively connected at the rear end thereof. The bottoms of both the middle tube 2 and the inner tube 1 are provided with outward-facing trumpet-shaped baffles. The trumpet-shaped baffle of the inner tube 1 is at an angle of 45° to the horizontal plane, and the ratio of the baffle length to the distance from the inner wall of the middle tube 2 to the outer wall of the inner tube 1 is 1:2; the trumpet-shaped baffle of the middle tube 2 is at an angle of 60° to the horizontal plane, and the ratio of the baffle length to the distance from the inner wall of the outer tube 3 to the inner wall of the middle tube 2 is 1:2.5.

[0034] In the above reactor, the outer cylinder 3 has a diameter of 12 cm and a height of 70 cm. The ratio of the cross-sectional area of ​​the outer cylinder 3 to that of the middle cylinder 2 is 100:45, the ratio of the cross-sectional area of ​​the middle cylinder 2 to that of the inner cylinder 1 is 100:25, and the height ratio of the middle cylinder 2 to that of the inner cylinder 1 is 100:60. The distance between the bottom of the inner cylinder 1 and the bottom of the outer cylinder 3 is 2 cm.

[0035] Method for hydrogenating anthraquinone using the above internal circulation hydrogenation reactor:

[0036] The inner tube 1 is filled with catalyst particles, and the anthraquinone working liquid and hydrogen enter the reactor from the mixed gas-liquid inlet 301 at the bottom, and enter the inner tube 1 after passing through the gas-liquid distribution plate 4. The working liquid, hydrogen and catalyst contact and react. Driven by the working liquid and hydrogen, the catalyst and working liquid ascend to the top of the inner tube 1, and then descend through the gap between the inner tube 1 and the middle tube 2, and descend between the middle tube 2 and the outer tube 3. The hydrogenation reaction continues under the hydrogen supplemented by the gas distribution plate I6 and the gas distribution plate II7. The reacted gas is discharged through the exhaust port I201 and the exhaust port II302. After the reaction liquid reaches the bottom, the hydrogen and working liquid as feeds are quickly passed through the exhaust port I201 and the exhaust port II302 because the reaction is in progress. The liquid ascends through the inner cylinder 1, generating a low-pressure zone at the bottom of the inner cylinder 1. Part of the reaction liquid and catalyst at the bottom flows toward the low-pressure zone and flows back into the inner cylinder 1, thus realizing the circulation of the catalyst and part of the working liquid. The other part of the reaction liquid, under the action of the outlet pressure, ascends through the gap between the middle cylinder 2 and the outer cylinder 3. The catalyst particles remaining in the reaction liquid precipitate during the upward process of the liquid and flow back to the bottom of the inner cylinder 1, thus completing the preliminary separation of the solid and the liquid. The separated working liquid is discharged through the liquid outlet Ⅰ311 and the liquid outlet Ⅱ312 respectively through the outlet baffle Ⅰ341 and the outlet baffle Ⅱ342 on the upper part of the outer cylinder, and is preliminarily filtered through the filter Ⅰ321 and the filter Ⅱ322 to obtain the hydrogenated liquid.

[0037] During the above reaction process, the catalyst particles settle and flow back to the bottom of the outer tube 3, and participate in the reaction again under the drive of the feed. When the catalyst needs to be replaced, the solid discharge port I 331 and the solid discharge port II 332 are opened to allow the catalyst to flow out at a certain flow rate for online unloading, and online addition is carried out through the solid feed port 202 above the middle tube 2.

[0038] The resulting hydrogenated liquid undergoes multi-stage filtration before entering the oxidation reactor of the oxidation unit, where it reacts with oxygen to produce an oxidized liquid containing hydrogen peroxide. This oxidized liquid is then extracted and separated in an extraction unit to produce the product hydrogen peroxide and anthraquinone working solution. The extracted working solution is then dried, purified, and recycled.

[0039] The working solution used in the following examples is: 2-ethylanthraquinone and a solvent mixed in a volume ratio of 1:1, and the solvent is a heavy aromatic hydrocarbon and tetrabutyl urea mixed in a volume ratio of 3:1.

