Upflow gas-liquid distributor, method of gas-liquid distribution, upflow reactor and its application, upflow hydrogenation reactor

Abstract

The present application relates to the technical field of petroleum chemical industry, in particular to an upflow gas-liquid distributor, a gas-liquid distribution method, an upflow reactor comprising the upflow gas-liquid distributor and application thereof, and an upflow hydrogenation reactor comprising the upflow reactor. The upflow gas-liquid distributor comprises, from bottom to top, a gas-liquid premixing component, at least one stage of gas-liquid dispersion component and a gas-liquid diffusion component which are sequentially communicated. The gas-liquid premixing component comprises an inner tube and an outer tube. The inner tube comprises a tube body and a liquid inlet, an inner tube gas hole and a liquid outlet arranged on the tube body. The outer tube comprises a main tube and a main tube gas hole arranged on the main tube. The tube body partially extends into the main tube, so that the liquid outlet is located inside the main tube. The upflow gas-liquid distributor enables efficient mixing, dispersion and mass transfer of gas and liquid. When the upflow gas-liquid distributor is used in an upflow reactor, the reaction efficiency is promoted by improving the gas-liquid mass transfer efficiency.

Description

Technical Field

[0001] This invention relates to the field of petrochemical technology, specifically to an upward-flowing gas-liquid distributor, a method for gas-liquid distribution, an upward-flowing reactor including the upward-flowing gas-liquid distributor and its application, and an upward-flowing hydrogenation reactor including the upward-flowing reactor. Background Technology

[0002] Compared with traditional downflow fixed-bed reactors, upflow reactors have advantages such as good adaptability to high-metal and low-quality raw materials, high reactor space utilization, and low pressure drop. However, they also have disadvantages such as uneven micro-expansion of the catalyst bed, which can easily lead to material flow deviation, causing temperature fluctuations in the catalyst bed, increased radial temperature difference, and the occurrence of hot spots.

[0003] In an upward-flowing reactor, both the gaseous and liquid phases of the reaction stream flow upwards. The liquid phase at the reactor outlet is continuous, while hydrogen is dispersed. Since hydrogen is supplied as dissolved hydrogen, to ensure stable hydrogen partial pressure and dissolution rate, the dissolved hydrogen in the liquid phase is always saturated, and a small amount of hydrogen exists in gaseous form. For gas-liquid two-phase mass transfer processes, especially liquid-phase hydrogenation processes where the reaction rate is much greater than the mass transfer rate, the mass transfer rate is crucial in determining the macroscopic reaction rate and thus becomes the controlling step. Increasing the mass transfer surface area can significantly improve the mass transfer rate; however, existing technologies have limited increases in mass transfer surface area due to the large bubble diameter, thus limiting the hydrogen dissolution rate and mass transfer efficiency.

[0004] CN205095759U discloses an upward-flowing gas-liquid distributor, which includes a guide pipe and mixing elements. Mixing elements are spaced apart above the upper opening of the guide pipe. The mixed fluid flowing through the guide pipe exits from the upper opening and reaches the mixing elements. However, this device only enhances the mixing between the gas and liquid phases through the mixing elements; it does not investigate technical parameters such as bubble size and distribution uniformity, nor the corresponding technical effects.

[0005] CN203737216U discloses an upward-flowing gas-liquid distributor for a multiphase flow reactor. The distributor comprises a rain cap, a distribution plate, a gas-liquid riser pipe, an inlet pipe, a connector, and baffles. This distributor effectively suppresses the generation of large bubbles, thereby improving the efficiency of gas-liquid mass transfer within the reactor. However, this distributor suffers from limitations such as limited operational flexibility.

[0006] CN202621143U discloses a gas-liquid distributor with a notch, comprising a distribution tube and a distribution plate. The upper end of the distribution tube is in fluid communication with the distribution plate, and the lower end of the distribution tube has an angled opening. The gas-liquid distributor also includes a baffle, with the angled opening connected to the baffle and the baffle covering the angled opening. A gas channel is provided on the wall of the distribution tube. Compared with the prior art, this distributor has advantages such as high gas-liquid distribution uniformity and large operational flexibility, but this structure lacks the function of radial gas diffusion.

[0007] CN211754819U discloses an upward-flowing gas-liquid distributor with packing material, comprising a coaxial and fixedly connected lower straight pipe section, a hyperbolic pipe, and an upper straight pipe section. The upper straight pipe section is filled with wire mesh corrugated packing material. The lower straight pipe section has a through hole, with the bottom opening of the lower straight pipe section serving as the inlet and the top opening of the upper straight pipe section as the outlet. However, this distributor lacks the function of radial gas diffusion; furthermore, it is unsuitable for hydrogenation processes such as those involving residual oil.

[0008] Therefore, there is an urgent need for an upward-flowing gas-liquid distributor that combines efficient gas-liquid mixing, dispersion, and mass transfer. Summary of the Invention

[0009] The purpose of this invention is to overcome the problems of poor gas-liquid mixing and dispersion, large bubble diameter, and limited radial dispersion in existing upward gas-liquid distributors. This invention provides an upward gas-liquid distributor, a gas-liquid distribution method, an upward reactor and its application, and an upward hydrogenation reactor. This upward gas-liquid distributor can achieve efficient gas-liquid mixing and generate microbubbles, thereby enhancing gas-liquid mass transfer efficiency. Simultaneously, the upward reactor containing this upward gas-liquid distributor is used for hydrogenation reactions, thereby improving reaction efficiency by enhancing gas-liquid mass transfer performance.

[0010] To achieve the above objectives, the first aspect of the present invention provides an upward gas-liquid distributor, which includes, from bottom to top, a gas-liquid premixing component, at least one gas-liquid dispersion component, and a gas-liquid diffusion component connected in sequence.

[0011] The gas-liquid premixing component includes an inner tube and an outer tube. The inner tube includes a tube body and a liquid phase inlet, an inner tube vent, and a liquid phase outlet disposed on the tube body. The outer tube includes a main tube and a main tube vent disposed on the main tube.

[0012] The tube body extends into the main tube, such that the liquid phase outlet is located inside the main tube.

[0013] Preferably, the inner tube vent is disposed on the tube wall of the tube body, and more preferably disposed on the tube wall of the tube body along the central axis.

[0014] Preferably, the inner tube vents are arranged in at least one row, preferably in 1-6 rows, and at least one row of the inner tube vents is located inside the main tube.

[0015] Preferably, the main vent is disposed on the wall of the main pipe, and more preferably disposed on the wall of the main pipe along the central axis.

[0016] Preferably, the main vent has at least one row, more preferably one to six rows, and the height of the main vent is lower than the height of the liquid phase outlet.

[0017] Preferably, the tube body comprises a lower tube and an upper tube that are connected, wherein the inner tube vent is respectively disposed on the tube wall of the lower tube and the upper tube.

[0018] Preferably, the main vent is disposed on the wall of the main pipe, and more preferably disposed on the wall of the main pipe along the central axis.

[0019] Preferably, the gas-liquid dispersion component comprises, from bottom to top: a connecting section-I, a narrowing section, a connecting section-II, and a widening section connected in sequence.

[0020] Preferably, in each stage of the gas-liquid dispersion component, the height ratio of the narrowing section to the expanding section is 1:0.2-3.

[0021] Preferably, the gas-liquid diffusion component includes: a connecting section-III and a bubble body connected in sequence, and a top outlet disposed on the bubble body.

[0022] A second aspect of the present invention provides a method for gas-liquid distribution, wherein the method performs gas-liquid distribution in an upward gas-liquid distributor provided in the first aspect;

[0023] The liquid phase entering from the liquid phase inlet and the gas phase entering from the inner tube vent and the main tube vent are initially premixed in the tube body from bottom to top, and then premixed again in the main tube. The resulting gas-liquid premix is ​​dispersed in the gas-liquid dispersion component, and the resulting gas-liquid dispersion is radially diffused in the gas-liquid diffusion component.

