A distributor, a distribution component, and a hydrogenation reactor for multiple gas-liquid cross-flow mixing

Abstract

A distributor, a distribution component, and a hydrogenation reactor for multiple gas-liquid cross-flow mixing, comprising a mixing channel. Along the length direction of the mixing channel, there is a gas-phase inlet. When high-speed gas enters the mixing channel, negative pressure is generated to suck in the liquid phase, and the gas phase and the liquid phase are mixed once to form a gas-liquid mixed flow. Below the mixing channel, there is an outward expansion area. The lower end opening of the outward expansion area is closed by a bottom plate, and gas-liquid mixed flow outlets are distributed on the bottom plate. In the outward expansion area, a flow-breaking plate is connected by an elastic connecting rod, and the edge of the flow-breaking plate extends beyond the bottom of the mixing channel and forms a variable-gap channel with the lower end of the mixing channel. The gas-liquid mixed flow formed by the mixing channel impacts the flow-breaking plate to achieve secondary mixing, causing the flow-breaking plate to vibrate. As a result, the gas-liquid mixed flow is deflected to the inner side wall of the outward expansion area to achieve tertiary mixing, and is deflected by the inner side wall of the outward expansion area to the bottom plate to achieve quaternary mixing, and finally flows out through the outlet on the bottom plate. In the present invention, the gas phase and the liquid phase can achieve multiple cross-flow mixings, making the mixing of the gas phase and the liquid phase more uniform.

Description

Technical Field

[0001] The present invention relates to the technical fields of oil refining and chemical engineering, and particularly to a distributor, a distribution component, and a hydrogenation reactor with multiple gas-liquid baffle mixings. Background Art

[0002] Hydrogenation reactions are widespread in the processes of oil refining and petrochemical engineering, such as hydrocracking, hydrofining reactions, etc. The effect of hydrogenation reactions depends on two main factors. One is the performance of the catalyst, and the other is the structure of the reactor. The key to fully exerting the effective energy of a highly active catalyst lies in whether the structural setting of the reactor can enable the solid phase (catalyst) - liquid phase (feedstock oil) - gas phase (hydrogen) to contact sufficiently and uniformly, so as to achieve the purpose of full reaction between the gas and liquid phases. Among them, the core component of the hydrogenation reactor - the gas-liquid distributor plays a decisive role in the distribution state of the gas-liquid mixture flow in the catalyst bed, that is, the gas-liquid distribution performance of the gas-liquid distributor directly affects the uniformity of the contact time between the reactants and the catalyst, and affects the degree of wetting of the catalyst surface by the liquid phase. If the gas-liquid mixture flow in the catalyst bed is unevenly distributed, it will form a bypass flow or local short circuit, which will cause some catalysts to be overused or not fully used, and easily lead to phenomena such as local overheating of the bed and catalyst coking, directly affecting the catalyst utilization rate and product distribution. The excessive radial temperature difference in the catalyst bed is likely to cause "temperature runaway", resulting in frequent shutdowns of the device and even threatening the safety of the device, thereby having a negative impact on the overall economic benefits of the refinery.

[0003] In the prior art, the gas-liquid distributor includes a main pipe and a fragmentation plate arranged below the main pipe. The main pipe is provided with an air inlet and a liquid inlet located below the air inlet. Among them, the fragmentation plate is fixedly connected to the lower end pipe orifice of the main pipe through a connecting leg, and a fluid channel is formed between the fragmentation plate and the lower end pipe orifice of the main pipe. The gas phase enters the main pipe through the air inlet, and the liquid phase enters the main pipe through the liquid inlet and mixes with the gas phase to form a gas-liquid mixed fluid. The gas-liquid mixed fluid flows downward and collides with the fragmentation plate. Part of the mixed fluid splashes and diffuses around, and finally flows out of the distributor through the fluid channel. In this distributor, the gas-liquid mixed flow only undergoes one fragmentation and mixing, and the gas-liquid mixing is not sufficient, resulting in uneven mixing. Summary of the Invention

[0004] In order to solve the problem of uneven mixing of the gas phase and the liquid phase in the prior art, the present invention provides a distributor, a distribution component, and a hydrogenation reactor with multiple gas-liquid baffle mixings, which can achieve multiple gas-liquid baffle mixings, making the gas phase and the liquid phase mix more evenly.

