Heterogeneous reaction system and method for heterogeneous reactions

Abstract

The application relates to the technical field of gas-liquid two-phase mixing, and discloses a multiphase reaction system and a multiphase reaction method, the system comprising a mixer and a reactor; wherein the mixer comprises a liquid flow guide pipe 1, a gas-liquid mixing pipe 2 and a gas cavity 3; wherein the liquid flow guide pipe 1 comprises a straight pipe section and a reduced diameter section, the reduced diameter section is connected with the gas-liquid mixing pipe 2; the gas-liquid mixing pipe 2 is connected with the reactor through the gas cavity 3. The multiphase reaction system provided by the application can make the gas phase contact with the liquid phase in the form of micro-bubbles, and can continuously provide micro-bubbles, thereby strengthening the gas-liquid two-phase mass transfer process and improving the reaction rate, and can be applied in liquid phase hydrogenation technology, and is especially suitable for hydrocarbon oil hydrogenation.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of gas-liquid two-phase mixing, and particularly relates to a multiphase reaction system and a multiphase reaction method. BACKGROUND

[0002] Various multiphase reaction processes exist in industrial production, such as gas-liquid reaction, gas-liquid-solid three-phase reaction, etc., and the reaction rate is related to the contact between two phases and the diffusion rate between different phases. For example, in a liquid-phase hydrogenation process, hydrogen gas is dissolved in raw oil to meet the hydrogen demand of the hydrogenation reaction, and a sufficient amount of hydrogen gas is dissolved in the liquid circulation to meet the needs of the hydrogenation reaction, and the reaction is carried out under the condition that the gas-liquid two-phase exists in the presence of a solid catalyst.

[0003] Compared with a trickle bed, the liquid-phase hydrogenation process technology saves the circulating compressor system, the high separation system and the corresponding equipment, and can greatly save investment and energy consumption. At the same time, since the liquid-phase hydrogenation process technology can eliminate the influence of the wetting factor of the catalyst, and the specific heat capacity of the circulating oil is large, the utilization efficiency of the catalyst is improved, the temperature rise of the reactor is greatly reduced, and the cracking and other side reactions are reduced.

[0004] In the liquid-phase hydrogenation process, the mixing and transfer process of the gas-liquid two-phase are involved. Only by strengthening the mass transfer between the two phases can more hydrogen gas be dissolved in the raw oil, even to achieve super-saturation dissolution, so as to reduce the hydrogen-oil ratio in the device operation, reduce the pressure drop of the reactor, and improve the reaction efficiency. Traditionally, the method of increasing the reaction temperature is used to improve the mass transfer coefficient, and the method of pressurization is used to enhance the mass transfer driving force. However, this will not only increase the equipment investment and process energy consumption, but also the mass transfer rate will not be greatly improved.

[0005] CN201010222023.9 proposes a low hydrogen-oil ratio hydrogenation treatment method and reactor. By setting a special internal member, the reaction hydrogen-oil ratio can be reduced, the hydrogen utilization efficiency can be improved, and the utilization rate of the catalyst and the reactor volume can be improved. CN201910824430.8 discloses a multiphase flow reaction intensification reactor, which uses a tube to strengthen the mass transfer rate of gas-liquid reaction. CN201410081189.1 discloses a micro-bubble generator structure which uses a micro-porous Venturi tube and ultrasonic method to generate micro-bubbles.

[0006] Although the existing public documents report that the hydrogen utilization rate can be improved to some extent, for the hydrogenation reaction process, there are still problems of uneven gas-liquid mixing, i.e. poor hydrogen mixing and dissolving effect, low mass transfer rate, which further affects the performance of the catalyst and the final reaction effect. SUMMARY

[0007] The purpose of this invention is to address the problems of uneven mixing and low mass transfer rate in existing gas-liquid two-phase technologies, and to provide a multiphase reaction system and method. This system is suitable for reactions involving both gas and liquid phases, allowing the gas phase to contact the liquid phase in the form of microbubbles, thereby enhancing the gas-liquid two-phase mass transfer process and increasing the reaction rate.

