CN117398927A

CN117398927A - Uplink gas-liquid distributor, gas-liquid distribution method, uplink reactor, application of uplink reactor and uplink hydrogenation reactor

Info

Publication number: CN117398927A
Application number: CN202210849906.5A
Authority: CN
Inventors: 艾涛; 王少兵; 赵梦轩
Original assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Current assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Priority date: 2022-07-07
Filing date: 2022-07-07
Publication date: 2024-01-16

Abstract

The invention relates to the technical field of petrochemical industry, in particular to an uplink gas-liquid distributor, a gas-liquid distribution method, an uplink reactor containing the uplink gas-liquid distributor and application thereof, and an uplink hydrogenation reactor containing the uplink reactor. The upward gas-liquid distributor comprises the following components from bottom to top: the device comprises a gas-liquid premixing component, at least one stage of gas-liquid dispersing component and a gas-liquid dispersing component which are communicated in sequence; the gas-liquid premixing component comprises an inner tube and an outer tube, wherein the inner tube comprises a tube body, and a liquid phase inlet, an inner tube air hole and a liquid phase outlet which are arranged on the tube body, and the outer tube comprises: the main pipe and the main pipe air hole are arranged on the main pipe; the body portion extends into the main tube such that the liquid phase outlet is located inside the main tube. The upward gas-liquid distributor enables gas-liquid to be efficiently mixed, dispersed and transferred; meanwhile, the uplink gas-liquid distributor is used in the uplink reactor, and the reaction efficiency is further improved by improving the gas-liquid mass transfer efficiency.

Description

Uplink gas-liquid distributor, gas-liquid distribution method, uplink reactor, application of uplink reactor and uplink hydrogenation reactor

Technical Field

The invention relates to the technical field of petrochemical industry, in particular to an uplink gas-liquid distributor, a gas-liquid distribution method, an uplink reactor containing the uplink gas-liquid distributor and application thereof, and an uplink hydrogenation reactor containing the uplink reactor.

Background

Compared with the traditional downflow fixed bed reactor, the upflow reactor has the advantages of good adaptability to high-metal inferior raw materials, high space utilization rate of the reactor, lower pressure drop and the like, but has the advantages of uneven micro-expansion of the catalyst bed, easy material bias flow caused catalyst bed temperature fluctuation, radial temperature difference increase and easy hot spot occurrence.

In an upward reactor, both the gas phase and the liquid phase of the reactant stream flow in the reactor in a bottom-up direction, the liquid phase at the reactor outlet section being the continuous phase and the hydrogen being the dispersed phase. Since hydrogen is supplied in the form of dissolved hydrogen, in order to ensure a stable hydrogen partial pressure and hydrogen dissolution rate, the dissolved hydrogen in the liquid phase is always in a saturated state and a small amount of hydrogen exists in the form of a gas. For the gas-liquid two-phase mass transfer process, particularly the liquid phase hydrogenation process with the reaction rate far greater than the mass transfer rate, the mass transfer rate is the key for determining the macroscopic reaction rate, so the control step is realized. The mass transfer rate can be obviously improved by increasing the mass transfer specific surface, but the mass transfer specific surface area is limited to be increased due to the large diameter of the bubble in the prior art, so that the hydrogen dissolution rate and the mass transfer effect are limited.

CN205095759U discloses an uplink gas-liquid distributor, which comprises a flow guiding pipe and a mixed flow piece, wherein the mixed flow piece is arranged above the upper pipe orifice of the flow guiding pipe at intervals, and mixed fluid passing through the flow guiding pipe flows out from the upper pipe orifice of the flow guiding pipe and then reaches the mixed flow piece. However, the device only enhances the mixing between the gas phase and the liquid phase through the mixed flow piece, and technical parameters such as the size and the distribution uniformity of bubbles and the corresponding technical effects are not researched.

CN203737216U discloses an upward gas-liquid distributor for multiphase flow reactor, which consists of rain cap, distribution plate, gas-liquid rising pipe, air inlet pipe, connector and baffle. The distributor has an effect of inhibiting the amount of larger bubbles generated, and can improve the efficiency of gas-liquid phase mass transfer in the reactor, but the distributor has the problems of small operation elasticity and the like.

CN202621143U discloses a notched distributor, which comprises a distributing pipe and a distributing plate, wherein the upper end of the distributing pipe is in fluid communication with the distributing plate, and the lower end of the distributing pipe is provided with an oblique angle opening; the gas-liquid distributor further comprises a baffle, the bevel opening is connected with the baffle, and the baffle covers the bevel opening; the wall of the distribution pipe is provided with a gas channel. Compared with the prior art, the distributor has the advantages of high gas-liquid distribution uniformity, high operation elasticity and the like, but the structure has no function of radial diffusion of gas.

CN211754819U discloses an uplink gas-liquid distributor with filler, comprising a special uplink gas-liquid distributor composed of a lower straight pipe section, a hyperbolic pipe and an upper straight pipe section which are coaxially and fixedly connected, wherein the upper straight pipe section is filled with silk screen corrugated filler; the lower straight pipe section is provided with a through hole, the bottom opening of the lower straight pipe section is an inlet, and the top opening of the upper straight pipe section is an outlet. But the distributor has no function of radial diffusion of the gas; in addition, the distributor cannot be applied to hydrogenation processes of residuum and the like.

Therefore, there is a need for an upward gas-liquid distributor that combines efficient gas-liquid mixing dispersion and mass transfer.

Disclosure of Invention

The invention aims to solve the problems of poor gas-liquid mixing and dispersing effect, larger diameter of generated bubbles, limited radial dispersing effect and the like in the existing uplink gas-liquid distributor, and provides an uplink gas-liquid distributor, a gas-liquid distributing method, an uplink reactor and application thereof, and an uplink hydrogenation reactor, wherein the uplink gas-liquid distributor can realize gas-liquid efficient mixing and generate micro bubbles so as to enhance gas-liquid mass transfer efficiency; meanwhile, the uplink reactor with the uplink gas-liquid distributor is used for hydrogenation reaction, and the reaction efficiency is further improved by improving the gas-liquid mass transfer efficiency.

In order to achieve the above object, a first aspect of the present invention provides an up-going gas-liquid dispenser, which includes, from bottom to top: the device comprises a gas-liquid premixing component, at least one stage of gas-liquid dispersing component and a gas-liquid dispersing component which are communicated in sequence;

wherein, the gas-liquid premixing part includes inner tube and outer tube, the inner tube includes the body and sets up liquid phase entry, inner tube gas pocket and the liquid phase export on the body, the outer tube includes: the main pipe and the main pipe air hole are arranged on the main pipe;

wherein the body portion extends into the main tube such that the liquid phase outlet is located inside the main tube.