[0040] The catalyst is a supported catalyst of palladium on alumina, with a palladium loading of 5%. The carrier is spherical alumina with a specific surface area greater than 800m 2 / g. Example 2

[0041] Based on the total volume of the middle cylinder, the loading amount of the catalyst particles is 60% (when the loading amount is large), the average particle size of the catalyst is 0.5mm, and the flow state of the catalyst and liquid in the reactor is shown in the figure below. Figure 2 As shown, the catalyst particles exist in both fluidized and mobile states, and the catalyst forms a moving bed between the inner tube 1 and the middle tube 2. In this state, the catalyst filling amount is large and the sedimentation separation effect is good.

[0042] The reaction temperature in the hydrogenation reactor is 50°C, the pressure is 0.2 MPa, and the working liquid feed rate is 0.12 m 3 / h, the total hydrogen feed rate is 0.48Nm 3 / h.

[0043] The liquid after the reaction is first filtered through filter I 321 and filter II 322, and backwash is performed when the filter pressure difference is set to be greater than 0.1Mpa. The hydrogenated liquid after filtration is then subjected to secondary filtration to reduce its solid content to less than 5ppm. The filtered hydrogenated liquid enters the oxidation reactor with a reaction temperature of 50°C and a pressure of 0.2MPa. The oxidized product enters the extraction tower at 55°C with a pure water flow rate of 1.2m 3 After the reaction stabilized, the hydrogen efficiency was 13 gH2O2 / L.

[0044] The above-mentioned internal circulation hydrogenation reactor has a large internal circulation volume, which can effectively take away the reaction heat. At the same time, the catalyst particles are in a flowing state to avoid the occurrence of hot spots. The entire system is close to a fully mixed state, and the mass and heat transfer effects are good.

[0045] During the above reaction process, the catalyst is replaced through online unloading and adding at a rate of 50% per year. The above reactor can operate at a high temperature for a long period of time to achieve continuous production. Example 3

[0046] Based on the total volume of the middle cylinder, the loading amount of catalyst particles is 25% (when the loading amount is small), the average particle size of the catalyst is 0.3mm, and the flow state of the catalyst and liquid in the reactor is shown in the figure below. Figure 3 As shown, the reactor is in a fluidized state as a whole, with good mass and heat transfer effects and good precipitation and separation.

[0047] The reaction temperature in the hydrogenation reactor is 50°C, the pressure is 0.2 MPa, and the working liquid feed volume is 0.12 m 3 / h, the total hydrogen feed rate is 0.48Nm 3 / h.

[0048] The liquid after the reaction is first filtered through filter I 321 and filter II 322, and backwash is performed when the filter pressure difference is set to be greater than 0.1Mpa. The hydrogenated liquid after filtration is then subjected to secondary filtration to reduce its solid content to less than 5ppm. The filtered hydrogenated liquid enters the oxidation reactor with a reaction temperature of 50°C and a pressure of 0.2MPa. The oxidized product enters the extraction tower at 55°C with a pure water flow rate of 1.2m 3 / h for extraction treatment. After the reaction stabilized, the hydrogen efficiency of the reaction was 12gH2O2 / L.

[0049] During the above reaction process, the catalyst is replaced at a rate of 200% per year through online unloading and adding. The above reactor can operate at a high temperature for a long period of time to achieve continuous production.

Claims

1. An internal circulation hydrogenation reactor for producing hydrogen peroxide by anthraquinone process, characterized in that: It includes a coaxially arranged outer cylinder and a middle cylinder, and at least one inner cylinder arranged in the middle cylinder. The bottoms of the inner cylinder, the middle cylinder and the outer cylinder are connected, and the tops of the outer cylinder and the middle cylinder are sealed together. At least one gas-liquid distribution plate is set at the bottom of each inner cylinder, and the gas-liquid distribution plate is connected to the mixed gas-liquid inlet. The upper end of the inner cylinder extends to the middle or upper part of the middle cylinder, and the upper end opening is connected to the inside of the middle cylinder. Several gas distribution plates are set at the bottom between the inner cylinder and the middle cylinder and are connected to the air inlet; at least one exhaust port is set at the top of the middle cylinder and the top between the middle cylinder and the outer cylinder, the top of the middle cylinder is provided with a solid feed port, the bottom between the middle cylinder and the outer cylinder is provided with a solid discharge port, and the upper part of the outer cylinder is provided with a liquid outlet.