[0024] A third aspect of the present invention provides an upward reactor, the upward reactor comprising: at least one distribution plate and an upward gas-liquid distributor provided in the first aspect;

[0025] The distribution plate is disposed inside the upward reactor, and the lower surface of the distribution plate is provided with at least one hole-III;

[0026] The hole-III and the upward gas-liquid distributor are respectively provided, and each hole is independently connected to the top outlet of the upward gas-liquid distributor.

[0027] The fourth aspect of the present invention provides an application of the upward reactor provided in the third aspect in a hydrogenation reaction.

[0028] The fifth aspect of the present invention provides an upward hydrogenation reactor, the upward hydrogenation reactor comprising: the upward reactor provided in the third aspect.

[0029] Compared with the prior art, the present invention has the following advantages:

[0030] (1) The upward gas-liquid distributor provided by the present invention includes, from bottom to top, a gas-liquid premixing component, a gas-liquid dispersion component and a gas-liquid diffusion component connected in sequence, so as to achieve efficient mixing, dispersion and mass transfer of gas and liquid, that is, to achieve efficient mixing of gas phase and liquid phase, and to make gas phase efficiently dispersed in liquid phase as micro bubbles, so as to significantly improve gas-liquid mass transfer efficiency and promote reaction efficiency.

[0031] (2) The gas-liquid distribution method provided by the present invention is carried out in the upward gas-liquid distributor. Specifically, the gas and liquid phases are premixed (i.e., initial premixing and remixing) in a sleeve structure with inner and outer holes (i.e., gas-liquid premixing structure) to form a uniformly distributed gas-liquid premix that flows upward through a multi-stage gas-liquid dispersion component (especially the expansion section containing hole-I), thereby reducing the size of the bubbles to enhance the gas phase dispersion effect. Then, the gas and liquid phases are further dispersed and radially diffused in the gas-liquid diffusion component (especially the bubble cap containing hole-II), and finally overflow through the top outlet to form a uniform bubbling flow.

[0032] (3) The upward gas-liquid distributor provided by the present invention is used in an upward reactor so that the gas and liquid phases in the gas-liquid co-flow direction can achieve efficient mixing, dispersion and mass transfer. In particular, by limiting the number of holes-III of the distribution plate, the gas-liquid mass transfer efficiency is improved and the reaction efficiency is promoted.

[0033] (4) The upward reactor provided by the present invention can be used for hydrogenation reactions, especially suitable for hydrogenation reactions of gasoline, diesel, residual oil, wax oil and lubricating oil;

[0034] (5) Using the upward reactor provided by the present invention as an upward hydrogenation reactor can effectively improve the hydrogenation reaction rate by promoting efficient gas-liquid mixing, dispersion and mass transfer. Attached Figure Description

[0035] Figure 1 This is a schematic diagram of the first structure of the upward-moving gas-liquid distributor provided by the present invention;

[0036] Figure 2 This is a schematic diagram of the second structure of the upward-moving gas-liquid distributor provided by the present invention;

[0037] Figure 3This is a schematic diagram of the third structure of the upward-moving gas-liquid distributor provided by the present invention;

[0038] Figure 4A This is a schematic diagram of a first hole and a second hole provided by the present invention;

[0039] Figure 4B This is another structural schematic diagram of the first hole and the second hole provided by the present invention;

[0040] Figure 5 This is a schematic diagram of a structure of an upward hydrogenation reactor provided by the present invention;

[0041] Figure 6 It is a gas-liquid distributor as shown in Comparative Example 1.

[0042] Explanation of reference numerals in the attached figures

[0043] 21. Inner tube; 22. Outer tube; 23. Gas-liquid dispersion component

[0044] 24. Gas-liquid diffusion components

[0045] 1. Liquid inlet 2. Baffle 3. Lower pipe

[0046] 4. Inner tube vent; 5. Main tube; 6. Main tube vent

[0047] 7. Upper pipe; 8. Liquid phase outlet; 9. Connecting section - I

[0048] 10. Reduction section; 11. Connecting section-II; 12. Expansion section

[0049] 13. First hole portion; 14. Bubble cap body; 15. Connecting section-III

[0050] 16. Top outlet; 17. Second hole.

[0051] 31. Distribution plate; 32. Hole-III; 33. Raw material inlet.

[0052] 34. Raw material exports

[0053] 41. Gas-liquid inlet; 42. Ascending pipe; 43. Vent.

[0054] 44. Gas-liquid outlet Detailed Implementation

[0055] The endpoints and any values of the ranges disclosed herein are not limited to the exact range or value, and these ranges or values should be understood to include values close to these ranges or values. For numerical ranges, between the endpoint values of each range, between the endpoint values of each range and individual point values, and between individual point values can be combined with each other to obtain one or more new numerical ranges, and these numerical ranges shall be regarded as being specifically disclosed herein.

[0056] In the present invention, unless otherwise specified, "first" and "second" neither indicate a sequence of precedence, nor limit the respective materials or steps, and are only used to distinguish that they are not the same material or step. For example, "first" and "second" in "first hole portion" and "second hole portion" are only used to indicate that they are not the same hole portion.

[0057] In a first aspect, the present invention provides an upflow gas-liquid distributor, which comprises, from bottom to top, a gas-liquid premixing component, at least one stage of gas-liquid dispersing component and a gas-liquid diffusing component that are communicated in sequence;

[0058] Wherein, the gas-liquid premixing component comprises an inner tube and an outer tube, the inner tube comprises a tube body and a liquid phase inlet, inner tube air holes and a liquid phase outlet arranged on the tube body, and the outer tube comprises a main tube and main tube air holes arranged on the main tube;

[0059] Wherein, the tube body partially extends into the main tube, so that the liquid phase outlet is located inside the main tube.

[0060] In the present invention, unless otherwise specified, the gas-liquid premixing component, at least one stage of gas-liquid dispersing component and gas-liquid diffusing component communicated in sequence means that the outlet of the gas-liquid premixing component is connected to the inlet of the gas-liquid dispersing component, and the outlet of the gas-liquid dispersing component is connected to the inlet of the gas-liquid diffusing component.

[0061] In some embodiments of the present invention, preferably, the inner tube air holes are arranged on the tube wall of the tube body, preferably arranged on the tube wall of the tube body upward along the central axis. In the present invention, unless otherwise specified, that the inner tube air holes are arranged upward along the central axis means that the inner tube air holes are arranged on the tube wall of the tube body along the vertical direction, and the inner tube air holes are preferably on the same vertical line.

[0062] In some embodiments of the present invention, preferably, there are at least 1 row of the inner tube air holes, preferably 1 to 6 rows, and at least 1 row of the inner tube air holes is located inside the main tube. Such arrangement is used to generate bubble groups in the radial direction of the main tube to increase the radial range of the bubble groups.

[0063] In the present invention, unless otherwise specified, a row is used as a measurement unit for the inner tube air holes or the main tube air holes along the vertical direction.

[0064] In this invention, to improve the efficiency of gas-liquid mixing and dispersion, preferably, the number of air holes in each row of the inner tube is 1-12; more preferably, the air holes in each row are evenly distributed on the tube wall of the tube body, and the equivalent diameter of the air holes is 1-10 mm.

[0065] In this invention, unless otherwise specified, the number of air holes in each row refers to the number of air holes on the pipe wall of the pipe body on the same horizontal plane; the uniform distribution of air holes on the pipe wall of the pipe body means that the included angle between two adjacent air holes is the same on the same horizontal plane.

[0066] In one specific embodiment of the present invention, the inner tube vents are arranged along the central axis on the tube wall of the tube body, and the inner tube vents are arranged in 1-6 rows, with at least one row of the inner tube vents located inside the main tube; wherein, the number of the inner tube vents in each row is 1-12, and they are evenly distributed on the tube wall of the tube body; wherein, the equivalent diameter of the inner tube vents is 1-10 mm.

[0067] In some embodiments of the present invention, preferably, the main pipe vent is disposed on the wall of the main pipe, and more preferably disposed along the central axis on the wall of the main pipe. Wherein, "the main pipe vent is disposed along the central axis" means that the main pipe vent is disposed vertically on the wall of the main pipe, and preferably, the main pipe vents are on the same vertical line.