Preferably, the inner tube air hole is arranged on the tube wall of the tube body, and is preferably arranged on the tube wall of the tube body upwards along the central axis.

Preferably, the inner tube air holes are at least 1 row, preferably 1-6 rows, and at least 1 row of the inner tube air holes are positioned in the main tube.

Preferably, the main pipe air hole is arranged on the pipe wall of the main pipe, and is preferably arranged on the pipe wall of the main pipe upwards along the central axis.

Preferably, the main pipe air holes are at least 1 row, preferably 1-6 rows, and the height of the main pipe air holes is lower than the height of the liquid phase outlet.

Preferably, the tube body includes: and the inner pipe air holes are respectively arranged on the pipe walls of the lower pipe and the upper pipe.

Preferably, the gas-liquid dispersing part comprises, from bottom to top: the connecting section-I, the reducing section, the connecting section-II and the expanding section are communicated in sequence.

Preferably, in each stage of the gas-liquid dispersing component, the height ratio of the diameter-reducing section to the diameter-expanding section is 1:0.2-3.

Preferably, the gas-liquid diffusion member includes: the connecting section-III and the bubble cap body are communicated in sequence, and a top outlet is arranged on the bubble cap body.

A second aspect of the present invention provides a method of gas-liquid distribution in an uplink gas-liquid distributor provided in the first aspect;

the gas-liquid dispersion device comprises a gas-liquid dispersion component, a main pipe, a gas-liquid premixing body, a gas-liquid dispersion component and a gas-liquid premixing body, wherein the gas-liquid dispersion component is arranged in the gas-liquid dispersion component, the gas-liquid premixing body is arranged in the gas-liquid dispersion component, and the gas-liquid dispersion body is arranged in the gas-liquid dispersion component.

A third aspect of the present invention provides an up-flow reactor comprising: at least one distribution tray, an upstream gas-liquid distributor provided in the first aspect;

wherein the distribution plate is arranged inside the upward reactor, and the lower surface of the distribution plate is provided with at least one hole-III;

wherein the holes-III and the upward gas-liquid distributor are correspondingly arranged, and the holes are respectively and independently connected with the top outlet of the upward gas-liquid distributor.

In a fourth aspect, the present invention provides a use of the upgoing reactor provided in the third aspect in hydrogenation reactions.

In a fifth aspect, the present invention provides an upward hydrogenation reactor, the upward hydrogenation reactor comprising: the third aspect provides an upgoing reactor.

Compared with the prior art, the invention has the following advantages:

(1) The invention provides an uplink gas-liquid distributor, which comprises the following components from bottom to top: the gas-liquid premixing component, the gas-liquid dispersing component and the gas-liquid dispersing component are sequentially communicated, so that gas-liquid efficient mixing, dispersion and mass transfer are realized, namely, gas phase and liquid phase efficient mixing is realized, and the gas phase is efficiently dispersed in the liquid phase in the form of tiny bubbles, so that the gas-liquid mass transfer efficiency is remarkably improved, and the reaction efficiency is promoted;

(2) The method for distributing gas and liquid provided by the invention is carried out in the ascending gas-liquid distributor, in particular, gas-liquid two phases are premixed (namely, pre-mixed and re-premixed) in a sleeve structure (namely, a gas-liquid premixing structure) with inner and outer holes, so that a uniformly distributed gas-liquid premix is formed to flow upwards through a multi-stage gas-liquid dispersing component (particularly, an expanding section containing holes-I), and the size of bubbles is reduced to enhance the gas-phase dispersing effect; then the gas-liquid two phases are further dispersed and radially diffused in a gas-liquid diffusion component (particularly a bubble cap body containing holes-II), and finally overflowed through a top outlet to form uniform bubbling flow;

(3) The uplink gas-liquid distributor provided by the invention is used in an uplink reactor, so that gas-liquid two phases in parallel flow direction of gas and liquid are efficiently mixed, dispersed and transferred, and particularly, the reaction efficiency is promoted by limiting the number of holes-III of a distribution plate and improving the gas-liquid transfer efficiency;

(4) The up-flow reactor provided by the invention can be used for hydrogenation reaction, and is especially suitable for hydrogenation reaction of gasoline and diesel oil, residual oil, wax oil, lubricating oil and the like;

(5) The up-flow reactor provided by the invention is used as an up-flow hydrogenation reactor, and the hydrogenation reaction rate can be effectively improved by promoting efficient mixing, dispersion and mass transfer of gas and liquid.

Drawings

FIG. 1 is a schematic diagram of a first structure of an up-flow gas-liquid distributor according to the present invention;

FIG. 2 is a schematic diagram of a second structure of an up-flow gas-liquid distributor according to the present invention;

FIG. 3 is a schematic view of a third structure of an up-flow gas-liquid distributor according to the present invention;

FIG. 4A is a schematic view of a first and second hole portion structure according to the present invention;

FIG. 4B is a schematic view of another structure of the first hole portion and the second hole portion according to the present invention;

FIG. 5 is a schematic diagram of an upward hydrogenation reactor according to the present invention;

fig. 6 is a gas-liquid distributor of comparative example 1.

Description of the reference numerals

21. Inner tube 22, outer tube 23, and gas-liquid dispersing member

24. Gas-liquid diffusion member

1. Liquid phase inlet 2, baffle 3, lower pipe

4. Inner pipe air hole 5, main pipe 6 and main pipe air hole

7. Upper pipe 8, liquid phase outlet 9, connection section-I

10. Diameter-reducing section 11, connecting section-II 12 and diameter-expanding section

13. First hole portion 14, blister body 15, connecting section-III

16. Top outlet 17, second hole portion

31. Distribution tray 32, holes-III 33, raw material inlet

34. Raw material outlet

41. Gas-liquid inlet 42, riser 43, and air hole

44. Gas-liquid outlet

Detailed Description

The endpoints and any values of the ranges disclosed herein are not limited to the precise range or value, and are understood to encompass values approaching those ranges or values. For numerical ranges, one or more new numerical ranges may be found between the endpoints of each range, between the endpoint of each range and the individual point value, and between the individual point value, in combination with each other, and are to be considered as specifically disclosed herein.

In the present invention, unless specifically stated otherwise, the terms "first" and "second" do not denote a sequential order, nor do they denote a limitation of individual materials or steps, but are used solely to distinguish one from another. For example, "first" and "second" in "first hole portion" and "second hole portion" are used only to indicate that this is not the same hole portion.