[0008] To achieve the above objectives, a first aspect of the present invention provides a multiphase reaction system, the system comprising a mixer and a reactor; wherein the mixer comprises: a liquid guide pipe 1, a gas-liquid mixing pipe 2, and a gas chamber 3; wherein the liquid guide pipe 1 comprises a straight section and a narrowed section, the narrowed section being connected to the gas-liquid mixing pipe 2; the gas-liquid mixing pipe 2 passing through the gas chamber 3 and being connected to the reactor.

[0009] A second aspect of the present invention provides a method for a multiphase reaction, the method comprising introducing gaseous and liquid feedstocks into the multiphase reaction system described in the first aspect of the present invention for reaction.

[0010] The beneficial technical effects achieved by the present invention through the above technical solution are as follows:

[0011] 1) In a preferred embodiment of the present invention, a multiphase reaction system is provided. By setting a narrowing section in the liquid guide tube and using a gas-liquid mixing tube to diffuse the gas phase into the liquid phase, the gas phase can contact the liquid phase in the form of microbubbles and can continuously provide microbubbles, thereby enhancing the gas-liquid two-phase mass transfer process and improving the reaction rate.

[0012] 2) In a preferred embodiment of the multiphase reaction system provided by the present invention, the crushing effect can be further enhanced by setting a crusher, which is beneficial to obtaining smaller and more numerous microbubbles and further enhancing the mixing effect;

[0013] 3) The multiphase reaction system provided in a preferred embodiment of the present invention can be applied in liquid phase hydrogenation technology, especially suitable for hydrocarbon oil hydrogenation. It can achieve rapid dissolution equilibrium of hydrogen in hydrocarbon oil, and the excess gas still exists in the form of microbubbles, thereby enhancing the gas-liquid two-phase mass transfer process and improving hydrogen utilization and reaction rate, which is suitable for industrial promotion. Attached Figure Description

[0014] Figure 1 This is a structural diagram of a multiphase reaction system according to a preferred embodiment of the present invention;

[0015] Figure 2 This is a partially enlarged cross-sectional view of the liquid inlet in a preferred embodiment of the present invention;

[0016] Figure 3This is a structural diagram of a multiphase reaction system according to a preferred embodiment of the present invention.

[0017] Explanation of reference numerals in the attached figures

[0018] 1. Liquid guide pipe; 11. Liquid inlet port; 2. Gas-liquid mixing pipe

[0019] 3. Gas chamber 31, Gas feed inlet 4. Crusher

[0020] 5. Liquid chamber 51, liquid raw material inlet 61, reactor shell

[0021] 62, catalyst bed 7, separator Detailed Implementation

[0022] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0023] In this invention, unless otherwise specified, cross-sectional area refers to the cross-sectional area perpendicular to the material flow direction.

[0024] A first aspect of the present invention provides a multiphase reaction system, the system comprising a mixer and a reactor; wherein the mixer comprises: a liquid guide pipe 1, a gas-liquid mixing pipe 2, and a gas chamber 3; wherein the liquid guide pipe 1 comprises a straight section and a narrowed section, the narrowed section being connected to the gas-liquid mixing pipe 2; the gas-liquid mixing pipe 2 penetrates the gas chamber 3 and is connected to the reactor, as shown below. Figure 1 As shown.

[0025] The multiphase reaction system provided in this invention is suitable for reactions involving both gas and liquid phases. It allows the gas phase to contact the liquid phase in the form of microbubbles and can continuously provide microbubbles to the reactor, thereby enhancing the multiphase mass transfer process and increasing the reaction rate.

[0026] In one embodiment of the present invention, in the liquid guide pipe 1, the length ratio of the reduced diameter section to the length of the straight pipe section is 1:0.1-10, preferably 1:1-5.

[0027] In one embodiment of the present invention, the ratio of the cross-sectional area of ​​the inlet end to the cross-sectional area of ​​the reduced diameter section is 1-100:1, preferably 2-80:1, and more preferably 2-50:1. The inlet end of the reduced diameter section refers to the end connected to the straight pipe, and the outlet end of the reduced diameter section refers to the end connected to the gas-liquid mixing pipe.