[0068] In some embodiments of the present invention, preferably, the main vent holes are arranged in at least one row, more preferably in 1-6 rows, and the height of the main vent holes is lower than the height of the liquid phase outlet. This arrangement is used to prevent or interfere with the formation of bubble clusters in the pipe body. Wherein, "the height of the main vent holes is lower than the height of the liquid phase outlet" means that, along the vertical direction, the height of the highest main vent hole is lower than the height of the liquid phase outlet.

[0069] In this invention, to improve the efficiency of gas-liquid mixing and dispersion, preferably, the number of main pipe vents in each row is 1-12; more preferably, the main pipe vents in each row are evenly distributed on the pipe wall of the main pipe, and the equivalent diameter of each main pipe vent is 1-10 mm.

[0070] In this invention, unless otherwise specified, the number of main pipe vents in each row refers to the number of main pipe vents located on the pipe wall of the main pipe on the same horizontal plane; the uniform distribution of main pipe vents on the pipe wall of the main pipe means that the included angle between two adjacent main pipe vents is the same on the same horizontal plane.

[0071] In one specific embodiment of the present invention, the main pipe vents are arranged along the central axis on the pipe wall of the main pipe, and the main pipe vents are arranged in 1-6 rows, and the height of the main pipe vents is lower than the height of the liquid phase outlet; wherein, the number of the main pipe vents in each row is 1-12, and they are evenly distributed on the pipe wall of the main pipe; wherein, the equivalent diameter of the main pipe vents is 1-10 mm.

[0072] In some embodiments of the present invention, preferably, the tube body comprises a lower tube and an upper tube that are connected, wherein the inner tube vents are respectively disposed on the tube walls of the lower tube and the upper tube. In the present invention, the number of rows of inner tube vents disposed on the tube walls of the lower tube and the upper tube is not limited, as long as the tube walls of the lower tube and the upper tube are provided with inner tube vents.

[0073] In some embodiments of the present invention, preferably, the outlet diameter of the lower pipe is less than the outlet diameter of the upper pipe, or the outlet diameter of the lower pipe is equal to the outlet diameter of the upper pipe, or the outlet diameter of the lower pipe is greater than the outlet diameter of the upper pipe.

[0074] In this invention, unless otherwise specified, the outlet diameter of the lower tube refers to the diameter of the upper surface of the lower tube; the outlet diameter of the upper tube refers to the diameter of the upper surface of the upper tube.

[0075] In some specific embodiments of the present invention, preferably, the outlet diameter ratio of the lower pipe and the upper pipe is 0.1-10:1, for example, 0.1:1, 0.5:1, 1:1, 1.5:1, 2:1, 3:1, 4:1, 5:1, 8:1, 10:1, and any value within the range of any two values, preferably 0.1-5:1, more preferably 0.5-2:1. The main purpose is to facilitate manufacturing using existing standard pipe fittings and reduce costs.

[0076] In some embodiments of the present invention, preferably, the height ratio of the lower tube to the upper tube is 0.1-10:1, for example, 0.1:1, 0.2:1, 0.5:1, 1:1, 2:1, 3:1, 5:1, 8:1, 10:1, and any value within the range of any two values, preferably 0.2-3:1.

[0077] In this invention, a wide range of types of upper and lower tubes can be selected. Preferably, the upper and lower tubes are each independently a regular or irregular shape, preferably a regular shape, more preferably selected from at least one of cylinder, frustum, cuboid, and cube, and most preferably a cylinder.

[0078] In some embodiments of the present invention, preferably, the cross-sections of the upper tube and the lower tube are each independently a regular shape or an irregular shape, preferably a regular shape, and more preferably selected from at least one of rectangle, square and trapezoid.

[0079] In this invention, unless otherwise specified, a cross section refers to a section along the central axis of the component.

[0080] In some embodiments of the present invention, preferably, the liquid phase inlet is disposed at the bottom of the tube body and the liquid phase outlet is disposed at the top of the tube body; more preferably, the liquid phase inlet is disposed at the bottom of the lower tube and the liquid phase outlet is disposed at the top of the upper tube.

[0081] In some embodiments of the present invention, preferably, the inner tube further includes a baffle connecting the lower tube and the liquid phase inlet; more preferably, the included angle α between the liquid phase inlet and the side of the baffle is ≤90°, and more preferably 60-90°.

[0082] In some embodiments of the present invention, preferably, the side of the baffle is provided with a hole-I, and the opening ratio is 10-80%; more preferably, the hole-I is selected from elongated holes and / or round holes.

[0083] In some embodiments of the present invention, preferably, the horizontal surface of the liquid inlet is provided with a hole-II, and the opening ratio is 5-30%; more preferably, the hole-II is selected from at least one of a triangular hole, a quadrilateral hole and a circular hole, and more preferably from at least one of an equilateral triangular hole, a square hole and a concentric circular hole.

[0084] In some embodiments of the present invention, the main tube is preferably a regular shape or an irregular shape, preferably a regular shape, more preferably selected from at least one of cylinder, frustum, cuboid and cube, and most preferably a cylinder.

[0085] In some embodiments of the present invention, preferably, the cross-section of the tube is a regular shape or an irregular shape, preferably a regular shape, more preferably selected from at least one of rectangle, square and trapezoid, and most preferably a rectangle.

[0086] In some embodiments of the present invention, preferably, the diameter ratio of the lower tube to the main tube is 1:2-25, for example, 1:2, 1:5, 1:8, 1:10, 1:15, 1:20, 1:25, and any value within the range of any two values, preferably 1:2-10.

[0087] In one specific embodiment of the present invention, preferably, the diameter of the tube body is 0.2-10 mm, and the diameter of the main tube is 20-50 mm. The diameter range of the tube body includes the diameter range of the lower tube and the diameter range of the upper tube.

[0088] In one specific embodiment of the present invention, when both the lower tube and the upper tube are cylindrical, the diameter ratio of the lower tube to the upper tube is 0.1-5:1; the diameter ratio of the lower tube to the main tube is 1:3-10; and the diameter ratio of the upper tube to the main tube is 1:2-10.

[0089] In some embodiments of the present invention, preferably, the ratio of the diameter of the liquid phase outlet to the inlet diameter of the upper pipe is 1:0.1-5, for example, 1:0.1, 1:0.5, 1:1, 1:2, 1:3, 1:4, 1:5, and any value within the range of any two values, preferably 1:1-4. Wherein, the ratio of the diameter of the liquid phase outlet to the inlet diameter of the upper pipe is equal to the ratio of the outlet diameters of the upper pipe and the lower pipe.

[0090] In some embodiments of the present invention, preferably, the ratio of the height of the tube extending into the main tube to the height of the main tube is 0.01-0.8:1, for example, 0.01:1, 0.1:1, 0.2:1, 0.3:1, 0.5:1, 0.8:1, and any value within the range of any two values, preferably 0.1-0.5:1.

[0091] In some embodiments of the present invention, preferably, the portion of the tube extending into the main tube is selected from at least a portion of the upper tube and optionally a portion of the lower tube, preferably from the upper tube. That is, the portion extending into the main tube can be a portion of the upper tube, the upper tube and a portion of the lower tube, or it can be only the upper tube.

[0092] In this invention, a multi-stage gas-liquid dispersion component is used to enhance the dispersion effect of the gas and liquid phases. Preferably, the gas-liquid dispersion component has 1-5 stages, for example, 1 stage, 2 stages, 3 stages, 4 stages, and 5 stages, preferably 1-3 stages.

[0093] In some embodiments of the present invention, preferably, the gas-liquid dispersion component comprises, from bottom to top: a connecting section-I, a narrowing section, a connecting section-II, and a widening section connected in sequence.

[0094] In some embodiments of the present invention, preferably, the ratio of the inner diameter of the reduced diameter section to the inner diameter of the main pipe is 0.1-0.8:1, for example, 0.1:1, 0.2:1, 0.4:1, 0.6:1, 0.8:1, and any value within the range of any two values, preferably 0.2-0.6:1; the ratio of the inner diameter of the expanded diameter section to the inner diameter of the main pipe is 1-3:1, for example, 1:1, 1.5:1, 2:1, 3:1, and any value within the range of any two values, preferably 1-2:1.