The first aspect of the invention provides an uplink gas-liquid distributor, which comprises the following components from bottom to top: the device comprises a gas-liquid premixing component, at least one stage of gas-liquid dispersing component and a gas-liquid dispersing component which are communicated in sequence;

In the present invention, unless otherwise specified, the gas-liquid premixing member, the at least one stage of the gas-liquid dispersing member, and the gas-liquid dispersing member which are sequentially communicated means that an outlet of the gas-liquid premixing member is connected to an inlet of the gas-liquid dispersing member, and an outlet of the gas-liquid dispersing member is connected to an inlet of the gas-liquid dispersing member.

In some embodiments of the present invention, the inner tube air hole is preferably disposed on a wall of the tube body, preferably disposed on a wall of the tube body upward along a central axis. In the invention, the fact that the inner pipe air hole is arranged upwards along the central axis means that the inner pipe air hole is arranged on the pipe wall of the pipe body along the vertical direction, and the inner pipe air hole is preferably arranged on the same vertical line.

In some embodiments of the invention, preferably, the inner tube air holes are at least 1 row, preferably 1-6 rows, and at least 1 row of the inner tube air holes are located inside the main tube. This is provided for generating a bubble group in the main pipe radial direction to increase the bubble group radial range.

In the present invention, unless otherwise specified, a row is used to indicate a unit of measurement of an inner pipe air hole or a main pipe air hole in the vertical direction.

In the invention, the effect of high-efficiency gas-liquid mixing and dispersing is improved. Preferably, the number of the inner pipe air holes in each row is 1-12; further preferably, each row of the inner pipe air holes is uniformly distributed on the pipe wall of the pipe body, and the equivalent diameter of the inner pipe air holes is 1-10mm.

In the invention, the number of the inner pipe air holes in each row refers to the number of the inner pipe air holes arranged on the pipe wall of the pipe body on the same horizontal plane without special condition; the inner pipe air holes are uniformly distributed on the pipe wall of the pipe body, namely on the same horizontal plane, and the included angles of two adjacent inner pipe air holes are the same.

In one specific embodiment of the invention, the inner pipe air holes are upwards arranged on the pipe wall of the pipe body along the central axis, the inner pipe air holes are in 1-6 rows, and at least one row of the inner pipe air holes are positioned in the main pipe; wherein the number of the air holes of the inner pipe in each row is 1-12, and the air holes are uniformly distributed on the pipe wall of the pipe body; wherein the equivalent diameter of the inner tube air hole is 1-10mm.

In some embodiments of the present invention, the main pipe air hole is preferably disposed on the pipe wall of the main pipe, preferably upward along the central axis. The main pipe air hole is arranged upwards along the central axis, namely the main pipe air hole is arranged on the pipe wall of the main pipe along the vertical direction, and the main pipe air hole is preferably arranged on the same vertical line.

In some embodiments of the invention, preferably, the main pipe has at least 1 row, preferably 1-6 rows, of air holes, and the main pipe has a height lower than the height of the liquid phase outlet. This is provided to prevent and disturb the bubble group generation effect in the tube. The height of the main pipe air hole is lower than that of the liquid phase outlet, namely the height of the highest main pipe air hole is lower than that of the liquid phase outlet along the vertical direction.

In the invention, the effect of high-efficiency gas-liquid mixing and dispersing is improved. Preferably, the number of the main pipe air holes in each row is 1-12; further preferably, each row of main pipe air holes are uniformly distributed on the pipe wall of the main pipe, and the equivalent diameter of each main pipe air hole is 1-10mm.

In the invention, the number of the air holes of each row of the main pipe refers to the number of the air holes of the main pipe arranged on the pipe wall of the main pipe on the same horizontal plane without special condition; the main pipe air holes are uniformly distributed on the pipe wall of the main pipe, namely on the same horizontal plane, and the included angles of two adjacent main pipe air holes are the same.

In a specific embodiment of the invention, the main pipe air holes are arranged on the pipe wall of the main pipe upwards along the central axis, the main pipe air holes are arranged in 1-6 rows, and the height of the main pipe air holes is lower than the height of the liquid phase outlet; wherein the number of the air holes of each row of the main pipe is 1-12, and the air holes are uniformly distributed on the pipe wall of the main pipe; wherein the equivalent diameter of the main pipe air hole is 1-10mm.

In some embodiments of the invention, preferably, the tube body comprises: and the inner pipe air holes are respectively arranged on the pipe walls of the lower pipe and the upper pipe. In the present invention, the number of rows of the inner tube air holes provided on the tube walls of the lower tube and the upper tube is not limited as long as the inner tube air holes are provided on the tube walls of the lower tube and the upper tube.

In some embodiments of the present invention, preferably, the outlet diameter of the lower tube is smaller than the outlet diameter of the upper tube, or the outlet diameter of the lower tube=the outlet diameter of the upper tube, or the outlet diameter of the lower tube is larger than the outlet diameter of the upper tube.

In the present invention, the outlet diameter of the lower tube means the diameter of the upper surface of the lower tube, unless otherwise specified; the outlet diameter of the upper tube refers to the diameter of the upper surface of the upper tube.

In some embodiments of the invention, the outlet diameter ratio of the lower and upper tubes is preferably in the range of 0.1-10:1, e.g., 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 in the range of any two values, preferably 0.1-5:1, more preferably 0.5-2:1. The main aim is to facilitate the manufacture by adopting the existing standard pipe fittings, and reduce the cost.

In some embodiments of the invention, the height ratio of the lower tube to the upper tube is preferably in the range of 0.1-10:1, e.g., 0.1:1, 0.2:1, 0.5:1, 1:1, 2:1, 3:1, 5:1, 8:1, 10:1, and any value in the range of any two values, preferably 0.2-3:1.

In the present invention, a wide selection range is provided for the types of the upper pipe and the lower pipe. Preferably, the upper tube and the lower tube are each independently of a regular shape or an irregular shape, preferably a regular shape, more preferably at least one selected from the group consisting of a cylinder, a truncated cone, a rectangular parallelepiped, and a square, most preferably a cylinder.

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

In the present invention, unless otherwise specified, cross section refers to a section along the central axis of the member.

In some embodiments of the present invention, preferably, the liquid phase inlet is disposed at a bottom of the pipe body, and the liquid phase outlet is disposed at a top of the pipe body; further preferably, the liquid phase inlet is provided at the bottom of the lower pipe; the liquid phase outlet is arranged at the top of the upper pipe.

In some embodiments of the present invention, preferably, the inner tube further comprises: a baffle connecting the lower tube and the liquid phase inlet; further preferably, the angle α between the liquid phase inlet and the side of the baffle is less than or equal to 90 °, preferably 60-90 °.