[0005] To achieve the above object, the specific solution adopted by the present invention is as follows: A distributor for multi-stage gas-liquid cross-flow mixing includes a mixing channel, which has a gas-phase inlet along the length direction of the mixing channel. High-speed gas enters the mixing channel to generate negative pressure to suck in liquid phase, and the gas phase and the liquid phase are mixed once to form a gas-liquid mixed flow. There is an outward expansion area below the mixing channel, and the lower end opening of the outward expansion area is closed by a bottom plate, and gas-liquid mixed flow outlets are distributed on the bottom plate; a fragmentation plate is connected in the outward expansion area through an elastic connecting rod, and the edge of the fragmentation plate extends beyond the bottom of the mixing channel and forms a variable clearance channel with the lower end of the mixing channel; the gas-liquid mixed flow formed by the mixing channel impacts the fragmentation plate to achieve secondary mixing, and causes the fragmentation plate to vibrate, thereby making the gas-liquid mixed flow flow to the inner side wall of the outward expansion area for tertiary mixing, and being deflected by the inner side wall of the outward expansion area to the bottom plate for quaternary mixing, and finally flowing out through the outlet on the bottom plate.

[0006] As an optimized solution of the above distributor for multi-stage gas-liquid cross-flow mixing: The mixing channel is a main pipe with a closed top, the gas-phase inlet is opened on the side wall of the main pipe, and a liquid suction port for the liquid phase to enter is opened on the side wall of the main pipe below the gas-phase inlet.

[0007] As another optimized solution of the above distributor for multi-stage gas-liquid cross-flow mixing: The diameter of the fragmentation plate is larger than the diameter of the main pipe and smaller than the diameter of the outward expansion area, and a flow deflection channel is formed between the edge of the fragmentation plate and the inner side wall of the outward expansion area.

[0008] As another optimized solution of the above distributor for multi-stage gas-liquid cross-flow mixing: Multiple convex ribs are distributed on the upper surface of the fragmentation plate, and the convex ribs make the upper surface of the fragmentation plate form a corrugated shape.

[0009] As another optimized solution of the above distributor for multi-stage gas-liquid cross-flow mixing: The bottom plate includes a support ring connected to the inner side wall of the outward expansion area, and a plurality of parallel strip-shaped rods are arranged inside the support ring, and slits are formed between adjacent two strip-shaped rods to form the outlets of the gas-liquid mixed flow.

[0010] As another optimized solution of the above distributor for multi-stage gas-liquid cross-flow mixing: The bottom plate is a circular plate-like structure, and outlets of the gas-liquid mixed flow are opened on the bottom plate.

[0011] As another optimized solution of the above distributor for multi-stage gas-liquid cross-flow mixing: The fragmentation plate is connected to the bottom plate through an elastic connecting rod.

[0012] As another optimization solution for the distributor of the above-mentioned gas-liquid multi-pass baffle mixing: an inner tube capable of reciprocating along the gas-liquid flow direction is arranged in the mixing channel, the baffle plate is connected to the lower end opening of the inner tube, and a fluid channel communicating with the inner cavity of the outer expansion area is formed between the lower end of the inner tube and the baffle plate. The mixing channel is provided with a liquid suction port below the gas phase inlet for the liquid phase to enter. The gas-liquid mixed flow impacts the baffle plate to drive the inner tube to move along the mixing channel, thereby adjusting the area of the liquid suction port blocked by it.

[0013] As another optimization solution for the distributor of the above-mentioned gas-liquid multi-pass baffle mixing: the inner tube is of a cylindrical structure, the mixing channel is formed by a cylindrical main pipe with a closed top, and the top end of the inner tube extends to the liquid suction port.

[0014] As another optimization solution for the distributor of the above-mentioned gas-liquid multi-pass baffle mixing: the baffle plate is connected to the lower end opening of the inner tube through a plurality of connecting legs distributed at intervals, and the gaps between the connecting legs form a fluid channel.

[0015] As another optimization solution for the distributor of the above-mentioned gas-liquid multi-pass baffle mixing: the side wall of the main pipe is provided with a limiting groove distributed along its axial direction, and a limiting rod connected to the outer side wall of the inner tube is slidably arranged in the limiting groove.