[0095] In some embodiments of the present invention, preferably, the height ratio of each stage of the gas-liquid dispersion component to the main pipe is 0.1-0.5:1, for example, 0.1:1, 0.2:1, 0.3:1, 0.5:1, and any value within the range of any two values, preferably 0.2-0.3:1. Wherein, the height of each stage of the gas-liquid dispersion component is the sum of the heights of connecting section-I, the narrowing section, connecting section-II, and the widening section.

[0096] In some embodiments of the present invention, preferably, in each stage of the gas-liquid dispersion component, the height ratio of the narrowing section to the expanding section is 1:0.2-3, for example, 1:0.2, 1:0.5, 1:0.6, 1:1, 1:1.5, 1:2, 1:3, and any value within the range of any two values, preferably 1:0.6-2.

[0097] In some embodiments of the present invention, more preferably, in each stage of the gas-liquid dispersion component, the height ratio of the connecting section-I, the narrowing section, the expanding section, and the connecting section-II is 0.1-0.5∶1∶0.2-3∶0.1-0.5, more preferably 0.2-0.3∶1∶0.6-2∶0.2-0.3. Using this preferred height ratio more effectively improves the ability of each component to generate bubble clusters while ensuring a relatively small distributor height.

[0098] In this invention, to further improve the dispersion effect of the gas-liquid two phases, preferably, the interior of the diameter-expanding section is provided with a first perforation; more preferably, the first perforation is selected from packing material and / or a porous plate.

[0099] In some embodiments of the present invention, preferably, the porosity of each of the first pores is independently ≥20%, preferably 50-99%; and the specific surface area is ≥200m². -1 Preferably 200-2000m -1 .

[0100] In one specific embodiment of the present invention, preferably, the filler is selected from wire mesh filler and / or corrugated filler; preferably, the perforated plate is selected from perforated plate, etc.

[0101] In one specific embodiment of the present invention, the structural schematic diagram of the first hole is shown below. Figure 4A As shown, by Figure 4A It can be seen that the first hole is filled with wire mesh, the material of which is selected from carbon steel and stainless steel, and the porosity is 50-99%.

[0102] In another specific embodiment of the present invention, the structural schematic diagram of the first hole is as follows: Figure 4B As shown, by Figure 4B It can be seen that the first hole is a porous plate, and the material is selected from carbon steel and stainless steel, with a porosity of 50-99%.

[0103] In some embodiments of the present invention, preferably, the gas-liquid diffusion component includes: a connecting section-III and a bubble body connected in sequence, and a top outlet disposed on the bubble body.

[0104] In some embodiments of the present invention, preferably, the blister pack is composed of sieve holes and / or sieve mesh; more preferably, the interior of the blister pack is provided with a second hole portion, the second hole portion being selected from filler and / or porous plate.

[0105] In this invention, the filler and the porous plate of the second hole are both as defined above, and will not be described in detail here.

[0106] In some embodiments of the present invention, preferably, the porosity of each of the second pores is independently ≥20%, more preferably 50-99%; and the specific surface area is ≥200m². -1 Preferably 200-2000m -1 .

[0107] In one specific embodiment of the present invention, preferably, the filler is selected from wire mesh filler and / or corrugated filler; preferably, the perforated plate is selected from perforated plate, etc.

[0108] In one specific embodiment of the present invention, the structural schematic diagram of the second hole is shown below. Figure 4A As shown, by Figure 4A It can be seen that the second pore is filled with wire mesh, the material of which is selected from carbon steel and stainless steel, and the porosity is 50-99%.

[0109] In another specific embodiment of the present invention, the structural schematic diagram of the second hole is as follows: Figure 4B As shown, by Figure 4B It can be seen that the second hole is a porous plate, made of carbon steel or stainless steel, with a porosity of 50-99%.

[0110] In some embodiments of the present invention, the blister pack is preferably a regular shape and / or an irregular shape, preferably a regular structure, and more preferably selected from at least one of cylinder, hemisphere, cuboid and cube.

[0111] In some embodiments of the present invention, preferably, the cross-section of the blister pack is a regular shape or an irregular shape, preferably a regular shape, and more preferably selected from at least one of rectangle, square, trapezoid and semicircle.

[0112] In this invention, the liquid phase inlet, lower pipe, upper pipe, main pipe, liquid phase outlet, narrowing section, widening section, and top outlet are each independently connected by movable parts; wherein, the movable parts include, but are not limited to, threads.

[0113] A schematic diagram of the first upward-moving gas-liquid distributor provided by this invention is shown below. Figure 1 As shown, by Figure 1 It can be seen that the upward-flowing gas-liquid distributor includes, from bottom to top: a gas-liquid premixing component, a primary gas-liquid dispersion component 23, and a gas-liquid diffusion component 24 connected in sequence; the gas-liquid premixing component includes an inner tube 21 and an outer tube 22, wherein the inner tube 21 includes: a lower tube 3 and an upper tube 7 connected in series, an inner tube vent 4 provided on the tube walls of the lower tube 3 and the upper tube 7, a liquid phase inlet 1 provided at the bottom of the lower tube 3, a liquid phase outlet 8 provided at the top of the upper tube 7, and a baffle 2 connecting the lower tube 3 and the liquid phase inlet 1; the outer tube 22 includes: a main tube 5 and a main tube vent 6 provided on the tube wall of the main tube 5;

[0114] The upper pipe 7 extends into the interior of the main pipe 5, so that the liquid phase outlet 8 is located inside the main pipe 5; the outlet diameter of the lower pipe 3 is greater than the outlet diameter of the upper pipe 7; the cross-section of the lower pipe 3 is rectangular, and the cross-section of the upper pipe 7 is trapezoidal; the included angle α between the liquid phase inlet 1 and the baffle 2 is 90°.

[0115] Among them, at least one row of inner tube vents 4 is located inside the main tube 5; the height of the main tube vents 6 is lower than the height of the liquid phase inlet 8;

[0116] The gas-liquid dispersion component 23 includes, from bottom to top: a connecting section-I 9, a narrowing section 10, a connecting section-II 11, and an expanding section 12 connected in sequence; wherein, the expanding section 12 has a first hole 13 inside;

[0117] The gas-liquid diffusion component 24 includes: a connecting section-III 15 and a bubble body 14 connected in sequence, and a top outlet 16 disposed on the bubble body 14; a second hole 17 is disposed inside the bubble body 14; the cross-section of the bubble body 14 is rectangular.

[0118] A schematic diagram of the second type of upward-moving gas-liquid distributor provided by the present invention is shown below. Figure 2 As shown, by Figure 2 It can be seen that the upward-flowing gas-liquid distributor includes, from bottom to top: a gas-liquid premixing component, a secondary gas-liquid dispersion component 23, and a gas-liquid diffusion component 24 connected in sequence; the gas-liquid premixing component includes an inner tube 21 and an outer tube 22, wherein the inner tube 21 includes: a lower tube 3 and an upper tube 7 connected in series, an inner tube vent 4 provided on the tube walls of the lower tube 3 and the upper tube 7, a liquid phase inlet 1 provided at the bottom of the lower tube 3, a liquid phase outlet 8 provided on the upper tube 7, and a baffle 2 connecting the lower tube 3 and the liquid phase inlet 1; the outer tube 22 includes: a main tube 5 and a main tube vent 6 provided on the tube wall of the main tube 5;

[0119] The upper pipe 7 extends into the interior of the main pipe 5, so that the liquid phase outlet 8 is located inside the main pipe 5; the outlet diameter of the lower pipe 3 is less than the outlet diameter of the upper pipe 7; the cross-section of the lower pipe 3 is rectangular, and the cross-section of the upper pipe 7 is an inverted trapezoid; the included angle α between the liquid phase inlet 1 and the side of the baffle 2 is less than 90°.

[0120] Among them, at least one row of inner tube vents 4 is located inside the main tube 5; the height of the main tube vents 6 is lower than the height of the liquid phase inlet 8;

[0121] Each gas-liquid dispersion component 23 includes, from bottom to top: a connecting section-I 9, a narrowing section 10, a connecting section-II 11, and an expanding section 12 connected in sequence; wherein, the expanding section 12 is provided with a first hole 13 inside;

[0122] The gas-liquid diffusion component 24 includes: a connecting section-III 15 and a bubble body 14 connected in sequence, and a top outlet 16 disposed on the bubble body 14; a second hole 17 is disposed inside the bubble body 14; the cross-section of the bubble body 14 is semi-circular.