[0028] In one embodiment of the present invention, the conical angle α between the pipe wall of the reduced diameter section and the pipe wall of the straight pipe section is 120-175°, preferably 150-170°.

[0029] In this invention, by setting a narrowing section, the liquid entering the gas-liquid mixing tube can generate a higher speed of swirling shear, which can promptly carry away small bubbles precipitated on the surface of the gas-liquid mixing tube, preventing the bubbles from growing further, thereby controlling the bubble size within a small range.

[0030] In one embodiment of the present invention, one end of the straight pipe section is closed, and the other end is connected to the reduced diameter section; wherein, a liquid inlet hole 11 is provided on the pipe wall at the closed end of the straight pipe section, the liquid inlet hole 11 allowing liquid to enter the liquid guide pipe 1 tangentially and form a swirling flow within the liquid guide pipe 1. A partial cross-sectional view of the liquid guide pipe and the liquid inlet hole is shown below. Figure 2 As shown.

[0031] In one embodiment of the present invention, the liquid inlet hole 11 extends in the pipe wall in a direction perpendicular to the extension direction of the pipe wall.

[0032] In one embodiment of the present invention, the liquid inlet holes 11 may be provided in multiple ways, preferably 1 to 8; wherein, the liquid inlet holes 11 are preferably evenly distributed along the circumferential direction of the pipe wall.

[0033] In one embodiment of the present invention, the liquid inlet 11 has a rectangular or circular cross-section perpendicular to the liquid flow direction, preferably a circle.

[0034] In one embodiment of the present invention, the system further includes a liquid chamber 5 disposed outside the liquid guide pipe 1. The liquid chamber 5 is used to supply liquid to the liquid guide pipe 1. The gas chamber and the liquid chamber are independent of each other and are not connected to each other.

[0035] In one embodiment of the present invention, a liquid phase raw material inlet 51 is provided on the liquid chamber 5; in a further preferred embodiment, the liquid phase raw material inlet 51 allows the liquid phase raw material (i.e., liquid) to enter the liquid chamber 5 tangentially.

[0036] In this invention, the liquid raw material first enters the liquid chamber through the liquid raw material inlet, then enters the straight section of the liquid guide pipe through the liquid feed hole, then enters the narrowing section, and finally enters the gas-liquid mixing pipe. The inventors of this invention have discovered that, compared to directly setting the liquid raw material inlet on the wall of the straight section of the liquid guide pipe, this invention, by using the liquid chamber for liquid entry and setting multiple liquid raw material inlets, can achieve a more uniform liquid distribution within the liquid guide pipe, and is suitable for reaction processes with large throughput or for industrial scale-up.

[0037] In one embodiment of the present invention, the wall of the gas-liquid mixing tube 2 is a porous tube, which is prepared from a porous medium material; preferably, the porous medium material is selected from metal porous tubes and / or ceramic membrane tubes.

[0038] In one embodiment of the present invention, the gas-liquid mixing tube 2 has a pore size of ≤200μm, preferably ≤50μm, and more preferably 100nm-10μm.

[0039] In this invention, the liquid in the liquid guide tube enters the gas-liquid mixing tube and flows inside. The gas in the gas chamber can enter the interior of the gas-liquid mixing tube through the pores on the tube wall and mix with the liquid inside. By utilizing the pores on the tube wall to pre-disperse the gas phase and by leveraging the high-speed shear flow of the liquid phase on the surface of the gas-liquid mixing tube, the generated bubbles can be promptly removed from the porous tube surface, preventing the formation of large bubbles.

[0040] In one embodiment of the present invention, the ratio of the cross-sectional area of ​​the gas-liquid mixing pipe 2 to the cross-sectional area of ​​the gas chamber 3 is 1:100-1000, preferably 1:500-800. In the present invention, the cross-sectional area of ​​the gas-liquid mixing pipe and the cross-sectional area of ​​the gas chamber refer to the cross-sectional area of ​​the inner wall. The area formed by the gas-liquid mixing pipe and the gas chamber is called the mixing zone.