[0016] As another optimization solution for the distributor of the above-mentioned gas-liquid multi-pass baffle mixing: the free end of the limiting rod extends into the inner cavity of the outer expansion area, and the limiting rod is connected to the top of the outer expansion area through an elastic connecting rod.

[0017] A gas-liquid multi-pass baffle mixing distribution assembly includes a distribution plate with a plurality of distribution holes formed on its surface. Each distribution hole is provided with the above-mentioned distributor. The main pipe of the distributor passes through the distribution hole and is vertically fixed on the distribution plate, and the outer expansion area is located below the distribution plate, and the liquid suction port is located above the distribution plate. A liquid suction area is formed between the liquid suction port and the distribution plate.

[0018] A gas-liquid multi-pass baffle mixing hydrogenation reactor has the above-mentioned distribution assembly.

[0019] Compared with the prior art, the present invention has the following beneficial effects:

[0020] 1. The present invention provides a distributor for multi - stage gas - liquid cross - flow mixing. The high - speed gas phase enters the mixing channel through the gas phase inlet, creating a negative pressure in the mixing channel. Then, the liquid phase is sucked into the mixing channel. The gas phase and the liquid phase are mixed in the mixing channel to achieve a primary mixing, forming a gas - liquid mixed flow. The gas - liquid mixed flow continues to move downward and impacts the flow - breaking plate to achieve a secondary mixing. Moreover, when it impacts the flow - breaking plate, it is deflected to the inner side wall of the outer expansion area to achieve a tertiary mixing, and then deflected to the bottom plate to achieve a quaternary mixing. Finally, it flows out of the distributor through the outlet of the gas - liquid mixed flow on the bottom plate. That is, the gas - liquid mixed flow undergoes multiple cross - flow mixings in the outer expansion area, extending the contact time between the gas phase and the liquid phase. And when the liquid phase is deflected and impacted, it breaks into small droplets, strengthening the gas - liquid mixing and making the mixing more uniform. At the same time, the gas - liquid mixed flow impacts the flow - breaking plate, causing it to vibrate up and down. And the upper surface of the flow - breaking plate is corrugated, which will cause self - excited vibration of the gas - liquid mixed flow on the flow - breaking plate, strengthening the turbulence degree of the gas - liquid mixed flow and further enhancing the mixing of the gas - liquid two - phase.

[0021] 2. In the present invention, an increase or decrease in the gas phase flow rate will increase or decrease the impact force on the flow - breaking plate. That is, the flow - breaking plate moves downward or upward, driving the inner tube to slide downward or upward, thereby adjusting the area of its occlusion of the liquid suction port to increase or decrease the liquid suction port, and finally resulting in an increase or decrease in the liquid inlet volume. That is, the liquid inlet volume can be automatically adjusted according to the gas phase flow rate. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] Figure 1 is a schematic structural diagram of the present invention;

[0023] Figure 2 is a schematic structural diagram of the bottom plate;

[0024] Figure 3 is a cross - sectional schematic diagram of the bottom plate;

[0025] Figure 4 is another schematic structural diagram of the bottom plate;

[0026] Figure 5 is a schematic structural diagram of the flow - breaking plate;

[0027] Figure 6 is a schematic diagram of the mechanism of Embodiment 3;

[0028] Figure 7 is a schematic structural diagram of Embodiment 4;

[0029] Figure 8 is a schematic structural diagram of Embodiment 5;

[0030] Figure 9 Schematic structural diagram of the distribution component;

[0031] Reference numerals: 1, mixing channel; 101, gas phase inlet; 102, main pipe; 103, liquid suction port; 104, limiting groove; 2, outer expansion area; 201, elastic connecting rod; 3, bottom plate; 301, support ring; 302, strip-shaped rod; 303, strip slot; 304, sieve hole; 4, broken flow plate; 401, baffle channel; 402, convex rib; 5, inner pipe; 501, limiting rod; 502, connecting leg; 503, fluid channel; 6, distribution plate; 601, liquid suction area. Detailed implementation mode

[0032] The technical solutions of the present invention will be further elaborated in detail below in combination with specific embodiments. For the parts not detailedly recorded and disclosed in the following embodiments of the present invention, they should all be understood as the prior art known or should be known to those skilled in the art, such as the specific structure of the distribution plate, the arrangement mode and opening rate of the distribution holes on the distribution plate, the arrangement mode of the distributors on the distribution plate, other component mechanisms of the hydrogenation reactor, etc.