[0123] The structural schematic diagram of the third type of upward-moving gas-liquid distributor provided by the present invention is shown below. Figure 3 As shown, by Figure 3 It can be seen that the upward-flowing gas-liquid distributor includes, from bottom to top: a gas-liquid premixing component, a three-stage gas-liquid dispersion component 23, and a gas-liquid diffusion component 24 connected in sequence; the gas-liquid premixing component includes an inner tube 21 and an outer tube 22, wherein the inner tube 21 includes: a lower tube 3 and an upper tube 7 connected in series, an inner tube vent 4 provided on the tube walls of the lower tube 3 and the upper tube 7, a liquid phase inlet 1 provided at the bottom of the lower tube 3, a liquid phase outlet 8 provided at the upper tube 7, and a baffle 2 connecting the lower tube 3 and the liquid phase inlet 1; the outer tube 22 includes: a main tube 5 and a main tube vent 6 provided on the main tube 5;

[0124] The upper pipe 7 extends into the main pipe 5, so that the liquid phase outlet 8 is located inside the main pipe 5; the outlet diameter of the lower pipe 3 is equal to the outlet diameter of the upper pipe 7; the cross-sections of both the lower pipe 3 and the upper pipe 7 are rectangular; the included angle α between the liquid phase inlet 1 and the side of the baffle 2 is less than 90°.

[0125] Among them, at least one row of inner tube vents 4 is located inside the main tube 5; the height of the main tube vents 6 is lower than the height of the liquid phase inlet 8;

[0126] Each gas-liquid dispersion component 23 includes, from bottom to top: a connecting section-I 9, a narrowing section 10, a connecting section-II 11, and an expanding section 12 connected in sequence; wherein, the expanding section 12 is provided with a first hole 13 inside;

[0127] The gas-liquid diffusion component 24 includes a connecting section-III 15 and a bubble body 14 connected in sequence, and a top outlet 16 disposed on the bubble body 14; a second hole 17 is disposed inside the bubble body 14; the cross-section of the bubble body 14 is an inverted trapezoid.

[0128] A second aspect of the present invention provides a method for gas-liquid distribution, wherein the method performs gas-liquid distribution in an upward gas-liquid distributor provided in the first aspect;

[0129] The liquid phase entering from the liquid phase inlet and the gas phase entering from the inner tube vent and the main tube vent are initially premixed in the tube body from bottom to top, and then premixed again in the main tube. The resulting gas-liquid premix is ​​dispersed in the gas-liquid dispersion component, and the resulting gas-liquid dispersion is radially diffused in the gas-liquid diffusion component.

[0130] In some embodiments of the present invention, preferably, m 3 The liquid phase and m 3 The calculated flow rate ratio of the gas phase is 0.1-5∶2-30, preferably 0.2-1∶3-10. That is, relative to a flow rate of 0.1-5 m³ / s... 3 The flow rates of the liquid and gas phases are 2-30 m³ / s. 3 .

[0131] In some embodiments of the present invention, preferably, the feed rate of the liquid phase is 0.2-1 m / s. 3 / h, for example, 0.2, 0.3, 0.4, 0.5, 0.8, 1, and any value within the range of any two values, preferably 0.2-0.5m. 3 / h.

[0132] In some embodiments of the present invention, preferably, the space velocity of the gas phase is 2-15 h⁻¹. -1For example, 2, 3, 4, 5, 8, 10, 12, 15, and any value within a range of any two values, preferably 3-5h. -1 .

[0133] In some embodiments of the present invention, preferably, the flow rate ratio of the gas phase through the inner tube vent and the main tube vent is 0.1-2:3-10, more preferably 0.5-1:3-5. By adjusting the flow rate ratio of the inner tube vent and the main tube vent, gas-liquid phase mixing can be effectively promoted and bubble cluster formation can be facilitated.

[0134] A third aspect of the present invention provides an upward reactor, the upward reactor comprising: at least one distribution plate and an upward gas-liquid distributor provided in the first aspect;

[0135] The distribution plate is disposed inside the upward reactor, and the lower surface of the distribution plate is provided with at least one hole-III;

[0136] The hole-III and the upward gas-liquid distributor are respectively provided, and each hole-III is independently connected to the top outlet of the upward gas-liquid distributor.

[0137] In some embodiments provided by the present invention, preferably, the number of distribution disks is 1-5, and more preferably 1-3.

[0138] In some embodiments provided by the present invention, preferably, the ratio of the vertical distance between two adjacent distribution discs to the height of the upward gas-liquid distributor is 1-50:1, for example, 1:1, 2:1, 5:1, 10:1, 15:1, 20:1, and any value within the range of any two values, preferably 2-20:1.

[0139] In some embodiments provided by the present invention, preferably, the height ratio of the distribution disk and the upward gas-liquid distributor is 0.01-0.5∶1, for example, 0.01∶1, 0.05∶1, 0.1∶1, 0.2∶1, 0.3∶1, 0.5∶1, and any value within the range of any two values, preferably 0.05-0.5∶1. Wherein, the height of the distribution disk refers to the vertical distance between the upper and lower surfaces of the distribution disk; the height of the upward gas-liquid distributor refers to the sum of the height of the gas-liquid premixing component, the height of at least one stage of gas-liquid dispersion component, and the height of the gas-liquid diffusion component.

[0140] In some embodiments of the present invention, preferably, the number of holes-III is 1-10, more preferably 1-5.

[0141] In some embodiments of the present invention, preferably, the holes-III are uniformly distributed on the lower surface of the distribution disk.

[0142] In some embodiments of the present invention, preferably, the upward reactor further includes a raw material inlet and a raw material outlet, wherein the raw material inlet is located at the bottom of the upward reactor and the raw material outlet is located at the top of the upward reactor.

[0143] A schematic diagram of an upward-flowing reactor provided by this invention is shown below. Figure 5 As shown, the upward reactor includes: two distribution disks 31, which are disposed inside the upward reactor, and each distribution disk 31 has three holes-III 32 evenly distributed on its lower surface;

[0144] Among them, hole-III 32 and the upward gas-liquid distributor are respectively provided, and hole-III 32 is independently connected to the top outlet of the upward gas-liquid distributor;

[0145] It also includes a raw material inlet 33 located at the bottom of the upward reactor and a raw material outlet 34 located at the top of the upward reactor.

[0146] The fourth aspect of the present invention provides an application of the upward reactor provided in the third aspect in a hydrogenation reaction.

[0147] The upward-flowing gas-liquid distributor provided by this invention can be used in upward-flowing reactors for gas-liquid two-phase dispersion, especially for hydrogenation reactions of gasoline, diesel, residual oil, wax oil and lubricating oil.

[0148] The fifth aspect of the present invention provides an upward hydrogenation reactor, the upward hydrogenation reactor comprising: the upward reactor provided in the fourth aspect.

[0149] In some embodiments of the present invention, preferably, the upward reactor provided in the fourth aspect is used as an upward hydrogenation reactor.

[0150] According to a particularly preferred embodiment of the present invention, an upward gas-liquid distributor includes, from bottom to top: a gas-liquid premixing component, at least one gas-liquid dispersion component, and a gas-liquid diffusion component connected in sequence.

[0151] The gas-liquid premixing component includes an inner tube and an outer tube. The inner tube includes a tube body and a liquid phase inlet, an inner tube vent, and a liquid phase outlet disposed on the tube body. The outer tube includes a main tube and a main tube vent disposed on the main tube.

[0152] The tube body extends into the main tube, such that the liquid phase outlet is located inside the main tube;

[0153] The tube body includes a lower tube and an upper tube that are connected to each other. The inner tube vents are respectively disposed on the tube walls of the lower tube and the upper tube along the central axis. The inner tube vents are arranged in 1-6 rows, and at least one row of the inner tube vents is located inside the main tube.

