A catalytic reaction device for reducing acid consumption in isooctane production

Abstract

This invention discloses a catalytic reaction device for reducing acid consumption in isooctane production, comprising a reactor, a raw material processing unit, and a reactant processing unit. The reactor is equipped with a Venturi tube, which is connected to a mixture distribution pipe. Below the mixture distribution pipe is a distribution disk, below which is packing material. Below the packing material is an acid-hydrocarbon sedimentation and separation zone. The mixture distribution pipe is connected to the distribution disk. A first support seat is provided on the inner wall of the reactor, and a first support spring is mounted on the first support seat, abutting against the distribution disk. A first rotating shaft is located at the bottom of the distribution disk, with a rotation drive component at one end. A first vibrating cam is mounted on the first rotating shaft, abutting against the distribution disk. This invention uses the Venturi tube for premixing to avoid concentrated reaction heat, the vibration of the distribution disk to improve distribution uniformity, and the packing material to increase the specific surface area. These three elements work synergistically to solve the problems of high acid consumption, numerous side reactions, and low mass transfer efficiency in production.

Description

Technical Field

[0001] This utility model relates to the field of alkylation production technology, specifically to a catalytic reaction device for reducing acid consumption in isooctane production. Background Technology

[0002] Isooctane is an important fuel additive. When isooctane is produced by alkylation, the preparation operation needs to be completed in a corresponding preparation reactor. During the preparation of isooctane, sulfuric acid needs to be added as a catalyst for catalytic operation. Isooctane is produced by low-temperature liquid-phase reaction. When sulfuric acid is used as a catalyst, the uneven distribution of the liquid phase leads to "channeling" or "dead zones", resulting in concentrated reaction heat. This can easily lead to problems such as high acid consumption, many side reactions, and low mass transfer efficiency.

[0003] Chinese Patent Publication No. CN203764234U discloses an alkylation reactor, including a reaction vessel and a raw material inlet and a catalyst inlet located at the top of the reaction vessel. The interior of the reaction vessel, from top to bottom, includes a material distribution and mixing section, a reaction section, and a product separation section. This patent uses the material distribution and mixing section to distribute and mix the raw material and catalyst without a stirrer. Static packing is installed inside the reactor to enhance mass transfer at high olefin hourly space velocities, allowing sulfuric acid, olefin-rich materials, and isobutane-rich materials to enter the reactor for reaction. However, because the acid-hydrocarbon mixer in the material distribution and mixing section is statically mixed, uneven distribution is prone to occur, thus affecting the subsequent mass transfer effect and leading to high acid consumption. Utility Model Content

[0004] The main objective of this invention is to overcome the defects of the prior art and provide a catalytic reaction device for reducing acid consumption in isooctane production.

[0005] To achieve the above objectives, this utility model proposes a catalytic reaction device for reducing acid consumption in isooctane production, comprising a reactor, a raw material processing unit, and a reactant processing unit. A Venturi tube is provided at the top of the reactor. The mixing outlet end of the Venturi tube extends into the interior of the reactor and is horizontally connected to several mixing distribution pipes. A distribution plate is provided below the mixing distribution pipes, and several sets of packing are provided below the distribution plate. An acid-hydrocarbon sedimentation separation zone is provided below the packing. The mixing distribution pipes are connected to the distribution plate. The outlet end of the raw material processing unit is connected to the feed end of the Venturi tube. The reactant processing unit is connected to the acid-hydrocarbon sedimentation separation zone. A first support seat is provided on the inner wall of the reactor. A first support spring is provided on the first support seat. The top end of the first support spring abuts against the bottom surface of the distribution plate. A first rotating shaft is horizontally provided at the bottom of the distribution plate. A rotating drive component is provided at one end of the first rotating shaft. A first vibrating cam is provided on the first rotating shaft, and the first vibrating cam abuts against the bottom surface of the distribution plate.