In some embodiments of the invention, preferably, the side of the baffle is provided with holes-I and the aperture ratio is 10-80%; further preferably, the holes-I are selected from elongated holes and/or round holes.

In some embodiments of the invention, preferably, the level of the liquid phase inlet is provided with holes-II and the aperture ratio is 5-30%; further preferably, the hole-II is selected from at least one of a triangular hole, a quadrangular hole, and a circular hole, and more preferably from at least one of a regular triangular hole, a square hole, and a concentric circular hole.

In some embodiments of the present invention, preferably, the main pipe is of a regular shape or an irregular shape, preferably a regular shape, more preferably at least one selected from a cylinder, a truncated cone, a cuboid, and a cube, and most preferably a cylinder.

In some embodiments of the present invention, the cross section of the main pipe is preferably regular or irregular, preferably regular, more preferably at least one selected from rectangular, square and trapezoid, most preferably rectangular.

In some embodiments of the invention, preferably, the diameter ratio of the lower tube to the main tube is 1:2-25, e.g., 1:2, 1:5, 1: 8. any value in the range of 1:10, 1:15, 1:20, 1:25, and any two values, preferably 1:2-10.

In one embodiment of the present invention, preferably, the diameter of the pipe body is 0.2-10mm, and the diameter of the main pipe is 20-50mm. Wherein the diameter range of the pipe body includes a diameter range of the lower pipe and a diameter range of the upper pipe.

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

In some embodiments of the invention, the ratio of the diameter of the liquid phase outlet to the inlet diameter of the upper tube is preferably in the range of 1:0.1-5, e.g., 1:0.1, 1:0.5, 1:1, 1:2, 1:3, 1:4, 1:5, and any value in 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 tube is equal to the ratio of the outlet diameters of the upper tube and the lower tube.

In some embodiments of the invention, the ratio of the height of the pipe body extending into the main pipe to the height of the main pipe is preferably any value in the range of 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 two values, preferably 0.1-0.5:1.

In some embodiments of the invention, preferably the portion of the tubular body extending into the main tube is selected from at least part of the upper tube and optionally part of the lower tube, preferably from the upper tube. That is, the portion extending into the main pipe may be a portion of the upper pipe, and a portion of the lower pipe, or may be the upper pipe.

In the invention, the multistage gas-liquid dispersing component is adopted to strengthen the dispersing effect of the gas-liquid two phases. Preferably, the gas-liquid dispersing section has a number of stages of 1 to 5, for example, 1 stage, 2 stage, 3 stage, 4 stage, 5 stage, preferably 1 to 3 stage.

In some embodiments of the present invention, preferably, the gas-liquid dispersing part includes, from bottom to top: the connecting section-I, the reducing section, the connecting section-II and the expanding section are communicated in sequence.

In some embodiments of the invention, preferably, the ratio of the inside diameter of the reduced diameter section to the main tube is in the range of 0.1-0.8:1, e.g., 0.1:1, 0.2:1, 0.4:1, 0.6:1, 0.8:1, and any value in the range of any two values, preferably 0.2-0.6:1; the ratio of the inner diameters of the expanded section and the main pipe is 1-3:1, for example, 1:1, 1.5:1, 2:1, 3:1, and any value in the range of any two values, preferably 1-2:1.

In some embodiments of the invention, preferably, the height ratio of the gas-liquid dispersion member to the main pipe of each stage is in the range of 0.1-0.5:1, for example, 0.1:1, 0.2:1, 0.3:1, 0.5:1, and any value in the range of any two values, preferably 0.2-0.3:1. The height of each stage of the gas-liquid dispersing component is the sum of the heights of the connecting section-I, the reducing section, the connecting section-II and the expanding section.

In some embodiments of the invention, preferably, the height ratio of the reduced diameter section and the expanded diameter section in each stage of the gas-liquid dispersion member is any value in the range of 1:0.2 to 3, for example, 1:0.2, 1:05, 1:0.6, 1:1, 1:1.5, 1:2, 1:3, and any two values, preferably 1:0.6 to 2.

In some embodiments of the present invention, it is further preferred that the height ratio of the connecting section-I, the reducing section, the expanding section and the connecting section-II in each stage of the gas-liquid dispersing section is 0.1-0.5:1:0.2-3:0.1-0.5, preferably 0.2-0.3:1:0.6-2:0.2-0.3. The preferred height ratio is used to more effectively increase the ability of each component to generate a bubble group and to ensure a smaller dispenser height.

In the present invention, the dispersion effect of the gas-liquid two phases is further improved. Preferably, a first hole part is arranged in the diameter expansion section; further preferably, the first well is selected from a packing and/or a porous plate.

In some embodiments of the invention, preferably, the porosity of the first pore portions is each independently ≡20%, preferably 50-99%; specific surface area is more than or equal to 200m ^-1 Preferably 200-2000m ^-1 。

In one embodiment of the invention, preferably, the filler is selected from wire mesh filler and/or corrugated filler; preferably, the porous plate is selected from a punching plate and the like.

In a specific embodiment of the present invention, a schematic structural diagram of the first hole portion is shown in fig. 4A, and as can be seen from fig. 4A, the first hole portion is a wire mesh filler, and the material is selected from carbon steel and stainless steel, and has a porosity of 50-99%.

In another embodiment of the present invention, a schematic structural diagram of the first hole portion is shown in fig. 4B, and as can be seen from fig. 4B, the first hole portion is a porous plate, and the material is selected from carbon steel and stainless steel, and has a porosity of 50-99%.

In some embodiments of the present invention, preferably, the gas-liquid diffusion member includes: the connecting section-III and the bubble cap body are communicated in sequence, and a top outlet is arranged on the bubble cap body.

In some embodiments of the invention, preferably, the blister is made up of a mesh and/or screen; further preferably, the interior of the blister body is provided with a second aperture portion selected from the group consisting of a filler and/or a porous plate.

In the present invention, the filler and the porous plate of the second hole portion are defined as described above, and the present invention will not be described in detail.

Some embodiments of the inventionPreferably, the porosity of the second pore portions is each independently equal to or more than 20%, preferably 50 to 99%; specific surface area is more than or equal to 200m ^-1 Preferably 200-2000m ^-1 。

In a specific embodiment of the present invention, a schematic structural diagram of the second hole portion is shown in fig. 4A, and as can be seen from fig. 4A, the second hole portion is a wire mesh filler, and the material is selected from carbon steel and stainless steel, and has a porosity of 50-99%.

In another embodiment of the present invention, the second hole portion is schematically shown in fig. 4B, and as can be seen from fig. 4B, the second hole portion is a porous plate, and the material is selected from carbon steel and stainless steel, and the porosity is 50-99%.