[0033] Embodiment 1

[0034] Such as Figure 1As shown in the figure, a distributor for multi-stage gas-liquid cross-flow mixing includes a mixing channel 1. The mixing channel 1 is formed by a main pipe 102 with a closed top. The main pipe 102 is a circular tubular structure with a wall thickness of 1 to 4 mm. The top of the main pipe 102 is closed by a baffle. The diameter of the baffle is equal to the outer diameter of the main pipe 102, and the connection between the two can be integral connection, welding or bolt connection. In this embodiment, the baffle and the main pipe 102 are integrally connected. The gas-phase and liquid-phase logistics coming from above are blocked by the baffle at the top of the main pipe 102 to prevent the gas-phase and liquid-phase from directly entering the main pipe 102 through the top end of the main pipe 102, resulting in uneven gas-liquid mixing. The mixing channel 1 has a gas-phase inlet 101 along its length direction. Specifically, the gas-phase inlet 101 is opened on the inner side wall of the main pipe 102 and close to the top end of the main pipe 102. The number of gas-phase inlets 101 is 2 to 8 and they are evenly distributed along the circumferential direction of the main pipe 102. In this embodiment, the number of gas-phase inlets 101 is 4, and the heights of the 4 gas-phase inlets 101 are the same. The shape of the gas-phase inlet 101 can be circular, rectangular or triangular, etc. In this embodiment, the gas-phase inlet 101 is a circular hole structure. The high-speed gas-phase enters the mixing channel 1 through the gas-phase inlet 101, generating a negative pressure to suck in the liquid-phase, and the gas-phase and liquid-phase are mixed once in the mixing channel 1 to form a gas-liquid mixed flow. Specifically, a plurality of liquid suction ports 103 for the liquid-phase to enter are opened on the outer side wall of the main pipe 102. The liquid suction ports 103 are located below the gas-phase inlets 101. The number of liquid suction ports 103 is 2 to 8 and they are evenly distributed along the circumferential direction of the main pipe 102. In this embodiment, the number of liquid suction ports 103 is 4, and the heights of the 4 liquid suction ports 103 are the same. The shape of the liquid suction port 103 can be circular, rectangular or triangular. In this embodiment, the liquid suction port 103 is a circular hole structure.

[0035] Below the mixing channel 1, there is an outward expansion area 2. Specifically, the lower end of the main pipe 102 is coaxially connected with the outward expansion area 2. The lower end opening of the outward expansion area 2 is closed by the bottom plate 3, and gas-liquid mixed flow outlets are distributed on the bottom plate 3. Among them, the top opening of the outward expansion area 2 is closed by the top plate, and a through hole is opened at the center position of the top plate. The diameter of the through hole is equal to the outer diameter of the main pipe 102. The lower end of the main pipe 102 can extend through the through hole into the inner cavity of the outward expansion area 2 or be communicated with the through hole and then with the inner cavity of the outward expansion area 2. In this embodiment, the outer side wall of the lower end of the main pipe 102 is hermetically connected to the inner side wall of the through hole, that is, the lower end of the main pipe 102 does not extend into the inner cavity of the outward expansion area 2. Correspondingly, the diameter of the through hole is equal to the outer diameter of the main pipe 102. Inside the outward expansion area 2, a fragmentation plate 4 is connected by an elastic connecting rod 201, and the edge of the fragmentation plate 4 extends beyond the bottom of the mixing channel 1 and forms a variable clearance channel with the lower end of the mixing channel 1. In this embodiment, the fragmentation plate 4 is located at the middle position of the outward expansion area 2. The setting of the fragmentation plate 4 increases the degree of gas-liquid turbulence in the distributor, breaks the liquid phase into small droplets, and thus strengthens the mixing of the gas phase and the liquid phase. At the same time, it increases the flow time of the gas-liquid mixed flow, thereby prolonging the contact time between the gas phase and the liquid phase and improving the mixing effect of the gas phase and the liquid phase. And the fragmentation plate 4 is connected to the outward expansion area 2 through an elastic connecting rod 201. The gas-liquid mixed flow formed by the mixing channel 1 impacts the fragmentation plate 4 to achieve secondary mixing. The small-amplitude high-frequency vibration of the fragmentation plate 4 causes the gas-liquid mixed flow to deflect to the inner side wall of the outward expansion area 2 to achieve tertiary mixing, and then deflects again to the bottom plate 3 to achieve quaternary mixing, and finally flows out through the outlet on the bottom plate 3. The gas-liquid mixed flow undergoes multiple deflections and mixings in the outward expansion area 2, prolonging the contact time between the gas phase and the liquid phase, strengthening the gas-liquid mixing and making the mixing more uniform.