[0006] In a further optimized technical solution, the feed end of the Venturi tube is equipped with a circulating acid inlet, a raw material inlet, and a circulating hydrocarbon inlet. The circulating acid inlet is connected to the acid outlet of the acid-hydrocarbon sedimentation and separation zone via an acid circulation pipe. The raw material inlet is connected to the raw material processing unit via a raw material pipe, and the circulating hydrocarbon inlet is connected to the reactant processing unit via a circulating hydrocarbon pipe. Premixing the reactants using the Venturi tube avoids the heat concentration caused by traditional direct feeding. Vibration of the distribution plate optimizes liquid phase dispersion and improves the uniformity of the mixture distribution. The packing provides a large specific surface area, promoting continuous contact and reaction between the acid and hydrocarbon phases. This effectively solves the problems of high acid consumption, numerous side reactions, and low mass transfer efficiency in isooctane production.

[0007] In a further optimized technical solution, an acid circulation pump is installed on the acid circulation pipe. The acid circulation pipe is connected to a waste acid discharge pipe, a new acid replenishment pipe, and an acid bypass pipe. The acid bypass pipe connects to the lower middle part of the acid-hydrocarbon settling and separation zone, and a filter is installed on the bypass pipe. By bypassing the venturi tube through the acid bypass pipe and the filter, a portion of the circulating acid is directly injected into the acid-hydrocarbon settling and separation zone for filtration and purification, preventing particulate matter generated during the reaction from clogging the packing material.

[0008] In a further optimized technical solution, the mixture distribution pipe is provided with several discharge connectors, and the distribution disc is provided with several inlet connectors corresponding to the discharge connectors. The discharge connectors are connected to the inlet connectors via connecting hoses. Connecting the mixture distribution pipe and the distribution disc via connecting hoses prevents vibration from the distribution disc from being transmitted to the mixture distribution pipe when it vibrates.

[0009] In a further optimized technical solution, the inner wall of the reactor is provided with a second support seat corresponding to several groups of packing materials. A second support spring is provided on the second support seat, and the top end of the second support spring abuts against the bottom surface of the packing material. A second rotating shaft is horizontally provided at the bottom of the several groups of packing materials. A second vibration cam is provided on the second rotating shaft, and the second vibration cam abuts against the bottom surface of the packing material. A transmission shaft perpendicular to the first rotating shaft is provided on the outer wall of the reactor. The transmission shaft is connected to the first and second rotating shafts respectively through multiple sets of bevel gears. By causing the packing material to vibrate, the adhesion of the sulfate ester polymer generated in the hydrocarbon reaction to the packing surface is disrupted, forcing the liquid to form a dynamic liquid film on the packing surface. This avoids "channeling" caused by local surface tension differences, prevents clogging, and increases the reaction rate.

[0010] In a further optimized technical solution, the raw material processing unit includes a hydrolysis tank, a desulfurization tank, a hydrogenation reactor, and a light hydrocarbon removal tower. The inlet of the hydrolysis tank is connected to an external C4 raw material source, the outlet of the hydrolysis tank is connected to the inlet of the desulfurization tank, the outlet of the desulfurization tank is connected to the inlet of the hydrogenation reactor, and a hydrogenation pipe is connected to the connecting pipeline. The outlet of the hydrogenation reactor is connected to the inlet of the light hydrocarbon removal tower, and the outlet of the light hydrocarbon removal tower is connected to the raw material pipeline. Through the synergistic action of the hydrolysis tank, the desulfurization tank, and the hydrogenation reactor, the raw material is desulfurized, achieving deep purification of the C4 raw material and reducing acid consumption in subsequent reactions.

[0011] In a further optimized technical solution, the top of the light hydrocarbon removal tower is connected to a reflux tank via a gas phase discharge pipe. A first condenser is connected to the gas phase discharge pipe. The bottom reflux port of the reflux tank is connected to the light hydrocarbon removal tower, and the non-condensable gas discharge port of the reflux tank is connected to an external fuel gas pipeline network. Maintaining a suitable reflux ratio within the reactor through the reflux tank enhances gas-liquid contact and improves the separation accuracy of light components.

[0012] In a further optimized technical solution, a hydrogen flash evaporator is installed on the raw material pipe. The hydrogen flash evaporator removes trace amounts of hydrogen that may dissolve in the liquid hydrocarbons in the raw material.