In some embodiments of the present invention, preferably, the blister is regular and/or irregular, preferably regular, and more preferably at least one selected from the group consisting of a cylinder, a hemisphere, a cuboid, and a cube.

In some embodiments of the present invention, the cross section of the blister body is preferably regular or irregular, preferably regular, more preferably at least one selected from rectangular, square, trapezoidal and semicircular.

In the invention, the liquid phase inlet, the lower pipe, the upper pipe, the main pipe, the liquid phase outlet, the diameter reducing section, the diameter expanding section and the top outlet are respectively and independently connected through movable components; wherein the movable part includes, but is not limited to, threads.

The schematic structural diagram of the first uplink gas-liquid distributor provided by the invention is shown in fig. 1, and as can be seen from fig. 1, the uplink gas-liquid distributor comprises from bottom to top: the gas-liquid premixing component, the primary gas-liquid dispersing component 23 and the gas-liquid dispersing component 24 are communicated in sequence; the gas-liquid premixing part comprises an inner tube 21 and an outer tube 22, wherein the inner tube 21 comprises: a lower pipe 3 and an upper pipe 7 which are communicated, an inner pipe air hole 4 arranged on the pipe walls of the lower pipe 3 and the upper pipe 7, a liquid phase inlet 1 arranged at the bottom of the lower pipe 3, a liquid phase outlet 8 arranged at the top of the upper pipe 7, and a baffle plate 2 connecting the lower pipe 3 and the liquid phase inlet 1; the outer tube 22 includes: a main pipe 5 and a main pipe air hole 6 arranged on the pipe wall of the main pipe 5;

Wherein the upper pipe 7 extends into the interior of the main pipe 5 such that the liquid phase outlet 8 is located inside the main pipe 5; wherein the outlet diameter of the lower tube 3 > the outlet diameter of the upper tube 7; the cross section of the lower pipe 3 is rectangular, and the cross section of the upper pipe 7 is trapezoidal; wherein the included angle alpha=90° between the liquid phase inlet 1 and the baffle 2;

wherein at least 1 row of inner tube air holes 4 are positioned in the main tube 5; the height of the main pipe air hole 6 is lower than that of the liquid phase inlet 8;

wherein the gas-liquid dispersing part 23 comprises, from bottom to top: the connecting section-I9, the reducing section 10, the connecting section-II 11 and the expanding section 12 are communicated in sequence; wherein, the inside of the expanding section 12 is provided with a first hole part 13;

wherein the gas-liquid diffusion member 24 includes: a connecting section-III 15 and a bubble cap body 14 which are communicated in sequence, and a top outlet 16 arranged on the bubble cap body 14; the second hole 17 is provided in the blister body 14; the blister body 14 is rectangular in cross-section.

The schematic structural diagram of the second uplink gas-liquid distributor provided by the invention is shown in fig. 2, and as can be seen from fig. 2, the uplink gas-liquid distributor comprises from bottom to top: a gas-liquid premixing part, a secondary gas-liquid dispersing part 23 and a gas-liquid dispersing part 24 which are communicated in sequence; the gas-liquid premixing part comprises an inner tube 21 and an outer tube 22, wherein the inner tube 21 comprises: a lower pipe 3 and an upper pipe 7 which are communicated, an inner pipe air hole 4 arranged on the pipe walls of the lower pipe 3 and the upper pipe 7, a liquid phase inlet 1 arranged at the bottom of the lower pipe 3, a liquid phase outlet 8 arranged on the upper pipe 7, and a baffle plate 2 connecting the lower pipe 3 and the liquid phase inlet 1; the outer tube 22 includes: a main pipe 5 and a main pipe air hole 6 arranged on the pipe wall of the main pipe 5;

Wherein the upper pipe 7 extends into the interior of the main pipe 5 such that the liquid phase outlet 8 is located inside the main pipe 5; wherein the outlet diameter of the lower tube 3 < the outlet diameter of the upper tube 7; the cross section of the lower pipe 3 is rectangular, and the cross section of the upper pipe 7 is inverted trapezoid; wherein the included angle alpha between the liquid phase inlet 1 and the side part of the baffle plate 2 is smaller than 90 degrees;

wherein each stage of the gas-liquid dispersing part 23 comprises, from bottom to top: the connecting section-I9, the reducing section 10, the connecting section-II 11 and the expanding section 12 are communicated in sequence; wherein, the inside of the expanding section 12 is provided with a first hole part 13;

wherein the gas-liquid diffusion member 24 includes: a connecting section-III 15 and a bubble cap body 14 which are communicated in sequence, and a top outlet 16 arranged on the bubble cap body 14; the second hole 17 is provided in the blister body 14; the blister 14 is semi-circular in cross-section.

The structural schematic diagram of the third uplink gas-liquid distributor provided by the invention is shown in fig. 3, and as can be seen from fig. 3, the uplink gas-liquid distributor comprises from bottom to top: a gas-liquid premixing part, a three-stage gas-liquid dispersing part 23 and a gas-liquid dispersing part 24 which are communicated in sequence; the gas-liquid premixing part comprises an inner tube 21 and an outer tube 22, wherein the inner tube 21 comprises: a lower pipe 3 and an upper pipe 7 which are communicated, an inner pipe air hole 4 arranged on the pipe walls of the lower pipe 3 and the upper pipe 7, a liquid phase inlet 1 arranged at the bottom of the lower pipe 3, a liquid phase outlet 8 arranged on the upper pipe 7, and a baffle plate 2 connecting the lower pipe 3 and the liquid phase inlet 1; the outer tube 22 includes: a main pipe 5 and a main pipe air hole 6 arranged on the main pipe 5;

Wherein the upper pipe 7 extends into the main pipe 5 such that the liquid phase outlet 8 is located inside the main pipe 5; wherein the outlet diameter of the lower tube 3 = the outlet diameter of the upper tube 7; the cross sections of the lower pipe 3 and the upper pipe 7 are rectangular; wherein the included angle alpha between the liquid phase inlet 1 and the side part of the baffle plate 2 is smaller than 90 degrees;

wherein the gas-liquid diffusion member 24 includes: a connecting section-III 15 and a bubble cap body 14 which are communicated in sequence, and a top outlet 16 arranged on the bubble cap body 14; the second hole 17 is provided in the blister body 14; the blister body 14 has an inverted trapezoidal cross section.