[0041] In one embodiment of the present invention, a gaseous material inlet 31 is provided on the gas chamber 3. The present invention does not impose any special limitation on the shape of the gas chamber 3 and the gaseous material inlet 31; the gas chamber 3 can be cylindrical, and the gaseous material inlet 31 can be circular or rectangular.

[0042] In one embodiment of the present invention, the height ratio of the air chamber 3 to the liquid chamber 5 is 0.5-20:1, more preferably 1-5:1.

[0043] The gas in the gas chamber passes through the wall of the gas-liquid mixing tube and comes into contact with the liquid in the liquid chamber inside the gas-liquid mixing tube. This allows the gas phase to exist in the liquid phase in the form of small bubbles, resulting in a uniformly mixed gas-liquid mixture.

[0044] In one embodiment of the present invention, the system further includes a crusher 4, which is disposed at the outlet of the gas-liquid mixing pipe 2 and located inside the reactor.

[0045] In one embodiment of the present invention, the crusher 4 is connected to the outlet end of the gas-liquid mixing pipe 2 by a thread. The crusher further enhances the crushing effect, resulting in smaller and more numerous microbubbles, thus further strengthening the mixing effect.

[0046] In one embodiment of the present invention, the method in which the crusher 4 is arranged within the reactor is not particularly limited. The crusher may be entirely housed within the reactor, or its outlet end may be located within the reactor.

[0047] In one embodiment of the present invention, the crusher 4 is a nozzle, and the nozzle is provided with one or more spray holes.

[0048] In one embodiment of the present invention, the shape of the nozzle is selected from circular and / or elliptical, preferably circular with a diameter of 0.1-100 μm.

[0049] In one embodiment of the present invention, the nozzle is selected from a planar hole or a three-dimensional hole; wherein, a planar hole refers to a hole directly cut out of the nozzle surface, and a three-dimensional hole, taking a circular nozzle as an example, refers to a hollow cylinder set on the nozzle surface. The height of the three-dimensional hole is <10mm.

[0050] In one embodiment of the present invention, the plurality of nozzles are uniformly distributed on the surface of the nozzle.

[0051] In one embodiment of the present invention, the plurality of nozzles are arranged in a triangular or circular array around the center of the nozzle on the surface of the nozzle.

[0052] In one embodiment of the present invention, one gas chamber 3 and one liquid chamber 5 are each provided, and multiple liquid guide pipes 1, gas-liquid mixing pipes 2 and crushers 4 are provided respectively; wherein each gas-liquid mixing pipe 2 is independently connected to one liquid guide pipe 1 and one crusher 4.

[0053] In this invention, each gas-liquid mixing pipe is independently connected to a liquid guide pipe and a crusher, forming an independent component. By setting multiple independent components in the gas chamber and liquid chamber, the mixing effect of the gas and liquid phases can be further improved, the throughput can be increased, and industrial scale-up can be facilitated.

[0054] In one embodiment of the present invention, the average diameter of the microbubbles in the gas-liquid mixture flowing out of the crusher 4 is 0.1-1000 μm, preferably 50-800 μm.

[0055] In one embodiment of the invention, the mixer is connected to the reactor, which includes a reactor shell 61 and an optional catalyst bed 62, as well as an outlet disposed on the upper part of the reactor shell 61.

[0056] This invention does not impose any special limitations on the connection method between the mixer and the reactor. The mixer can be installed inside the reactor shell or outside the reactor shell.

[0057] In one embodiment of the present invention, the mixer is connected to the reactor, the reactor including a reactor shell 61 and a catalyst bed 62, and an outlet disposed on the upper part of the reactor shell 61.

[0058] In one embodiment of the invention, the system further includes a separator 7 connected to the outlet of the reactor for separating the gas phase and the liquid phase, such as... Figure 3 As shown.