[0154] The main vent is arranged along the central axis upward on the pipe wall of the pipe body; the main vent is arranged in 1-6 rows, and the height of the main vent is lower than the height of the liquid phase outlet;

[0155] The gas-liquid dispersion component comprises, from bottom to top: a connecting section-I, a narrowing section, a connecting section-II, and a widening section connected in sequence; the widening section has a first hole inside.

[0156] The gas-liquid diffusion component includes: a connecting section-III and a bubble body connected in sequence, and a top outlet disposed on the bubble body; the bubble body has a second hole inside;

[0157] The porosity of the first and second pores is independently 50-99%; the specific surface area is independently 200-2000 m². -1 .

[0158] The present invention will be described in detail below through embodiments.

[0159] Gas holdup parameter measurement process: The initial liquid level height and the liquid level height after bubbling are measured using the volume expansion method, and the gas holdup E in the liquid phase is calculated. a The calculation formula is as follows:

[0160]

[0161] In Equation I, H i H represents the initial liquid level height. n This refers to the liquid level height after bubbling.

[0162] Bubble diameter parameter measurement process: The diameter of bubbles in the cross-section of the liquid is measured, and the average bubble diameter is used to represent the mixing effect between the gas and liquid phases. During the measurement process, it is assumed that all bubbles are spherical, and the equivalent diameter d of the bubble can be represented by the Sauter chord length of the bubble. 32 The calculation formula is as follows:

[0163]

[0164] In Equation II, n i For a diameter of d i The number of bubbles; N is the total number of bubbles counted.

[0165] The gas holdup parameters and bubble diameter parameters of Examples 1-3 and Comparative Example 1 are listed in Table 1.

[0166] Example 1

[0167] A schematic diagram of the upward-flowing gas-liquid distributor is shown below. Figure 1 As shown, by Figure 1 It can be seen that the upward-flowing gas-liquid distributor includes, from bottom to top: a gas-liquid premixing component, a primary gas-liquid dispersion component 23, and a gas-liquid diffusion component 24 connected in sequence; the gas-liquid premixing component includes an inner tube 21 and an outer tube 22. The inner tube 21 includes: a liquid inlet 1, a baffle 2, a lower tube 3, an inner tube vent 4, an upper tube 7, and a liquid outlet 8. The outer tube 22 includes: a main tube 5 and a main tube vent 6; wherein, the upper tube 7 extends into the interior of the main tube 5; the gas-liquid dispersion component 23 includes, from bottom to top: a connecting section-I 9, a narrowing section 10, a connecting section-II 11, and an expanding section 12 connected in sequence. The expanding section 12 has a first orifice 13 inside; the gas-liquid diffusion component 24 includes: a connecting section-III 15 and a bubble body 14 connected in sequence, and a top outlet 16 provided on the bubble body 14; the bubble body 14 has a second orifice 17 inside; the cross-section of the bubble body 14 is rectangular.

[0168] The lower tube 3 is cylindrical with an outlet diameter of 5 mm, and the upper tube 7 is frustum-shaped with a liquid phase outlet diameter of 0.5 mm; the height ratio of the lower tube 3 to the upper tube 7 is 1:1.

[0169] Among them, the lower tube 3 and the upper tube 7 each have two rows of inner tube vent holes 4, with 6 holes in each row, evenly distributed on the tube wall. The diameter of the inner tube vent holes 4 is 2mm.

[0170] The upper tube 7 extends into the interior of the main tube 5, and the height ratio of the upper tube 7 to the main tube 5 is 0.4:1.

[0171] Among them, the main pipe 5 is a cylinder with a diameter of 20mm, and the main pipe vent 6 has 3 rows of 12 vents in each row, which are evenly distributed on the pipe wall of the main pipe. The diameter of the main pipe vent 6 is 2mm.

[0172] The included angle α between the side of liquid inlet 1 and baffle 2 is 90°. The side of baffle 2 is provided with hole-I (circular hole) with an opening rate of 30%. The horizontal surface of liquid inlet 1 is provided with hole-II (equilateral triangular hole) with an opening rate of 10%.

[0173] The narrowing section 10 has a diameter of 10 mm and a height of 25 mm; the widening section 12 has a diameter of 30 mm and a height of 20 mm; the first aperture 13 is filled with wire mesh with a porosity of 80% and a specific surface area of ​​300 m². -1 ;

[0174] The second pore section 17 is filled with wire mesh with a porosity of 85% and a specific surface area of ​​300 m². -1 .

[0175] Gas-liquid distribution method:

[0176] In the above-mentioned upward gas-liquid distributor, the method includes: the liquid phase entering from the liquid phase inlet 1 and the gas phase entering from the inner tube vent 4 and the main tube vent 6 are initially premixed from bottom to top in the lower tube 3 and the upper tube 7, and then premixed again in the main tube 5. The resulting gas-liquid premix is ​​dispersed in the gas-liquid dispersion component 23, and the resulting gas-liquid dispersion is radially diffused in the gas-liquid diffusion component 24.

[0177] The ratio of liquid to gas phase is 1:5, and the feed rate of the liquid phase is 0.4 m / s. 3 / h, the gas phase space velocity is 5h -1 The flow rate ratio of the gas phase through the inner tube vent and the main tube vent is 1:3.

[0178] Example 2

[0179] A schematic diagram of the upward-flowing gas-liquid distributor is shown below. Figure 2 As shown, by Figure 2 It can be seen that the upward-flowing gas-liquid distributor includes, from bottom to top: a gas-liquid premixing component, a secondary gas-liquid dispersion component 23, and a gas-liquid diffusion component 24 connected in sequence; the gas-liquid premixing component includes an inner tube 21 and an outer tube 22. The inner tube 21 includes: a liquid inlet 1, a baffle 2, a lower tube 3, an inner tube vent 4, an upper tube 7, and a liquid outlet 8. The outer tube 22 includes: a main tube 5 and a main tube vent 6; wherein, the upper tube 7 extends into the interior of the main tube 5; the gas-liquid dispersion component 23 includes, from bottom to top: a connecting section-I 9, a narrowing section 10, a connecting section-II 11, and an expanding section 12 connected in sequence. The expanding section 12 has a first orifice 13 inside; the gas-liquid diffusion component 24 includes: a connecting section-III 15 and a bubble body 14 connected in sequence, and a top outlet 16 provided on the bubble body 14; the bubble body 14 has a second orifice 17 inside; the cross-section of the bubble body 14 is semi-circular.

[0180] The lower tube 3 is cylindrical with an outlet diameter of 5 mm, and the upper tube 7 is frustum-shaped with a liquid phase outlet diameter of 15 mm; the height ratio of the lower tube 3 to the upper tube 7 is 2:1.

[0181] Among them, the lower tube 3 and the upper tube 7 each have two rows of inner tube vent holes 4, with 6 holes in each row, evenly distributed on the inner tube wall, and the diameter of the inner tube vent holes 4 is 5mm.

[0182] The upper tube 7 extends into the interior of the main tube 5, and the height ratio of the upper tube 7 to the main tube 5 is 0.5:1.

[0183] Among them, the main pipe 5 is a cylinder with a diameter of 20mm, and the main pipe vent 6 has 3 rows of 12 vents in each row, which are evenly distributed on the pipe wall of the main pipe. The diameter of the main pipe vent 6 is 2mm.

[0184] The included angle α between the side of liquid inlet 1 and baffle 2 is less than 90°. The side of baffle 2 is provided with hole-I (circular hole) with an opening rate of 50%. The horizontal surface of liquid inlet 1 is provided with hole-II (equilateral triangular hole) with an opening rate of 15%.

[0185] The two narrowing sections 10 each have a diameter of 10 mm and a height of 20 mm; the two expanding sections 12 each have a diameter of 30 mm and a height of 20 mm; the first aperture 13 is filled with wire mesh with a porosity of 90% and a specific surface area of ​​1000 m². -1 ;

[0186] The second pore section 17 is filled with wire mesh with a porosity of 95% and a specific surface area of ​​1500 m². -1 .