[0036] Specifically, the fragmentation plate 4 is a circular plate-like structure coaxially arranged with the main pipe 102. The diameter of the fragmentation plate 4 is larger than the diameter of the main pipe 102 and smaller than the diameter of the outward expansion area 2. A deflection channel 401 is formed between the edge of the fragmentation plate 4 and the inner side wall of the outward expansion area 2. If the diameter of the fragmentation plate 4 is smaller than the diameter of the main pipe 102, part of the gas-liquid mixed flow in the main pipe 102 will flow out of the distributor directly without impacting the fragmentation plate 4, resulting in uneven mixing of the gas-liquid mixed flow. Therefore, the diameter of the fragmentation plate 4 being larger than the diameter of the main pipe 102 enables all the gas-liquid mixed flow in the main pipe 102 to impact the fragmentation plate 4, causing it to impact and break on the fragmentation plate 4, strengthening the mixing of the two phases. At the same time, it deflects the gas-liquid mixed flow to the inner side wall of the outward expansion area 2. If the diameter of the fragmentation plate 4 is equal to that of the outward expansion area 2, the edge of the fragmentation plate 4 will be in close contact with the inner side wall of the outward expansion area 2, resulting in the inability of the gas-liquid mixed flow to flow out. Therefore, the diameter of the fragmentation plate 4 is larger than the diameter of the main pipe 102 and smaller than the inner diameter of the outward expansion area 2. Specifically, the ratio of the diameter of the fragmentation plate 4 to the diameter of the outward expansion area 2 is 0.5 - 0.9. In this embodiment, the ratio of the two is 0.8.

[0037] Further limitations are imposed on the structure of the bottom plate 3: AsFigure 2 and Figure 3 As shown in Figure 3 , the bottom plate 3 is located at the opening at the lower end of the outward expansion area 2. The bottom plate 3 includes a support ring 301 connected to the inner side wall of the outward expansion area 2. The outer diameter of the support ring 301 is equal to the inner diameter of the outward expansion area 2. The outer side wall of the support ring 301 is fixedly connected to the inner side wall of the outward expansion area 2, and the connection method between the two is welding or interference fit. A plurality of parallel strip-shaped rods 302 are arranged inside the support ring 301. The lengths of each strip-shaped rod 302 are different, and a slit 303 exists between two adjacent strip-shaped rods 302 to form an outlet for the gas-liquid mixture.

[0038] In other embodiments of the present invention, as Figure 4 shown in Figure 4 , the bottom plate 3 is a circular plate-like structure, and an outlet for the gas-liquid mixed flow is opened on the bottom plate 3. The outlet can be a sieve hole 304 or a through groove.

[0039] The above is the basic embodiment of the present invention, and further improvements, optimizations and limitations can be made on this basis to obtain the following embodiments:

[0040] Embodiment 2

[0041] This embodiment is an improved scheme based on Embodiment 1. Its main structure is the same as that of Embodiment 1. The improvement lies in: as Figure 1 shown in Figure 1 , the crushing flow plate 4 is connected to the bottom plate 3 through elastic connecting rods 201. The number of elastic connecting rods 201 is 3 to 4 and is evenly distributed around the axis of the crushing flow plate 4. In this embodiment, the number of elastic connecting rods 201 is 4. One end of the elastic connecting rod 201 is connected to the upper surface of the bottom plate 3, and the other end of the elastic connecting rod 201 is connected to the lower surface of the crushing flow plate 4. The connection part of the elastic connecting rod 201 and the crushing flow plate 4 is close to the edge of the crushing flow plate 4.