[0013] In a further optimized technical solution, the reactant processing unit includes a refrigeration compressor, a primary coalescer, and a secondary coalescer. The inlet of the refrigeration compressor is connected to the vaporization outlet of the acid-hydrocarbon settling and separation zone, and the outlet of the refrigeration compressor is connected to the circulating hydrocarbon pipe. The feed inlet of the primary coalescer is connected to the reactant outlet of the acid-hydrocarbon settling and separation zone, the hydrocarbon feed inlet of the primary coalescer is connected to the circulating hydrocarbon pipe, the reactant inlet of the primary coalescer is connected to the secondary coalescer, and the hydrocarbon feed inlet of the secondary coalescer is connected to an external fractionation device. A gas-liquid separator is provided in the acid-hydrocarbon settling and separation zone, and the gas phase outlet of the gas-liquid separator is connected to the vaporization outlet. The vaporized light hydrocarbon gas is pressurized, condensed, and cooled by heat exchange in the refrigeration compressor and then returned to the reactor as part of the circulating hydrocarbon, cooling the heat generated by the alkylation reaction, thereby achieving direct cooling of the reactor, effectively reducing the reaction temperature, reducing side reactions, and reducing acid consumption.

[0014] The beneficial effects of this invention include: premixing via a Venturi tube avoids the concentration of reaction heat caused by traditional direct feeding; vibration of the distribution disk optimizes liquid phase dispersion and improves the uniformity of the mixed liquid distribution; and the packing provides a huge specific surface area to promote continuous contact reaction between the acid and hydrocarbon phases. The synergistic effect of these three factors effectively solves the problems of high acid consumption, numerous side reactions, and low mass transfer efficiency in isooctane production. Attached Figure Description

[0015] Figure 1 This is an overall schematic diagram of the catalytic reaction device in an embodiment of this utility model.

[0016] Figure 2 This is a schematic diagram of the reactor section in an embodiment of this utility model.

[0017] Figure 3 This is a schematic diagram of the assembly of the distribution disc and the packing in an embodiment of this utility model.

[0018] Figure 4 This is a schematic diagram of the assembly of the Venturi tube and the distribution plate in an embodiment of this utility model.

[0019] Figure reference numerals: 1 Reactor; 101 First support; 102 First support spring; 103 Second support; 104 Second support spring; 2 Raw material processing unit; 201 Hydrolysis tank; 202 Desulfurization tank; 203 Hydrogenation reactor; 204 Light hydrocarbon removal tower; 205 Hydrogenation pipe; 206 Gas phase discharge pipe; 207 Reflux tank; 208 Non-condensable gas discharge port; 209 Hydrogen flash tank; 3 Reactant processing unit; 301 Refrigeration compressor; 302 Primary coalescer; 303 Secondary coalescer; 304 Gas-liquid separator; 4 Venturi tube; 401 Circulating acid inlet. ; 402 Raw material inlet; 403 Circulating hydrocarbon inlet; 5 Mixed material distribution pipe; 501 Discharge connector; 502 Connecting hose; 6 Distribution disc; 601 Feed connector; 7 Packing; 8 Acid-hydrocarbon settling and separation zone; 9 First rotating shaft; 10 Rotary drive component; 11 First vibrating cam; 12 Acid circulation pipe; 1201 Acid circulation pump; 1202 Waste acid discharge pipe; 1203 New acid replenishment pipe; 1204 Acid bypass pipe; 1205; 13 Raw material pipe; 14 Circulating hydrocarbon pipe; 15 Second rotating shaft; 16 Second vibrating cam; 17 Drive shaft; 18 Bevel gear set. Detailed Implementation

[0020] To make the technical problems, technical solutions, and beneficial effects of the embodiments of this utility model clearer, the present utility model will be further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the present utility model and are not intended to limit the present utility model.

[0021] It should be noted that when a component is referred to as "fixed to" or "set on" another component, it can be directly on or indirectly on that other component. When a component is referred to as "connected to" another component, it can be directly connected to or indirectly connected to that other component. Furthermore, a connection can be for both fixing and circuit connection purposes.

[0022] It should be understood that the terms "length", "width", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", and "outer" indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are only for the convenience of describing the embodiments of this utility model and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this utility model.

[0023] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of embodiments of this utility model, "a plurality of" means two or more, unless otherwise explicitly specified.