[0059] A second aspect of the present invention provides a method for a multiphase reaction, the method comprising introducing gaseous and liquid feedstocks into the gas-liquid phase reaction system described in the first aspect of the present invention for reaction.

[0060] In this process, liquid feedstock is introduced into the liquid chamber through the liquid feedstock inlet. The liquid feedstock then enters the liquid guide pipe through the liquid feed hole and subsequently enters the gas-liquid mixing pipe. Gas feedstock enters the gas chamber through the gas feedstock inlet. The gas feedstock passes through the wall of the gas-liquid mixing pipe, forming small bubbles on the wall. These small bubbles are sheared by the swirling liquid feedstock within the gas-liquid mixing pipe and enter the liquid feedstock, forming a gas-liquid mixture containing small bubbles. This gas-liquid mixture containing small bubbles enters a crusher where the small bubbles are further broken into microbubbles, forming a gas-liquid mixture containing microbubbles. This gas-liquid mixture containing microbubbles flows out of the crusher and into the reactor, where it passes through the catalyst bed and begins to react. Preferably, the products generated after the reaction are collected through the outlet and then separated in a separator.

[0061] In one embodiment of the present invention, the method includes introducing a gaseous feedstock, a liquid feedstock, and a catalyst into a multiphase reaction system containing a catalyst bed for catalytic reaction; wherein the gaseous feedstock and the liquid feedstock are mixed by a mixer in the system and then enter the reactor in the system to contact the catalyst packed in the reactor for catalytic reaction;

[0062] In one embodiment of the present invention, the gaseous feedstock is hydrogen, and the liquid feedstock is hydrocarbon oil, selected from at least one of liquefied petroleum gas, naphtha, gasoline, kerosene, diesel, wax oil, and residual oil. The gasoline may be reformed oil. In this invention, reformed oil has a meaning known in the art and will not be elaborated further.

[0063] This invention does not impose specific limitations on the catalyst or the specific operating conditions of the catalytic reaction. Conventional catalysts and operating conditions can be selected based on the specific types of gaseous and liquid feedstocks. For example, in the catalytic reaction of hydrocarbon oil and hydrogen, the catalyst can be a supported catalyst with an active component supported on a heat-resistant inorganic oxide. The inorganic oxide can be selected from alumina and / or silica; the active component can be selected from one or more of nickel, molybdenum, tungsten, platinum, and palladium, as well as other auxiliary components such as chlorine, sulfur, and oxygen. Preferably, the catalyst is a solid particle, and the shape of the solid particle is selected from one or more of spherical, strip-shaped, butterfly-shaped, clover-shaped, and tetraclover-shaped. Preferably, the packing porosity of the catalyst in the catalyst bed is 30-60%.

[0064] In one embodiment of the present invention, in the catalytic reaction of hydrocarbon oil and hydrogen, the catalyst comprises, based on the total mass of the catalyst, 0.22-0.4 wt% Pd, 0.07-0.18 wt% Pt, 0.4-3 wt% chlorine, and 96.42-99.31 wt% sulfate-containing alumina support; wherein the mass content of Pd, Pt, and chlorine is based on elemental composition, and the sulfate-containing alumina support is based on the total mass; the sulfate content in the sulfate-containing alumina support is 0.3-3 wt% based on the total mass of the support. The catalyst can be prepared according to conventional methods in the art, or it can be a commercially available product, such as TORH-1, RS1000, or other commercially available catalysts.

[0065] In one embodiment of the present invention, in the catalytic reaction of hydrocarbon oil and hydrogen, the reaction conditions include: a reaction temperature of 50-400°C, preferably 50-300°C; a reaction pressure of 0.5-15 MPa, preferably 0.5-10 MPa; and a liquid-phase feedstock volume hourly space velocity of 0.1-20 h⁻¹. -1 Preferably 1-15h -1 The hydrogen-to-oil volume ratio is 1-500:1, preferably 2-300:1.

[0066] In one embodiment of the present invention, in the catalytic reaction of hydrocarbon oil and hydrogen, the theoretical chemical hydrogen consumption of the catalytic reaction is <1 wt%.