[0042] As Figure 5 shown in Figure 5 , a plurality of convex ridges 402 are distributed on the surface of the crushing flow plate 4. The convex ridges 402 make the upper surface of the crushing flow plate 4 form a corrugated shape. When the gas-liquid mixed flow impacts the crushing flow plate 4, the gas-liquid mixed flow breaks and realizes secondary mixing, and makes the crushing flow plate 4 vibrate up and down. The upper surface of the crushing flow plate 4 is corrugated, which will cause self-excited vibration of the gas-liquid mixed flow on the crushing flow plate 4, strengthening the turbulence degree of the gas-liquid mixed flow and further enhancing the mixing of the gas-liquid two phases.

[0043] Embodiment 3

[0044] This embodiment is an improved solution based on Embodiment 2. Its main structure is the same as that of Embodiment 1. The improvement lies in that: an inner tube 5 capable of reciprocating along the gas-liquid flow direction is arranged in the mixing channel 1. The inner tube 5 is coaxially arranged with the mixing channel 1. The inner tube 5 is a cylindrical structure with openings at both ends, and its top end extends to the liquid suction port 103. The outer diameter of the inner tube 5 is equal to the inner diameter of the main pipe 102, and the two are in clearance fit. During the reciprocating movement of the inner tube 5, the liquid suction port 103 can be blocked, thereby adjusting the liquid inflow volume in the main pipe 102. The fragmentation plate 4 is connected to the lower end pipe orifice of the inner tube 5, and a fluid channel 503 communicating with the inner cavity of the outer expansion area 2 is formed between the lower end of the inner tube 5 and the fragmentation plate 4. Specifically, the fragmentation plate 4 is connected to the lower end pipe orifice of the inner tube 5 through a plurality of connecting legs 502 distributed at intervals. The connecting legs 502 are strip-shaped rod structures. One end of the connecting leg 502 is fixedly connected to the lower end surface of the inner tube 5, and the other end of the connecting leg 502 is fixedly connected to the upper surface of the fragmentation plate 4. The number of the connecting legs 502 is 3 and they are evenly distributed along the circumferential direction of the inner tube 5. The gaps between the connecting legs 502 form the fluid channel 503. After the gas-liquid mixture flow impacts the fragmentation plate 4, it flows through the fluid channel 503 and deflects to the inner side wall of the outer expansion area 2. And the impact of the gas-liquid mixture flow on the fragmentation plate 4 drives the inner tube 5 to move up and down along the mixing channel 1, thereby adjusting the area of the liquid suction port 103 blocked by it. When the flow rate of the gas phase increases, the impact force of the gas phase on the fragmentation plate 4 increases. At this time, the height of the fragmentation plate 4 is less than the height of the fragmentation plate 4 before the increase in the gas phase flow rate, that is, the fragmentation plate 4 moves downward, thereby driving the inner tube 5 to move downward. Then the area of the liquid suction port 103 blocked by the inner tube 5 decreases, and the liquid inflow area of the liquid suction port 103 increases, thereby increasing the liquid inflow volume in the main pipe 102. That is, it can automatically adjust the liquid inflow volume in the main pipe 102 to match the gas phase flow rate and the liquid phase flow rate under different operating conditions. It should be noted that under the operating conditions of a given gas phase flow rate, the fluctuation of the gas phase flow rate is small, which will only cause the fragmentation plate 4 to vibrate with a small amplitude and high frequency, and will not cause the fragmentation plate 4 to vibrate with a large amplitude. Then the area of the liquid suction port 103 blocked by the inner tube 5 is also basically unchanged.