2. The internal circulation hydrogenation reactor according to claim 1, characterized in that The bottom end of the inner tube is lower than the bottom end of the middle tube.

3. The internal circulation hydrogenation reactor according to claim 1, characterized in that The ratio of the height difference between the bottom end of the inner cylinder and the bottom end of the outer cylinder to the diameter of the inner cylinder is 1:0.3-2.

4. The internal circulation hydrogenation reactor according to claim 1, characterized in that A baffle with holes is provided on the upper part of the middle cylinder and above the reaction zone of the inner cylinder to prevent solids in the inner cylinder from entering the upper outlet.

5. The internal circulation hydrogenation reactor according to claim 1, characterized in that The bottoms of the middle and inner tubes are both provided with outward trumpet-shaped baffles, the angle between the trumpet-shaped baffles and the horizontal plane is 10°-80°, the ratio of the length of the inner tube baffle to the distance from the inner wall of the middle tube to the outer wall of the inner tube is 1:1.5-8, and the ratio of the length of the middle tube baffle to the distance from the inner wall of the outer tube to the inner wall of the middle tube is 1:1.5-8.

6. The internal circulation hydrogenation reactor according to claim 1, characterized in that The ratio of the outer cylinder diameter of the hydrogenation reactor to the reactor height is 1:1-30, the ratio of the cross-sectional area of ​​the outer cylinder to the cross-sectional area of ​​the middle cylinder is 100:20-90, the ratio of the cross-sectional area of ​​the middle cylinder to the cross-sectional area of ​​the inner cylinder is 100:9-64, and the ratio of the length of the middle cylinder to the length of the inner cylinder is 100:20-90.

7. The internal circulation hydrogenation reactor according to claim 1, characterized in that A deflection baffle is also provided at the front end of the liquid outlet so that the liquid material passes through the deflection baffle and is discharged from the liquid outlet.

8. The internal circulation hydrogenation reactor according to claim 7, characterized in that The ratio of the distance from the deflection baffle to the inner wall of the outer cylinder to the distance from the outer wall of the middle cylinder to the inner wall of the outer cylinder is 1:1.5-10, and the ratio of the distance from the deflection baffle to the inner wall of the outer cylinder to the height of the deflection baffle is 1:2-15.

9. A hydrogenation method for producing hydrogen peroxide by an anthraquinone process, comprising: employing the internal circulation hydrogenation reactor according to any one of claims 1 to 8; wherein catalyst particles are filled in an inner cylinder; anthraquinone working fluid and hydrogen enter the reactor from a mixed gas-liquid inlet at the bottom, pass through a gas-liquid distribution plate, and enter the inner cylinder; the working fluid, hydrogen, and catalyst contact and react; driven by the working fluid and hydrogen, the catalyst and working fluid ascend to the top of the inner cylinder, then descend through the gap between the inner cylinder and the middle cylinder, and continue to undergo hydrogenation reaction under the hydrogen supplied between the middle cylinder and the outer cylinder via the gas distribution plate; upon reaching the bottom, part of the working fluid and catalyst refluxes into the inner cylinder, while part of the working fluid ascends through the gap between the middle cylinder and the outer cylinder; solid particles remaining in the working fluid precipitate during the upward movement of the liquid and reflux to the bottom of the inner cylinder, completing preliminary solid-liquid separation; and the separated working fluid is discharged through a liquid outlet at the top of the outer cylinder as hydrogenated liquid.

10. The hydrogenation method according to claim 9, characterized in that The filling amount of the catalyst particles is 20%-90% based on the total volume of the middle cylinder.

11. The hydrogenation method according to claim 9, characterized in that The average particle size of the catalyst particles is 0.01 mm to 3.0 mm.

12. The hydrogenation method according to claim 11, characterized in that When the loading amount of catalyst particles is ≥30%, the average particle size of the catalyst is not less than 0.5mm.

13. The hydrogenation method according to claim 9, characterized in that The reaction temperature of the inner tube of the reactor is 30-80°C, and the pressure inside the inner tube is 0.15-0.55Mpa.

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