[0024] Please see Figures 1 to 4The catalytic reaction device for reducing acid consumption in isooctane production disclosed in this utility model includes a reactor 1, a raw material processing unit 2, and a reactant processing unit 3. The reactor 1 has a tank structure. A venturi tube 4 is vertically installed at the top of the reactor 1. The mixing outlet end of the venturi tube 4 extends into the interior of the reactor 1 and is horizontally connected to several mixing distribution pipes 5. A distribution plate 6 is installed below the mixing distribution pipes 5. Several sets of packing materials 7 are installed below the distribution plate 6. An acid-hydrocarbon sedimentation and separation zone 8 is installed below the packing materials 7. The mixing distribution pipes 5 are connected to the distribution plate 6. The outlet end of the raw material processing unit 2 is connected to the feed end of the venturi tube 4. The reactant processing unit 3 is connected to the acid-hydrocarbon sedimentation and separation zone 8. A first support seat 101 is installed on the inner wall of the reactor 1. A first support spring 102 is installed on the first support seat 101. The top end of the first support spring 102 abuts against the bottom surface of the distribution plate 6. The bottom of the distribution plate 6 is horizontal. A first rotating shaft 9 is provided, with a rotating drive component 10 at one end of the first rotating shaft 9. A first vibrating cam 11 is provided on the first rotating shaft 9, and the first vibrating cam 11 abuts against the bottom surface of the distribution disk 6. Specifically, the feed end of the venturi tube 4 is provided with a circulating acid inlet 401, a raw material suction inlet 402, and a circulating hydrocarbon suction inlet 403. The circulating acid inlet 401 is connected to the acid outlet at the bottom of the acid-hydrocarbon sedimentation and separation zone 8 through the acid circulation pipe 12. The raw material suction inlet 402 is connected to the raw material processing unit 2 through the raw material pipe 13. The circulating hydrocarbon suction inlet 403 is connected to the circulating hydrocarbon outlet of the reactant processing unit 3 through the circulating hydrocarbon pipe 14. The first vibrating cam 11 and the support beam at the bottom of the distribution disk 6 are made of stainless steel or copper alloy to avoid sparks generated by steel-to-steel friction. The rotation vibration frequency of the first vibrating cam 11 is ≤50Hz to avoid high surface temperature caused by high-speed rotation and to ensure that the explosion-proof requirements are met. The rotating drive component 10 is a motor.In this embodiment, the recycled acid recovered in the sedimentation separation zone 8, the C4 feedstock processed by the raw material processing unit 2, and the recycled hydrocarbon feedstock processed by the reactant processing unit 3 are premixed through the Venturi tube 4 to avoid acid-hydrocarbon stratification, concentrated reaction heat, and reduce side reactions caused by excessively high local acid concentration. The mixture enters the distribution plate 6 through the horizontally distributed mixture distribution pipe 5 for uniform distribution. The uniformly distributed mixture falls onto the packing 7 below and undergoes contact reaction on the packing 7. At the same time as the mixture enters the distribution plate 6, the first rotating shaft 9 is driven to rotate by the rotary drive component 10, which in turn drives the first vibrating cam 11 to drive the distribution plate 6 to produce micro-vibration, avoiding "channeling" or "dead zones" of the mixture on the distribution plate 6. The mixture is evenly distributed and falls onto the packing 7 below, covering the surface of the packing 7 to form a uniform film, which enhances the mass transfer effect of the reactants (mixture) and promotes full contact and reaction between the acid and hydrocarbon phases. The reaction products fall into the acid and hydrocarbon settling and separation zone 8 for preliminary separation. The separated acid and hydrocarbon mixture enters the reactant processing unit 3 for further separation. In this embodiment, the premixing of the Venturi tube 4 avoids the concentration of reaction heat caused by traditional direct feeding. The vibration of the distribution disk 6 optimizes the liquid phase dispersion and improves the uniformity of the mixture distribution. The packing 7 provides a huge specific surface area to promote continuous contact and reaction between the acid and hydrocarbon phases. The synergistic effect of the three can effectively solve the problems of high acid consumption, many side reactions and low mass transfer efficiency in isooctane production.