In some embodiments of the invention, preferably, m ³ The sum of the liquid phases is calculated as m ³ The flow ratio of the gas phase is 0.1-5:2-30, preferably 0.2-1:3-10. Namely, 0.1 to 5m relative to the flow rate ³ The flow rate of the gas phase is 2-30m ³ 。

In some embodiments of the invention, it is preferred that the liquid phase is fed at a rate of 0.2 to 1m ³ For example, 0.2, 0.3, 0.4, 0.5, 0.8, 1, and any value in the range of any two values, preferably 0.2 to 0.5m ³ /h。

In some embodiments of the invention, preferably, the gas phase has a space velocity of from 2 to 15 hours ^-1 For example, any value in the range of 2, 3, 4, 5, 8, 10, 12, 15, and any two values, preferably 3-5h ^-1 。

In some embodiments of the invention, the flow ratio of the gas phase through the inner tube gas holes and the main tube gas holes is preferably 0.1-2:3-10, preferably 0.5-1:3-5. By regulating the flow ratio of the inner pipe air hole to the main pipe air hole, the gas-liquid phase mixing can be effectively promoted, and the generation of bubble groups is facilitated.

the hole-III and the upward gas-liquid distributor are correspondingly arranged, and the hole-III is respectively and independently connected with the top outlet of the upward gas-liquid distributor.

In some embodiments of the present invention, the number of the distribution trays is preferably 1 to 5, preferably 1 to 3.

In some embodiments of the present invention, preferably, the vertical distance between two adjacent distribution trays and the height of the ascending gas-liquid distributor are in the range of 1-50:1, for example, 1:1, 2:1, 5:1, 10:1, 15:1, 20:1, and any value in the range of any two values, preferably 2-20:1.

In some embodiments provided herein, the height ratio of the distributor tray to the upstream gas-liquid distributor is preferably any value in the range of 0.01-0.5:1, e.g., 0.01:1, 0.05:1, 0.1:1, 0.2:1, 0.3:1, 0.5:1, and any two values, preferably 0.05-0.5:1. Wherein the height of the distribution plate refers to the vertical distance between the upper surface and the lower surface of the distribution plate; the height of the upward gas-liquid distributor refers to the sum of the height of the gas-liquid premixing component, the height of the at least one stage of gas-liquid dispersing component and the height of the gas-liquid dispersing component.

In some embodiments of the invention, the number of holes-III is preferably 1-10, preferably 1-5.

In some embodiments of the invention, preferably, the holes-III are uniformly distributed on the lower surface of the distribution plate.

In some embodiments of the present invention, preferably, the up-flow reactor further comprises: a raw material inlet and a raw material outlet, wherein the raw material inlet is arranged at the bottom of the upward reactor, and the raw material outlet is arranged at the top of the upward reactor.

The structural schematic diagram of an uplink reactor provided by the invention is shown in fig. 5, and the uplink reactor comprises: 2 distribution trays 31, the distribution trays 31 being disposed inside the up-flow reactor, and the lower surface of each distribution tray 31 being uniformly provided with 3 holes-III 32;

wherein the hole-III 32 and the upward gas-liquid distributor are correspondingly arranged, and the holes-III 32 are respectively and independently connected with the top outlet of the upward gas-liquid distributor;

wherein the reactor further comprises a raw material inlet 33 arranged at the bottom of the upward reactor and a raw material outlet 34 arranged at the top of the upward reactor.

The upward gas-liquid distributor provided by the invention can be used in an upward reactor, can be used for gas-liquid two-phase dispersion in a gas-liquid parallel flow upward reactor, and is especially used for hydrogenation reaction of gasoline and diesel oil, residual oil, wax oil and lubricating oil.

In a fifth aspect, the present invention provides an upward hydrogenation reactor, the upward hydrogenation reactor comprising: the fourth aspect provides an upgoing reactor.

In some embodiments of the present invention, it is preferred to use the upgoing reactor provided in the fourth aspect as an upgoing hydrogenation reactor.

According to a particularly preferred embodiment of the present invention, an up-going gas-liquid distributor comprises, from bottom to top: the device comprises a gas-liquid premixing component, at least one stage of gas-liquid dispersing component and a gas-liquid dispersing component which are communicated in sequence;

wherein the pipe body part extends into the main pipe so that the liquid phase outlet is positioned inside the main pipe;

Wherein, the body includes: the inner pipe air holes are respectively arranged on the pipe walls of the lower pipe and the upper pipe along the central axis upwards; the inner tube air holes are 1-6 rows, and at least 1 row of inner tube air holes are positioned in the main tube;

wherein the main pipe air hole is upwards arranged on the pipe wall of the pipe body along the central axis; the main pipe air holes are arranged in 1-6 rows, and the height of the main pipe air holes is lower than that of the liquid phase outlet;

wherein, the gas-liquid dispersion part includes from bottom to top: the connecting section-I, the reducing section, the connecting section-II and the expanding section are communicated in sequence; a first hole part is arranged in the diameter expansion section;

wherein the gas-liquid diffusion member includes: the connecting section-III and the bubble cap body are sequentially communicated, and a top outlet is arranged on the bubble cap body; a second hole part is arranged in the bubble cap body;

wherein the porosity of the first and second pore portions is each independently 50-99%; the specific surface areas are each independently 200-2000m ^-1 。

The present invention will be described in detail by examples.

And (3) measuring a gas content parameter: measuring the initial liquid level and the liquid level after bubbling by using a volume expansion method, and calculating the gas content E in the liquid phase _a The calculation formula is as follows:

wherein in formula I, H _i Is the initial liquid level; h _n The liquid level after bubbling;

bubble diameter parameter measurement process: the bubble diameter of the liquid in the cross section is measured, and the average bubble diameter is used for representing the mixing effect between the gas phase and the liquid phase. In the measurement process, assuming that the bubbles are spherical, the equivalent diameter d of the bubbles can be expressed by the Sauter chord length of the bubbles ₃₂ The formula is as follows:

wherein in formula II, n _i Is of diameter d _i The number of bubbles; n is the total number of bubbles counted.

The gas content parameters and the bubble diameter parameters of examples 1-3 and comparative example 1 are shown in Table 1.

Example 1

The structural schematic diagram of the uplink gas-liquid distributor is shown in fig. 1, and as can be seen from fig. 1, the uplink gas-liquid distributor comprises from bottom to top: the gas-liquid premixing component, the primary gas-liquid dispersing component 23 and the gas-liquid dispersing component 24 are communicated in sequence; the gas-liquid premixing part includes an inner tube 21 and an outer tube 22, the inner tube 21 including: liquid phase inlet 1, baffle 2, lower tube 3, inner tube air vent 4, upper tube 7 and liquid phase outlet 8, outer tube 22 includes: a main pipe 5 and a main pipe air hole 6; wherein the upper pipe 7 extends into the interior of the main pipe 5; the gas-liquid dispersing part 23 includes, from bottom to top: the connecting section-I9, the reducing section 10, the connecting section-II 11 and the expanding section 12 are sequentially communicated, and a first hole part 13 is formed in the expanding section 12; the gas-liquid diffusion member 24 includes: a connecting section-III 15 and a bubble cap body 14 which are communicated in sequence, and a top outlet 16 arranged on the bubble cap body 14; the second hole 17 is provided in the blister body 14; the blister body 14 is rectangular in cross-section.