[0067] In one embodiment of the present invention, when the gaseous feedstock is hydrogen and the liquid feedstock is reformed oil, the reaction conditions for the hydrogenation reaction include: a reaction temperature of 100-200°C, a reaction pressure of 1-3 MPa, and a volume hourly space velocity (VHSV) of 5-15 h⁻¹ for the liquid feedstock. -1 The hydrogen-to-oil volume ratio is 1-25:1.

[0068] The present invention will be described in detail below through examples and comparative examples. TORH-1 was obtained from the Catalyst Division of Sinopec and is in the form of strip-shaped granules. The composition of the reformate oil in the examples and comparative examples is shown in Table 1:

[0069] Table 1

[0070]

[0071]

[0072] Example 1

[0073] The multiphase reaction system in Example 1 includes a mixer, a reactor, and a separator. The mixer includes a liquid guide pipe, a gas-liquid mixing pipe, a gas chamber, and a breaker. The liquid guide pipe includes a straight section and a reduced-diameter section. The straight section is 90 mm long, the reduced-diameter section is 30 mm long, the inner diameter of the inlet end of the reduced-diameter section is 40 mm, and the inner diameter of the outlet end of the reduced-diameter section is 8 mm. The cone angle α between the wall of the reduced-diameter section and the wall of the straight section is 170°. A liquid inlet hole is provided on the closed end of the straight section. The extension direction of the liquid inlet hole within the pipe wall is perpendicular to the extension direction of the pipe wall, allowing liquid to enter the liquid guide pipe tangentially and form a swirling flow within the liquid guide pipe. The liquid chamber is located outside the liquid guide pipe, with a height of 110 mm, and has a liquid-phase feed inlet.

[0074] The gas-liquid mixing tube is made of a porous metal tube with a pore size of 10 μm. The outer diameter of the gas-liquid mixing tube is 12 mm and the inner diameter is 8 mm. The inner diameter of the gas chamber is 200 mm and the height ratio of the gas chamber to the liquid chamber is 2. The breaker is a nozzle with three planar circular nozzles with a diameter of 100 μm evenly arranged.

[0075] There is one gas chamber and one liquid chamber, and three liquid guide pipes, three gas-liquid mixing pipes and three crushers. Each gas-liquid mixing pipe is independently connected to a liquid guide pipe and a crusher to form an independent component.

[0076] The reactor includes a reactor shell and a catalyst bed, as well as an outlet located at the top of the reactor shell; wherein, a mixer is located inside the reactor shell, below the catalyst bed, and a separator is connected to the reactor outlet.

[0077] Reformed oil is fed through the liquid feed inlet, and hydrogen is fed through the gaseous feed inlet. After being mixed in a mixer, the mixture enters a catalyst bed packed with TORH-1 to undergo reaction. The reaction products are collected through the outlet and sent to a separation unit for separation. The reaction temperature is 140℃, the reaction pressure is 1.7MPa, and the volume hourly space velocity (VHSV) of the reformed oil is 10.0 h⁻¹. -1 The hydrogen-to-oil volume ratio was 5, and the average diameter of the generated microbubbles was 500μm-800μm. The properties of the reaction products are shown in Table 2.

[0078] Example 2

[0079] Similar to Example 1, except that: the gas-liquid mixing tube in the gas-liquid phase reaction system is composed of a metal porous tube with a pore size of 1 μm, and the average diameter of the generated microbubbles is 300 μm-700 μm. The properties of the reaction products are shown in Table 2.

[0080] Example 3

[0081] Similar to Example 2, the difference is that: three liquid inlet holes are evenly distributed along the circumference of the pipe wall of the straight section of the liquid guide pipe, and the average diameter of the generated microbubbles is 50μm-300μm. The properties of the reaction products are shown in Table 2.

[0082] Comparative Example 1

[0083] Similar to Example 1, except that: the gaseous and liquid raw materials are directly mixed through pipelines and then enter the reactor, and the properties of the reaction products are shown in Table 2.