[0025] In a specific example, an acid circulation pump 1201 is installed on the acid circulation pipe 12. The acid circulation pipe 12 is connected to a waste acid discharge pipe 1202, a new acid replenishment pipe 1203, and an acid bypass pipe 1204. The acid bypass pipe 1204 connects to the lower middle part of the acid-hydrocarbon settling separation zone 8, and a filter 1205 is installed on the acid bypass pipe 1204. Through the acid bypass pipe 1204 and the filter 1205, a portion of the circulating acid bypasses the venturi tube 4 and is directly injected into the acid-hydrocarbon settling separation zone 8, forming an internal acid circulation system for filtering and purifying the circulating acid. This prevents particulate matter generated during the reaction from clogging the distribution plate 6 and the packing 7 during continuous circulation.

[0026] In a specific example, the mixture distribution pipe 5 is provided with several discharge connectors 501, and the distribution plate 6 is provided with several inlet connectors 601 corresponding to the discharge connectors 501. The discharge connectors 501 are connected to the inlet connectors 601 through connecting hoses 502. Connecting the mixture distribution pipe 5 and the distribution plate 6 through connecting hoses 502, instead of using a rigid connection, can effectively prevent vibration from the distribution plate 6 from being transmitted to the mixture distribution pipe 5 when it vibrates.

[0027] In a preferred embodiment, a second support seat 103 corresponding to several groups of packing 7 is provided on the inner wall of the reactor 1. A second support spring 104 is provided on the second support seat 103. The top end of the second support spring 104 abuts against the bottom surface of the packing 7. A second rotating shaft 15 is horizontally provided at the bottom of several groups of packing 7. A second vibration cam 16 is provided on the second rotating shaft 15. The second vibration cam 16 abuts against the bottom surface of the packing 7. A transmission shaft 17 perpendicular to the first rotating shaft 9 is provided on the outer wall of the reactor 1. The transmission shaft 17 is connected to the first rotating shaft 9 and the second rotating shaft 15 respectively through multiple sets of bevel gear sets 18. By introducing a vibration source at the bottom of the packing 7, the packing 7 also generates micro-vibration, which disrupts the adhesion of the sulfate ester polymer generated in the acid-hydrocarbon reaction to the surface of the packing 7, reducing the risk of packing 7 clogging; moreover, the vibration forces the liquid to form a dynamic liquid film on the surface of the packing 7, avoiding "channeling" caused by local surface tension differences, improving the reaction rate and reducing acid consumption; at the same time, the rotational power output by the rotational drive 10 is transmitted to each of the second rotational shafts 15 through the drive shaft 17, eliminating the need to add a power source and reducing costs.

[0028] In a preferred embodiment, the raw material processing unit 2 includes a hydrolysis tank 201, a desulfurization tank 202, a hydrogenation reactor 203, and a light hydrocarbon removal tower 204. The inlet of the hydrolysis tank 201 is connected to an external C4 raw material end, the outlet of the hydrolysis tank 201 is connected to the inlet of the desulfurization tank 202, the outlet of the desulfurization tank 202 is connected to the inlet of the hydrogenation reactor 203, and a hydrogenation pipe 205 is connected to the connected pipe. The outlet of the hydrogenation reactor 203 is connected to the inlet of the light hydrocarbon removal tower 204, and the outlet of the light hydrocarbon removal tower 204 is connected to the raw material pipe 13. The hydrolysis tank 201 contains JX-6B hydrolysis agent, and the desulfurization tank 202 contains NDS-2 desulfurizing agent. The C4 feedstock after etherification is converted into easily treatable H2S by the hydrolysis tank 201, and then removed by the desulfurization tank 202. It is then further desulfurized by the hydrogenation reactor 203, and the light hydrocarbon removal tower 204 removes C3 and below light hydrocarbons, so as to deeply purify the C4 feedstock and effectively reduce the acid consumption of subsequent reactions.

[0029] In a preferred embodiment, the top of the light hydrocarbon removal tower 204 is connected to the reflux tank 207 via a gas phase discharge pipe 206. A first condenser is connected to the gas phase discharge pipe 206. The reflux port at the bottom of the reflux tank 207 is connected to the light hydrocarbon removal tower 204. The non-condensable gas discharge port 208 of the reflux tank 207 is connected to an external fuel gas pipeline network. A hydrogen flash tank 209 is provided on the feed pipe 13. The reflux tank 207 maintains the reflux ratio in the reactor 1, enhances gas-liquid contact, improves the separation accuracy of light components, and prevents light components from entering the downstream and causing a decrease in product purity. The hydrogen flash tank 209 removes trace amounts of hydrogen that may dissolve in the liquid hydrocarbons in the feed pipe 13, preventing hydrogen from entering the reactor 1 and vaporizing, which could lead to abnormal pressure and equipment cavitation, thus ensuring the stability of the unit's operation.