[0045] Embodiment 4

[0046] This embodiment is an improved solution based on Embodiment 3. Its main structure is the same as that of Embodiment 1. The improvement lies in that: a limiting groove 104 distributed along its axial direction is arranged on the side wall of the main pipe 102, and a limiting rod 501 connected to the outer side wall of the inner tube 5 is slidably arranged in the limiting groove 104. As Figure 7As shown, specifically, the number of the limiting rods 501 is 2 to 4. The limiting rods 501 are circular rod-shaped, the axis of the limiting rods 501 is perpendicular to the axis of the inner tube 5, and the limiting rods 501 are evenly distributed along the circumferential direction of the inner tube 5. The number of the limiting grooves 104 is 2 to 4. The number of the limiting rods 501 corresponds to that of the limiting grooves 104 one by one, and the limiting rods 501 are slidably arranged in the limiting grooves 104. The limiting grooves 104 are strip-shaped holes with semi-circular ends at both ends. The cooperation between the limiting grooves 104 and the limiting rods 501 can limit the extreme displacement of the inner tube 5.

[0047] Embodiment 5

[0048] This embodiment is an improved scheme based on Embodiment 4. Its main structure is the same as that of Embodiment 1. The improvement lies in that, as Figure 8 shown, the free end of the limiting rod 501 extends into the inner cavity of the outward expansion area 2, and the limiting rod 501 is connected to the top of the outward expansion area 2 through an elastic connecting rod 201. Specifically, the lower end of the main pipe 102 has an extension part extending into the inner cavity of the outward expansion area 2, and the limiting groove 104 is opened on the outer side wall of the extension part of the main pipe 102, that is, both the limiting rod 501 and the limiting groove 104 are located in the inner cavity of the outward expansion area 2. The free end of the limiting rod 501 passes through the limiting groove 104 and extends into the inner cavity of the outward expansion area 2. The elastic connecting rods 201 are arranged at intervals between the limiting rod 501 and the top of the outward expansion area 2. One end of the elastic connecting rod 201 is fixed on the inner side wall of the top of the outward expansion area 2, and the other end is fixed on the limiting rod 501. In this embodiment, the number of the elastic connecting rods 201 corresponds to that of the limiting rods 501 one by one.

[0049] Embodiment 6

[0050] A distribution component for gas-liquid multi-stage baffle mixing is installed in a hydrogenation reactor. The distribution component includes a distribution plate 6 with a plurality of distribution holes formed on its surface. Each distribution hole is provided with the distributor described in the above embodiments. The main pipe 102 of the distributor passes through the distribution hole and is vertically fixed on the distribution plate 6, and the outward expansion area 2 is located below the distribution plate 6, and the liquid suction port 103 is located above the distribution plate �. A liquid suction area 601 is formed between the liquid suction port 103 and the distribution plate 6. The liquid phase first accumulates on the distribution plate 6. When the liquid phase accumulates to a certain thickness on the distribution plate 6, due to the entry of high-speed gas into the main pipe 102, there is a pressure difference inside and outside the main pipe 102, and then the liquid phase enters the main pipe 102 through the liquid suction port 103.

[0051] Embodiment 7

[0052] A hydrogenation reactor for gas-liquid multi-stage baffle mixing has the distribution component described in Embodiment 6 above.

[0053] The foregoing description of the disclosed embodiments enables those skilled in the art to implement or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of the present invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A distributor for multiple gas-liquid cross-flow mixing, comprising a mixing channel (1), having a gas phase inlet (101) along the length direction of the mixing channel (1). When high-speed gas phase enters the mixing channel (1), negative pressure is generated to suck in liquid phase, and the gas phase and the liquid phase are mixed once to form a gas-liquid mixed flow, characterized in that: Below the mixing channel (1) there is an outward expansion area (2). The lower end opening of the outward expansion area (2) is closed by a bottom plate (3), and the bottom plate (3) is distributed with gas-liquid mixed flow outlets; inside the outward expansion area (2), a flow-breaking plate (4) is connected by an elastic connecting rod (201), and the edge of the flow-breaking plate (4) extends beyond the bottom of the mixing channel (1) and forms a variable clearance channel with the lower end of the mixing channel (1); the gas-liquid mixed flow formed by the mixing channel (1) impacts the flow-breaking plate (4) to achieve secondary mixing, and causes the flow-breaking plate (4) to vibrate, thereby causing the gas-liquid mixed flow to be deflected to the inner side wall of the outward expansion area (2) to achieve tertiary mixing, and being deflected by the inner side wall of the outward expansion area (2) to the bottom plate (3) to achieve quaternary mixing, and finally flowing out through the outlets on the bottom plate (3). The mixing channel (1) is a main pipe (102) with a closed top. The gas phase inlet (101) is opened on the side wall of the main pipe (102), and the side wall of the main pipe (102) is provided with a liquid suction port (103) that can allow the liquid phase to enter below the gas phase inlet (101). Inside the mixing channel (1), an inner pipe (5) that can reciprocate along the gas-liquid flow direction is provided. The flow-breaking plate (4) is connected to the lower end pipe orifice of the inner pipe (5), and a fluid channel (503) communicating with the inner cavity of the outward expansion area (2) is formed between the lower end of the inner pipe (5) and the flow-breaking plate (4). The mixing channel (1) has a liquid suction port (103) that can allow the liquid phase to enter below the gas phase inlet (101). The gas-liquid mixed flow impacts the flow-breaking plate (4) to drive the inner pipe (5) to move along the mixing channel (1), thereby adjusting the area of its occlusion of the liquid suction port (103).