[0084] Table 2

[0085] Example 1 Example 2 Example 3 Comparative Example 1 Olefin removal, % 95.8 98.0 99.0 90.0 Hydrogenated product bromine index, mg Br / 100 g 103 48 24 243

[0086] The bromine index refers to the number of milligrams of bromine consumed per 100 grams of sample. Olefin removal rate % = [1 - (A...] p / A f )]×100%, where A p A represents the bromine index of the reaction product. f The bromine index is the value of the raw material.

[0087] As shown in Table 2, the multiphase reaction system provided in this invention can be applied to liquid-phase hydrogenation technology, especially suitable for hydrocarbon oil hydrogenation. It can achieve rapid dissolution equilibrium of hydrogen in hydrocarbon oil, thereby enhancing the gas-liquid two-phase mass transfer process and improving hydrogen utilization and reaction rate.

[0088] The preferred embodiments of the present invention have been described in detail above; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combinations of various technical features in any other suitable manner. These simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention.

Claims

1. A multiphase reaction system, characterized in that, The system includes a mixer and a reactor; wherein the mixer includes: a liquid guide pipe (1), a gas-liquid mixing pipe (2) and a gas chamber (3); the liquid guide pipe (1) includes a straight section and a narrowed section, the narrowed section being connected to the gas-liquid mixing pipe (2); the gas-liquid mixing pipe (2) passes through the gas chamber (3) and is connected to the reactor; The gas-liquid mixing pipe (2) has a porous wall.

2. The system according to claim 1, wherein, In the liquid guide tube (1), the length ratio of the reduced diameter section to the length of the straight section is 1:0.1-10.

3. The system according to claim 2, wherein, In the liquid guide tube (1), the length ratio of the reduced diameter section to the length of the straight section is 1:1-5.

4. The system according to claim 1, wherein, The ratio of the cross-sectional area at the inlet end of the reduced-diameter section to the cross-sectional area at the outlet end is 1-100:

1.

5. The system according to claim 4, wherein, The ratio of the cross-sectional area at the inlet end of the reduced-diameter section to the cross-sectional area at the outlet end is 2-80:

1.

6. The system according to claim 5, wherein, The ratio of the cross-sectional area at the inlet end of the reduced-diameter section to the cross-sectional area at the outlet end is 2-50:

1.

7. The system according to claim 1, wherein, The conical angle α between the wall of the reduced-diameter section and the wall of the straight section is 120-175°.

8. The system according to claim 7, wherein, The conical angle α between the wall of the reduced-diameter section and the wall of the straight section is 150-170°.

9. The system according to claim 1, wherein, One end of the straight pipe section is closed, and the other end is connected to the reduced diameter section; wherein, a liquid inlet hole (11) is provided on the pipe wall at the closed end of the straight pipe section, and the liquid inlet hole (11) allows the liquid to enter the liquid guide pipe (1) tangentially and form a swirling flow in the liquid guide pipe (1).

10. The system according to claim 1, wherein, The system also includes a liquid chamber (5) disposed outside the liquid guide tube (1) for supplying liquid to the liquid guide tube (1).

11. The system according to claim 10, wherein, The liquid chamber (5) is provided with a liquid raw material inlet (51).

12. The system according to claim 11, wherein, The liquid feed inlet (51) allows the liquid feed to enter the liquid chamber (5) tangentially.

13. The system according to claim 1, wherein, The gas-liquid mixing tube (2) is made of porous media material.

14. The system according to claim 13, wherein, The porous media material is selected from metal porous tubes and / or ceramic membrane tubes.

15. The system according to claim 1, wherein, The gas-liquid mixing tube (2) has an aperture of ≤200μm.

16. The system according to claim 15, wherein, The gas-liquid mixing tube (2) has an aperture of ≤50μm.

17. The system according to claim 16, wherein, The gas-liquid mixing tube (2) has a pore size of 100nm-10μm.

18. The system according to claim 1, wherein, The ratio of the cross-sectional area of ​​the gas-liquid mixing pipe (2) to the cross-sectional area of ​​the gas chamber (3) is 1:100-1000.