[0030] In a preferred embodiment, the reactant processing unit 3 includes a refrigeration compressor 301, a primary coalescer 302, and a secondary coalescer 303. The inlet of the refrigeration compressor 301 is connected to the vaporization outlet of the acid-hydrocarbon settling and separation zone 8, and the outlet of the refrigeration compressor 301 is connected to the circulating hydrocarbon pipe 14. The feed inlet of the primary coalescer 302 is connected to the reactant outlet of the acid-hydrocarbon settling and separation zone 8, the hydrocarbon feed inlet of the primary coalescer 302 is connected to the circulating hydrocarbon pipe 14, the reactant inlet of the primary coalescer 302 is connected to the secondary coalescer 303, and the hydrocarbon feed inlet of the secondary coalescer 303 is connected to an external fractionation device. The gas-liquid separator 304 is installed in the acid hydrocarbon settling and separation zone 8. The gas phase outlet of the gas-liquid separator 304 is connected to the vaporization outlet. The vaporized light hydrocarbon gas is mainly isobutane, n-butane and propane. After being pressurized and condensed by the refrigeration compressor 301, it is then pressurized by the pump and cooled by heat exchange as part of the circulating hydrocarbon. The light hydrocarbon refrigeration and compression process is existing technology and will not be described in detail here. The light hydrocarbon refrigerant is returned to the reactor 1 to cool the heat generated by the alkylation reaction, thereby realizing the direct cooling of the reactor 1, which can effectively reduce the reaction temperature, reduce side reactions (reduce the amount of acid-soluble oil generated), and reduce acid consumption.

[0031] The above description, in conjunction with specific / preferred embodiments, provides a further detailed explanation of the present invention and should not be construed as limiting the specific implementation of the present invention to these descriptions. For those skilled in the art, various substitutions or modifications can be made to these described embodiments without departing from the concept of the present invention, and all such substitutions or modifications should be considered within the protection scope of the present invention. In the description of this specification, the reference to terms such as "an embodiment," "some embodiments," "preferred embodiment," "example," "specific example," or "some examples," etc., indicates that the specific feature, structure, material, or characteristic described in connection with that embodiment or example is included in at least one embodiment or example of the present invention. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the described specific features, structures, materials, or characteristics can be combined in a suitable manner in any one or more embodiments or examples. Without contradiction, those skilled in the art can combine and integrate the different embodiments or examples described in this specification and the features of different embodiments or examples. Although embodiments of the present invention and their advantages have been described in detail, it should be understood that various changes, substitutions and alterations may be made herein without departing from the scope of protection of the patent application.

Claims

1. A catalytic reaction apparatus for reducing the acid consumption in the production of isooctane, characterized by: The reactor comprises a reactor, a raw material processing unit, and a reactant processing unit. A Venturi tube is located at the top of the reactor, with its mixing outlet extending into the reactor and horizontally connected to several mixing distribution pipes. A distribution plate is located below the mixing distribution pipes, and several sets of packing are located below the distribution plate. An acid-hydrocarbon sedimentation separation zone is located below the packing. The mixing distribution pipes are connected to the distribution plate. The outlet of the raw material processing unit is connected to the inlet of the Venturi tube. The reactant processing unit is connected to the acid-hydrocarbon sedimentation separation zone. A first support base is located on the inner wall of the reactor, and a first support spring is mounted on the first support base. The top of the first support spring abuts against the bottom surface of the distribution plate. A first rotating shaft is horizontally located at the bottom of the distribution plate, with a rotating drive component at one end of the first rotating shaft. A first vibrating cam is mounted on the first rotating shaft, and the first vibrating cam abuts against the bottom surface of the distribution plate.