Wherein the lower pipe 3 is a cylinder, the diameter of the outlet is 5mm, the upper pipe 7 is a round table, and the diameter of the liquid phase outlet 8 is 0.5mm; the height ratio of the lower tube 3 to the upper tube 7 is 1:1;

wherein, the lower tube 3 and the upper tube 7 are respectively provided with 2 rows of inner tube air holes 4, each row of 6 air holes are uniformly distributed on the tube wall of the tube body, and the diameter of the inner tube air holes 4 is 2mm;

wherein the upper pipe 7 extends into the main pipe 5, and the height ratio of the upper pipe 7 to the main pipe 5 is 0.4:1;

the main pipe 5 is a cylinder, the diameter of the main pipe is 20mm, the number of the main pipe air holes 6 is 3, each row of the main pipe air holes is 12, the main pipe air holes are uniformly distributed on the pipe wall of the main pipe, and the diameter of the main pipe air holes 6 is 2mm;

wherein, the included angle alpha=90° between the liquid phase inlet 1 and the side part of the baffle plate 2, the side part of the baffle plate 2 is provided with a hole-I (round hole), and the aperture ratio is 30%; the level of the liquid phase inlet 1 is provided with a hole-II (regular triangle hole), and the aperture ratio is 10%;

wherein the diameter of the diameter-reducing section 10 is 10mm, and the height is 25mm; the diameter of the expanding section 12 is 30mm, and the height is 20mm; the first hole part 13 is silk screen filler, the porosity is 80%, and the specific surface area is 300m ^-1 ；

Wherein the second hole 17 is a silk screen filler, the porosity is 85%, and the specific surface area is 300m ^-1 。

The gas-liquid distribution method comprises the following steps:

the method is carried out in the uplink gas-liquid distributor, and comprises the following steps: after the liquid phase entering from the liquid phase inlet 1 and the gas phase entering from the inner pipe gas holes 4 and the main pipe gas holes 6 are pre-mixed in the lower pipe 3 and the upper pipe 7 from bottom to top, the main pipe 5 is pre-mixed again, the obtained gas-liquid pre-mixture is dispersed in gas-liquid dispersing component 23, and the obtained gas-liquid dispersion is radially dispersed in gas-liquid dispersing component 24;

Wherein the ratio of the liquid phase to the gas phase is 1:5, and the feeding speed of the liquid phase is 0.4m ³ Per hour, the space velocity of the gas phase is 5 hours ^-1 The method comprises the steps of carrying out a first treatment on the surface of the The flow ratio of the gas phase to the main pipe gas hole is 1:3.

Example 2

As shown in fig. 2, the structure of the uplink gas-liquid distributor is schematically shown in fig. 2, and the uplink gas-liquid distributor includes from bottom to top: a gas-liquid premixing part, a secondary gas-liquid dispersing part 23 and a gas-liquid dispersing part 24 which are communicated in sequence; the gas-liquid premixing part includes an inner tube 21 and an outer tube 22, the inner tube 21 including: liquid phase inlet 1, baffle 2, lower tube 3, inner tube air vent 4, upper tube 7 and liquid phase outlet 8, outer tube 22 includes: a main pipe 5 and a main pipe air hole 6; wherein the upper pipe 7 extends into the interior of the main pipe 5; the gas-liquid dispersing part 23 includes, from bottom to top: the connecting section-I9, the reducing section 10, the connecting section-II 11 and the expanding section 12 are sequentially communicated, and a first hole part 13 is formed in the expanding section 12; the gas-liquid diffusion member 24 includes: a connecting section-III 15 and a bubble cap body 14 which are communicated in sequence, and a top outlet 16 arranged on the bubble cap body 14; the second hole 17 is provided in the blister body 14; the blister 14 is semi-circular in cross-section.

Wherein the lower pipe 3 is a cylinder, the diameter of the outlet is 5mm, the upper pipe 7 is a round table, and the diameter of the liquid phase outlet 8 is 15mm; the height ratio of the lower tube 3 to the upper tube 7 is 2:1;

Wherein, the lower tube 3 and the upper tube 7 are respectively provided with 2 rows of inner tube air holes 4, each row of 6 air holes are uniformly distributed on the wall of the inner tube, and the diameter of the inner tube air holes 4 is 5mm;

wherein the upper pipe 7 extends into the main pipe 5, and the height ratio of the upper pipe 7 to the main pipe 5 is 0.5:1;

wherein, the included angle alpha between the liquid phase inlet 1 and the side part of the baffle plate 2 is smaller than 90 degrees, the side part of the baffle plate 2 is provided with a hole-I (round hole), and the aperture ratio is 50%; the level of the liquid phase inlet 1 is provided with a hole-II (regular triangle hole), and the aperture ratio is 15%;

wherein, the diameters of the two reducing sections 10 are 10mm, and the heights are 20mm; the diameters of the two expanding sections 12 are 30mm, and the heights are 20mm; the first hole part 13 is silk screen filler, the porosity is 90%, the specific surface area is 1000m ^-1 ；

Wherein the second hole 17 is a silk screen filler, the porosity is 95%, and the specific surface area is 1500m ^-1 。

The gas-liquid distribution method comprises the following steps:

the method is carried out in the uplink gas-liquid distributor, and comprises the following steps: after the liquid phase entering from the liquid phase inlet 1 is primarily premixed with the gas phase entering from the inner pipe gas holes 4 and the main pipe gas holes 6 from bottom to top in the lower pipe 3 and the upper pipe 7, the premixing is performed again in the main pipe 5, the obtained gas-liquid premix is subjected to gas-liquid dispersion in the gas-liquid dispersion member 23, and the obtained gas-liquid dispersion is subjected to radial dispersion in the gas-liquid dispersion member 24;

Wherein the flow ratio of the liquid phase to the gas phase is 1:5, and the feeding speed of the liquid phase is 0.4m ³ Per hour, the space velocity of the gas phase is 5 hours ^-1 The method comprises the steps of carrying out a first treatment on the surface of the The flow ratio of the gas phase to the main pipe gas hole is 1:3.