[0187] Gas-liquid distribution method:

[0188] In the above-mentioned upward gas-liquid distributor, the method includes: the liquid phase entering from the liquid phase inlet 1 and the gas phase entering from the inner tube vent 4 and the main tube vent 6 are pre-mixed from bottom to top in the lower tube 3 and the upper tube 7, and then pre-mixed in the main tube 5. The resulting gas-liquid premix is ​​dispersed in the gas-liquid dispersion component 23, and the resulting gas-liquid dispersion is radially diffused in the gas-liquid diffusion component 24.

[0189] The flow rate ratio of the liquid phase to the gas phase is 1:5, and the feed rate of the liquid phase is 0.4 m / s. 3 / h, the gas phase space velocity is 5h -1 The flow rate ratio of the gas phase through the inner tube vent and the main tube vent is 1:3.

[0190] Example 3

[0191] A schematic diagram of the upward-flowing gas-liquid distributor is shown below. Figure 3 As shown, by Figure 3It can be seen that the upward-flowing gas-liquid distributor includes, from bottom to top: a gas-liquid premixing component, a three-stage gas-liquid dispersion component 23, and a gas-liquid diffusion component 24 connected in sequence; the gas-liquid premixing component includes an inner tube 21 and an outer tube 22. The inner tube 21 includes: a liquid inlet 1, a baffle 2, a lower tube 3, an inner tube vent 4, an upper tube 7, and a liquid outlet 8. The outer tube 22 includes: a main tube 5 and a main tube vent 6; wherein, the upper tube 7 extends into the interior of the main tube 5; the gas-liquid dispersion component 23 includes, from bottom to top: a connecting section-I 9, a narrowing section 10, a connecting section-II 11, and an expanding section 12 connected in sequence. The expanding section 12 has a first orifice 13 inside; the gas-liquid diffusion component 24 includes: a connecting section-III 15 and a bubble body 14 connected in sequence, and a top outlet 16 provided on the bubble body 14; the bubble body 14 has a second orifice 17 inside; the cross-section of the bubble body 14 is an inverted trapezoid.

[0192] Both the lower tube 3 and the upper tube 7 are cylinders with a diameter of 5mm; the height ratio of the lower tube 3 to the upper tube 7 is 0.5:1.

[0193] Among them, the lower tube 3 and the upper tube 7 each have 2 rows of inner tube vent holes 4, with 6 holes in each row, evenly distributed on the inner tube wall, and the diameter of the inner tube vent holes 4 is 2mm.

[0194] The upper tube 7 extends into the interior of the main tube 5, and the height ratio of the upper tube 7 to the main tube 5 is 0.5:1.

[0195] Among them, the main pipe 5 is a cylinder with a diameter of 50mm, and the main pipe vent 6 has 3 rows of 12 holes each, which are evenly distributed on the pipe wall of the main pipe. The diameter of the main pipe vent 6 is 2mm.

[0196] The included angle α between the side of liquid inlet 1 and baffle 2 is less than 90°. The side of baffle 2 is provided with hole-I (circular hole) with an opening rate of 80%. The horizontal surface of liquid inlet 1 is provided with hole-II (equilateral triangular hole) with an opening rate of 30%.

[0197] The three narrowing sections 10 each have a diameter of 10 mm and a height of 20 mm; the two expanding sections 12 each have a diameter of 50 mm and a height of 10 mm; the first pore section 13 is filled with wire mesh with a porosity of 98% and a specific surface area of ​​2000 m². -1 ;

[0198] The second pore section 17 is filled with wire mesh with a porosity of 98% and a specific surface area of ​​2000 m². -1 .

[0199] Gas-liquid distribution method:

[0200] In the above-mentioned upward gas-liquid distributor, the method includes: the liquid phase entering from the liquid phase inlet 1 and the gas phase entering from the inner tube vent 4 and the main tube vent 6 are initially premixed from bottom to top in the lower tube 3 and the upper tube 7, and then premixed again in the main tube 5. The resulting gas-liquid premix is ​​dispersed in the gas-liquid dispersion component 23, and the resulting gas-liquid dispersion is radially diffused in the gas-liquid diffusion component 24.

[0201] The flow rate ratio of the liquid phase to the gas phase is 1:5, and the feed rate of the liquid phase is 0.4 m / s. 3 / h, the gas phase space velocity is 5h -1 The flow rate ratio of the gas phase through the inner tube vent and the main tube vent is 1:3.

[0202] Comparative Example 1

[0203] A schematic diagram of the gas-liquid distributor is shown below. Figure 6 As shown, by Figure 6 It can be seen that the gas-liquid distributor includes: a gas-liquid inlet 41, a riser pipe 42, two gas holes 43, and a gas-liquid outlet 44;

[0204] The riser pipe has an inner diameter of 50mm and a length of 100mm.

[0205] Among them, the vent 43 is located in the middle of the riser pipe, and the diameter of the vent 43 is 5mm;

[0206] The top structure of the riser is a perforated plate with 20 holes, each 3mm in diameter.

[0207] Gas-liquid distribution method:

[0208] In the above-mentioned gas-liquid distributor, the liquid phase directly enters the riser pipe from the gas-liquid inlet 41, and part of the gas phase enters from the gas-liquid inlet 41 and part of the gas phase enters from the gas hole 43. After the two are mixed, they move upward and form bubbles at the middle opening, which overflow directly from the top into the upward reactor.

[0209] The flow rate ratio of the liquid phase to the gas phase is 1:5, and the feed rate of the liquid phase is 0.4 m / s. 3 / h, the gas phase space velocity is 5h -1 The flow rate ratio of the gas phase through the gas-liquid inlet and the gas pore is 1:3.

[0210] Table 1

[0211] Comparative Example 1 4.149 7.43 Example 1 6.251 2.13 Example 2 6.947 1.76 Example 3 7.511 1.14

[0212] As shown in Table 1, compared to Comparative Example 1, the gas-liquid distributors of Examples 1-3 provided by this invention all have higher gas holdup and better distribution performance; that is, the gas holdup E aThe larger the parameter, the better the gas-liquid distribution performance. Compared with Comparative Example 1, the gas-liquid distributor provided by this invention can provide a greater mass transfer driving force, thereby improving the mass transfer rate; in particular, the more stages the gas-liquid dispersion components have, the more beneficial it is to improve the mass transfer rate.

[0213] As shown in Table 1, the average bubble diameter of the gas-liquid distributor in Comparative Example 1 is 7.43 mm, while the bubble diameter of the gas-liquid distributors in Examples 1-3 is between 1-2 mm. This indicates that the gas-liquid distributor provided by this invention has a smaller bubble diameter d and better dispersion performance. This demonstrates that the gas-liquid distributor provided by this invention has a slightly better mixing effect than the gas-liquid distributor in Comparative Example 1, especially since the more stages of the gas-liquid dispersion components (i.e., the more diameter-reducing and diameter-expanding sections), the more effectively the dispersion effect between the gas and liquid phases is enhanced, resulting in smaller bubble diameters.

[0214] In upward-flowing gas-liquid two-phase reactions, generally speaking, a smaller bubble diameter (d) is more conducive to increasing the gas-liquid mass transfer surface area and prolonging the bubble residence time, both of which enhance mass transfer efficiency. For hydrogenation reactions, this translates to increased contact time between the hydrogen and oil components, further improving mass transfer and reaction rates between the gas and liquid phases. Therefore, minimizing bubble size is beneficial for both upward-flowing and all-liquid-phase hydrogenation processes from any perspective.

[0215] 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. An upward-flowing gas-liquid distributor, characterized in that, The upward-flowing gas-liquid distributor comprises, from bottom to top: a gas-liquid premixing component, at least one gas-liquid dispersion component, and a gas-liquid diffusion component connected in sequence; The gas-liquid premixing component includes an inner tube and an outer tube. The inner tube includes a tube body and a liquid phase inlet, an inner tube vent, and a liquid phase outlet disposed on the tube body. The outer tube includes a main tube and a main tube vent disposed on the tube wall of the main tube. The tube body extends into the main tube, such that the liquid phase outlet is located inside the main tube; The height of the main vent is lower than the height of the liquid phase outlet; The inner tube vent is disposed on the tube wall of the tube body; the inner tube vent is arranged in 1-6 rows, and at least one row of the inner tube vent is located inside the main tube; The ratio of the height of the tube portion extending into the main tube to the height of the main tube is 0.1-0.5:1; The gas-liquid dispersion component comprises, from bottom to top: a connecting section-I, a narrowing section, a connecting section-II, and a widening section connected in sequence, wherein the widening section has a first hole inside; The gas-liquid diffusion component includes: a connecting section-III and a bubble body connected in sequence, and a top outlet disposed on the bubble body. The bubble body is composed of a screen, and a second hole is disposed inside the bubble body.