2. The catalytic reaction device for reducing acid consumption in isooctane production according to claim 1, characterized by: The venturi tube is provided with a circulating acid inlet, a raw material inlet, and a circulating hydrocarbon inlet at its feed end. The circulating acid inlet is connected to the acid outlet of the acid-hydrocarbon sedimentation and separation zone through an acid circulation pipe. The raw material inlet is connected to the raw material processing unit through a raw material pipe. The circulating hydrocarbon inlet is connected to the reactant processing unit through a circulating hydrocarbon pipe.

3. The catalytic reaction apparatus for reducing acid consumption in isooctane production as described in claim 2, characterized in that: An acid circulation pump is installed on the acid circulation pipe. A waste acid discharge pipe, a new acid replenishment pipe, and an acid bypass pipe are connected to the acid circulation pipe respectively. The acid bypass pipe is connected to the middle and lower part of the acid hydrocarbon sedimentation and separation zone. A filter is installed on the acid bypass pipe.

4. The catalytic reaction apparatus for reducing the acid consumption in isooctane production according to claim 3, characterized in that: The mixture distribution pipe is provided with several discharge connectors, and the distribution plate is provided with several inlet connectors corresponding to the discharge connectors. The discharge connectors are connected to the inlet connectors through connecting hoses.

5. The catalytic reaction apparatus for reducing the acid consumption in isooctane production according to claim 4, characterized in that: The reactor has a second support seat corresponding to several groups of packing materials on its inner wall. The second support seat has a second support spring, the top of which abuts against the bottom surface of the packing material. The bottom of several groups of packing materials is provided with a second rotating shaft, and the second rotating shaft has a second vibrating cam, which abuts against the bottom surface of the packing material. The reactor has a transmission shaft perpendicular to the first rotating shaft on its outer wall. The transmission shaft is connected to the first rotating shaft and the second rotating shaft respectively through multiple sets of bevel gears.

6. The catalytic reaction device for reducing the acid consumption in the production of isooctane according to any one of claims 2 to 5, characterized in that: The raw material processing unit includes a hydrolysis tank, a desulfurization tank, a hydrogenation reactor, and a light hydrocarbon removal tower. The inlet of the hydrolysis tank is connected to an external C4 raw material source. The outlet of the hydrolysis tank is connected to the inlet of the desulfurization tank. The outlet of the desulfurization tank is connected to the inlet of the hydrogenation reactor, and a hydrogenation pipe is connected to the connecting pipeline. The outlet of the hydrogenation reactor is connected to the inlet of the light hydrocarbon removal tower, and the outlet of the light hydrocarbon removal tower is connected to the raw material pipe.

7. The catalytic reaction apparatus for reducing the acid consumption in isooctane production according to claim 6, characterized by: The top of the light hydrocarbon removal tower is connected to the reflux tank via a gas phase discharge pipe. A first condenser is connected to the gas phase discharge pipe. The bottom reflux port of the reflux tank is connected to the light hydrocarbon removal tower. The non-condensable gas discharge port of the reflux tank is connected to the external fuel gas pipeline network.

8. The catalytic reaction apparatus for reducing the acid consumption in isooctane production according to claim 7, characterized by: The raw material pipe is equipped with a hydrogen flash evaporator.

9. The catalytic reaction apparatus for reducing acid consumption in isooctane production as described in claim 6, characterized in that: The reactant processing unit includes a refrigeration compressor, a primary coalescer, and a secondary coalescer. The inlet of the refrigeration compressor is connected to the vaporization outlet of the acid-hydrocarbon settling and separation zone, and the outlet of the refrigeration compressor is connected to the circulating hydrocarbon pipe. The feed inlet of the primary coalescer is connected to the reactant outlet of the acid-hydrocarbon settling and separation zone, the hydrocarbon feed inlet of the primary coalescer is connected to the circulating hydrocarbon pipe, the reactant inlet of the primary coalescer is connected to the secondary coalescer, and the hydrocarbon feed inlet of the secondary coalescer is connected to an external fractionation device.

10. The catalytic reaction apparatus for reducing the acid consumption in isooctane production according to claim 9, characterized by: The acid hydrocarbon sedimentation and separation zone is equipped with a gas-liquid separator, and the gas phase outlet of the gas-liquid separator is connected to the vaporization outlet.

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