19. The system according to claim 18, wherein, The ratio of the cross-sectional area of ​​the gas-liquid mixing pipe (2) to the cross-sectional area of ​​the gas chamber (3) is 1:500-800.

20. The system according to claim 1, wherein, The gas chamber (3) is provided with a gaseous raw material inlet (31).

21. The system according to claim 10, wherein, The height ratio of the air chamber (3) to the liquid chamber (5) is 0.5-20:

1.

22. The system according to claim 1, wherein, The system also includes a crusher (4), which is located at the outlet of the gas-liquid mixing pipe (2) and inside the reactor.

23. The system according to claim 22, wherein, The crusher (4) is connected to the outlet end of the gas-liquid mixing pipe (2) by a thread.

24. The system according to claim 22, wherein, The crusher (4) is a nozzle, and the nozzle is provided with one or more spray holes.

25. The system according to claim 24, wherein, The multiple nozzles are evenly distributed on the surface of the nozzle.

26. The system according to claim 25, wherein, The multiple nozzles are arranged in a triangular or circular array around the center of the nozzle on the nozzle surface.

27. The system according to claim 22, wherein, The crusher (4) is installed entirely or partially inside the reactor.

28. The system according to any one of claims 1-27, wherein, Each of the gas chamber (3) and the liquid chamber (5) is configured as one; the liquid guide pipe (1), the gas-liquid mixing pipe (2) and the crusher (4) are configured as multiple; wherein each gas-liquid mixing pipe (2) is independently connected to a liquid guide pipe (1) and a crusher (4).

29. The system according to claim 1, wherein, The mixer is connected to the reactor, which includes a reactor shell (61) and an optional catalyst bed (62), as well as an outlet located on the upper part of the reactor shell (61).

30. The system according to claim 1, wherein, The system also includes a separator (7) for separating the gas phase and the liquid phase.

31. The system according to claim 29, wherein, The mixer is connected to the reactor, which includes a reactor shell (61) and a catalyst bed (62), as well as an outlet located on the upper part of the reactor shell (61).

32. A method for a multiphase reaction, characterized in that, The method includes introducing gaseous and liquid feedstocks into the system according to any one of claims 1-31 for reaction.

33. The method according to claim 32, wherein, The method includes introducing gaseous feedstock, liquid feedstock and catalyst into the system to carry out a catalytic reaction; The gaseous and liquid raw materials are mixed in the mixer of the system and then enter the reactor of the system, where they come into contact with the catalyst packed in the reactor to carry out a catalytic reaction.

34. The method according to claim 33, wherein, The gaseous feedstock is hydrogen; the liquid feedstock is hydrocarbon oil, selected from at least one of liquefied petroleum gas, naphtha, gasoline, kerosene, diesel, wax oil, and residual oil.

35. The method according to claim 33, wherein, The catalyst is a solid particle, and the shape of the solid particle is selected from one or more of the following: spherical, strip-shaped, butterfly-shaped, clover-shaped, and four-leaf clover-shaped.

36. The method according to claim 33, wherein, The catalyst has a packing void ratio of 30-60% in the catalyst bed.

37. The method according to claim 33, wherein, The reaction conditions for the catalytic reaction include: a reaction temperature of 50-400℃; a reaction pressure of 0.5-15MPa; and a volume hourly space velocity (VHSV) of 0.1-20h for the liquid phase feedstock. -1 The hydrogen-to-oil volume ratio is 1-500:

1.

38. The method according to claim 37, wherein, The reaction conditions for the catalytic reaction include: a reaction temperature of 50-300℃; a reaction pressure of 0.5-10MPa; and a liquid-phase feedstock volume hourly space velocity of 1-15h⁻¹. -1 The hydrogen-to-oil volume ratio is 2-300:

1.

39. The method according to any one of claims 33-38, wherein, The theoretical chemical hydrogen consumption of the catalytic reaction is <1 wt%.

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