2. The upward-flowing gas-liquid distributor according to claim 1, wherein, The inner tube vent is arranged along the central axis upward on the tube wall of the tube body; The number of air holes in each row of the inner tube is 1-12, and the air holes in each row are evenly distributed on the tube wall of the tube body.

3. The upward-flowing gas-liquid distributor according to claim 1, wherein, The main vent is provided along the central axis upward on the pipe wall of the main pipe; The main air vent has at least one row; The number of main pipe vents in each row is 1-12, and the main pipe vents in each row are evenly distributed on the pipe wall of the main pipe.

4. The upward-flowing gas-liquid distributor according to claim 3, wherein, The main vent has 1-6 rows.

5. The upward-flowing gas-liquid distributor according to claim 1 or 2, wherein, The tube body includes a lower tube and an upper tube that are connected, wherein the inner tube vents are respectively disposed on the tube walls of the lower tube and the upper tube.

6. The upward-flowing gas-liquid distributor according to claim 5, wherein, The outlet diameter of the lower pipe is less than the outlet diameter of the upper pipe, or the outlet diameter of the lower pipe is equal to the outlet diameter of the upper pipe, or the outlet diameter of the lower pipe is greater than the outlet diameter of the upper pipe.

7. The upward-flowing gas-liquid distributor according to claim 5, wherein, The ratio of the outlet diameter of the lower pipe to the upper pipe is 0.1-10:1; The height ratio of the lower tube to the upper tube is 0.1-10:

1.

8. The upward-flowing gas-liquid distributor according to claim 7, wherein, The ratio of the outlet diameter of the lower pipe to the upper pipe is 0.1-5:1; the ratio of the height of the lower pipe to the upper pipe is 0.2-3:

1.

9. The upward-flowing gas-liquid distributor according to claim 8, wherein, The ratio of the outlet diameter of the lower pipe to the upper pipe is 0.5-2:

1.

10. The upward-flowing gas-liquid distributor according to claim 5, wherein, The inner tube also includes a baffle that connects the lower tube and the liquid inlet; The included angle α between the liquid inlet and the baffle is ≤90°. The side of the baffle is provided with a hole-I, and the opening ratio is 10-80%; The horizontal surface of the liquid inlet is provided with a hole-II, and the opening ratio is 5-30%.

11. The upward-flowing gas-liquid distributor according to claim 10, wherein, The included angle α between the liquid inlet and the baffle is 60-90°.

12. The upward-flowing gas-liquid distributor according to claim 10, wherein, The diameter ratio of the lower pipe to the main pipe is 1:2-25; The diameter of the tube body is 0.2-10mm, and the diameter of the main tube is 20-50mm.

13. The upward-flowing gas-liquid distributor according to claim 12, wherein, The diameter ratio of the lower pipe to the main pipe is 1:2-10; The portion of the tube that extends into the main tube is selected from the upper tube.

14. The upward-flowing gas-liquid distributor according to claim 1, wherein, The number of stages of the gas-liquid dispersion component is 1-5; The ratio of the inner diameter of the narrowing section to the inner diameter of the main pipe is 0.1-0.8:1; the ratio of the inner diameter of the widening section to the inner diameter of the main pipe is 1-3:

1. The height ratio of the gas-liquid dispersion component to the main pipe in each stage is 0.1-0.5:1; In each stage of the gas-liquid dispersion component, the height ratio of the narrowing section to the expanding section is 1:0.2-3.

15. The upward-flowing gas-liquid distributor according to claim 14, wherein, The gas-liquid dispersion component has 1-3 stages; The ratio of the inner diameter of the narrowing section to the inner diameter of the main pipe is 0.2-0.6:1; the ratio of the inner diameter of the widening section to the inner diameter of the main pipe is 1-2:

1. The height ratio of the gas-liquid dispersion component to the main pipe in each stage is 0.2-0.3:1; In each stage of the gas-liquid dispersion component, the height ratio of the narrowing section to the expanding section is 1:0.6-2.

16. The upward-flowing gas-liquid distributor according to claim 1, wherein the porosity of the first orifice is ≥20%; and the specific surface area is ≥200 m². -1 .

17. The upward-flowing gas-liquid distributor according to claim 16, wherein, The first orifice is selected from packing material and / or a porous plate; The porosity of the first pore is 50-99%; the specific surface area is 200-2000 m². -1 .

18. The upward-flowing gas-liquid distributor according to claim 1, wherein, The porosity of the second pore is ≥20%; the specific surface area is ≥200m². -1 ; The second orifice is selected from packing material and / or a porous plate.

19. The upward-flowing gas-liquid distributor according to claim 18, wherein, The porosity of the second pore section is 50-99%; the specific surface area is 200-2000 m². -1 .

20. A method for gas-liquid distribution, characterized in that, The method is used to perform gas-liquid distribution in the upward gas-liquid distributor according to any one of claims 1-19; The liquid phase entering from the liquid phase inlet and the gas phase entering from the inner tube vent and the main tube vent are initially premixed in the tube body from bottom to top, and then premixed again in the main tube. The resulting gas-liquid premix is ​​dispersed in the gas-liquid dispersion component, and the resulting gas-liquid dispersion is radially diffused in the gas-liquid diffusion component.

21. The method according to claim 20, wherein, With m 3 The liquid phase and m 3 The calculated flow rate ratio of the gas phase is 0.1-5:2-30; The feed rate of the liquid phase is 0.2-1 m / s. 3 / h; The space velocity of the gas phase is 2-15 h⁻¹. -1 ; The flow rate ratio of the gas phase through the inner tube vent and the main tube vent is 0.1-2:3-10.

22. The method according to claim 21, wherein, With m 3 The liquid phase and m 3 The calculated flow rate ratio of the gas phase is 0.2-1:3-10; The feed rate of the liquid phase is 0.2-0.5 m / s. 3 / h; The space velocity of the gas phase is 3-5 h⁻¹. -1 ; The flow rate ratio of the gas phase through the inner tube vent and the main tube vent is 0.5-1:3-5.

23. An upward-flowing reactor, characterized in that, The upward reactor includes: at least one distribution plate and an upward gas-liquid distributor as described in any one of claims 1-19; The distribution plate is disposed inside the upward reactor, and the lower surface of the distribution plate is provided with at least one hole-III; The hole-III and the upward gas-liquid distributor are respectively provided, and each hole-III is independently connected to the top outlet of the upward gas-liquid distributor.

24. The upward-flowing reactor according to claim 23, wherein, The number of distribution disks is 1-5; The ratio of the vertical distance between two adjacent distribution discs to the height of the upward-moving gas-liquid distributor is 1-50:1; The height ratio of the distribution plate to the upward-moving gas-liquid distributor is 0.01-0.5:

1.

25. The upward-flowing reactor according to claim 24, wherein, The number of distribution disks is 1-3; The ratio of the vertical distance between two adjacent distribution discs to the height of the upward-moving gas-liquid distributor is 2-20:1; The height ratio of the distribution plate to the upward-moving gas-liquid distributor is 0.05-0.5:

1.

26. The upward-flowing reactor according to claim 23, wherein, The number of holes-III is 1-10; The holes-III are evenly distributed on the lower surface of the distribution plate; The upward reactor further includes a raw material inlet and a raw material outlet, wherein the raw material inlet is located at the bottom of the upward reactor and the raw material outlet is located at the top of the upward reactor.

27. The upward-flowing reactor according to claim 26, wherein, The number of holes-III is 1-5.

28. The application of the upward reactor according to any one of claims 23-27 in a hydrogenation reaction.

29. An upward-flowing hydrogenation reactor, characterized in that, The upward hydrogenation reactor includes the upward reactor as described in any one of claims 23-27.

Images