2. The distributor for gas-liquid multi-stage baffle mixing according to claim 1, characterized in that: The diameter of the flow-breaking plate (4) is larger than the diameter of the main pipe (102) and smaller than the diameter of the outward expansion area (2). A flow deflection channel (401) is formed between the edge of the flow-breaking plate (4) and the inner side wall of the outward expansion area (2).

3. The distributor for gas-liquid multi-pass baffle mixing according to claim 1, characterized in that: Multiple convex ribs (402) are distributed on the upper surface of the flow-breaking plate (4), and the convex ribs (402) make the upper surface of the flow-breaking plate (4) form a corrugated shape.

4. The distributor for gas-liquid multi-pass baffle mixing according to claim 1, characterized in that: The bottom plate (3) includes a support ring (301) connected to the inner side wall of the outward expansion area (2). Multiple parallel strip-shaped rods (302) are arranged inside the support ring (301). There are slits (303) between adjacent two strip-shaped rods (302) to form the outlets of the gas-liquid mixed flow.

5. The distributor for gas-liquid multi-pass baffle mixing according to claim 1, wherein: The bottom plate (3) is a circular plate-like structure, and the bottom plate (3) is provided with outlets for the gas-liquid mixed flow.

6. The distributor for gas-liquid multi-stage baffle mixing according to claim 1, characterized in that: The flow-breaking plate (4) is connected to the bottom plate (3) through an elastic connecting rod (201).

7. The distributor for gas-liquid multi-stage baffle mixing according to claim 1, characterized in that: The inner pipe (5) is a cylindrical structure. The mixing channel (1) is formed by a cylindrical main pipe (102) with a closed top, and the top end of the inner pipe (5) extends to the liquid suction port (103).

8. The distributor for gas-liquid multi-stage baffled mixing according to claim 1, characterized in that: The flow-breaking plate (4) is connected to the lower end pipe orifice of the inner pipe (5) through multiple spaced connecting legs (502), and the gaps between the connecting legs (502) form a fluid channel (503).

9. The distributor for gas-liquid multi-stage baffle mixing according to claim 1, characterized in that: The side wall of the main pipe (102) is provided with a limiting groove (104) distributed along its axial direction, and a limiting rod (501) connected to the outer side wall of the inner pipe (5) is slidably arranged in the limiting groove (104).

10. A distributor for gas-liquid multi-stage baffled mixing according to claim 9, characterized in that: The free end of the limiting rod (501) extends into the inner cavity of the outward expansion area (2), and the limiting rod (501) is connected to the top of the outward expansion area (2) through an elastic connecting rod (201).

11. A distribution component for multiple gas-liquid baffle mixing, comprising a distribution plate (6) with a plurality of distribution holes formed on its surface, characterized in that: A distributor as described in any one of claims 1 to 10 is provided in each distribution hole. The main pipe (102) of the distributor passes through the distribution hole and is vertically fixed on the distribution plate (6). The outward expansion area (2) is located below the distribution plate (6), and the liquid suction port (103) is located above the distribution plate (6). A liquid suction area (601) is formed between the liquid suction port (103) and the distribution plate (6).

12. A hydrogenation reactor with multiple gas-liquid folding and mixing, characterized in that: This hydrogenation reactor has a distribution assembly as described in claim 11.

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