Example 3

As shown in fig. 3, the structure of the up-going gas-liquid distributor is shown in fig. 3, and the up-going gas-liquid distributor includes from bottom to top: a gas-liquid premixing part, a three-stage gas-liquid dispersing part 23 and a gas-liquid dispersing part 24 which are communicated in sequence; the gas-liquid premixing part includes an inner tube 21 and an outer tube 22, the inner tube 21 including: liquid phase inlet 1, baffle 2, lower tube 3, inner tube air vent 4, upper tube 7 and liquid phase outlet 8, outer tube 22 includes: a main pipe 5 and a main pipe air hole 6; wherein the upper pipe 7 extends into the interior of the main pipe 5; the gas-liquid dispersing part 23 includes, from bottom to top: the connecting section-I9, the reducing section 10, the connecting section-II 11 and the expanding section 12 are sequentially communicated, and a first hole part 13 is formed in the expanding section 12; the gas-liquid diffusion member 24 includes: a connecting section-III 15 and a bubble cap body 14 which are communicated in sequence, and a top outlet 16 arranged on the bubble cap body 14; the second hole 17 is provided in the blister body 14; the blister body 14 has an inverted trapezoidal cross section.

Wherein, the lower tube 3 and the upper tube 7 are both cylinders, and the diameters are 5mm; the height ratio of the lower tube 3 to the upper tube 7 is 0.5:1;

Wherein, the lower tube 3 and the upper tube 7 are respectively provided with 2 rows of inner tube air holes 4, each row of 6 air holes are uniformly distributed on the wall of the inner tube, and the diameter of the inner tube air holes 4 is 2mm;

the main pipe 5 is a cylinder, the diameter of the main pipe is 50mm, the number of the main pipe air holes 6 is 3, each row of the main pipe air holes is 12, the main pipe air holes are uniformly distributed on the pipe wall of the main pipe, and the diameter of the main pipe air holes 6 is 2mm;

wherein, the included angle alpha between the liquid phase inlet 1 and the side part of the baffle plate 2 is smaller than 90 degrees, the side part of the baffle plate 2 is provided with a hole-I (round hole), and the aperture ratio is 80%; the level of the liquid phase inlet 1 is provided with a hole-II (regular triangle hole), and the aperture ratio is 30%;

wherein, the diameters of the three reducing sections 10 are 10mm, and the heights are 20mm; the diameters of the two expanding sections 12 are 50mm, and the heights are 10mm; the first hole part 13 is silk screen filler, the porosity is 98%, the specific surface area is 2000m ^-1 ；

Wherein the second hole 17 is a silk screen filler, the porosity is 98%, and the specific surface area is 2000m ^-1 。

The gas-liquid distribution method comprises the following steps:

Comparative example 1

A schematic structural diagram of the gas-liquid distributor is shown in fig. 6, and as can be seen from fig. 6, the gas-liquid distributor includes: a gas-liquid inlet 41, a riser 42, 2 air holes 43, and a gas-liquid outlet 44;

wherein, the inner diameter of the ascending pipe is 50mm, and the length is 100mm;

wherein, the air hole 43 is positioned in the middle of the rising pipe, and the diameter of the air hole 43 is 5mm;

wherein, the top structure of tedge is porous plate structure, and hole quantity is 20, and the diameter is 3mm.

The gas-liquid distribution method comprises the following steps:

in the gas-liquid distributor, the liquid phase directly enters the ascending pipe from the gas-liquid inlet 41, the gas phase partially enters from the gas-liquid inlet 41 and partially enters from the air holes 43, the gas phase and the air holes are mixed and then move upwards, and bubbles formed at the opening in the middle part directly overflow from the top to enter the ascending reactor;

wherein the flow ratio of the liquid phase to the gas phase is 1:5, and the feeding speed of the liquid phase is 0.4m ³ Per hour, the space velocity of the gas phase is 5 hours ^-1 The method comprises the steps of carrying out a first treatment on the surface of the The flow ratio of the gas phase through the gas-liquid inlet and the air hole is 1:3.

TABLE 1

	Gas content E _a ，％	Average diameter d, mm of bubbles
			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

As can be seen from the data in Table 1, compared with comparative example 1, the gas-liquid distributor provided by the invention has higher gas content and better distribution performance in examples 1-3; that is, the gas content E _a The larger the parameter, the better the gas-liquid distribution performance. Compared with the comparative example 1, the gas-liquid distributor provided by the invention can provide larger mass transfer driving force, thereby improving faster mass transfer speed; particularly, the more the number of stages of the gas-liquid dispersing component is, the more the mass transfer speed is improved.

As can be seen from the data in Table 1, the average diameter of the bubbles in the gas-liquid distributor in comparative example 1 is 7.43mm, and the diameters of the bubbles in the gas-liquid distributors in examples 1 to 3 are 1 to 2mm, i.e., the gas-liquid distributor provided by the invention has smaller bubble diameter d and better dispersion performance. The gas-liquid distributor provided by the invention has slightly better mixing effect than the gas-liquid distributor of comparative example 1, and especially the more the number of stages of gas-liquid dispersing components (i.e. the more the number of diameter-reducing sections and diameter-expanding sections), the more effectively the dispersing effect between the gas-liquid two phases is enhanced, so that the generated bubble diameter is smaller.

In the gas-liquid two-phase parallel flow upward flow and reaction process, generally, the smaller the bubble diameter d is, the more favorable the gas-liquid mass transfer surface area is increased and the bubble residence time is prolonged, and both the gas-liquid mass transfer surface area and the bubble residence time are favorable for the mass transfer effect enhancement. For hydrogenation reaction, the contact time between hydrogen oil materials is increased, and the effects of further improving the mass transfer and reaction speed between gas phase and liquid phase are achieved. Therefore, in either aspect, minimizing the bubble size is advantageous for an upward or full liquid phase hydrogenation reaction process.

The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, a number of simple variants of the technical solution of the invention are possible, including combinations of the individual technical features in any other suitable way, which simple variants and combinations should likewise be regarded as being disclosed by the invention, all falling within the scope of protection of the invention.

Claims

1. An upward gas-liquid distributor, which is characterized by comprising from bottom to top: the device comprises a gas-liquid premixing component, at least one stage of gas-liquid dispersing component and a gas-liquid dispersing component which are communicated in sequence;

2. The upward gas-liquid distributor according to claim 1, wherein the inner tube air holes are provided in the tube wall of the tube body, preferably in the tube wall of the tube body upwards along a central axis;

Preferably, the inner tube air holes are at least 1 row, preferably 1-6 rows, and at least 1 row of the inner tube air holes are positioned in the main tube;

preferably, the number of the air holes of the inner tube in each row is 1-12, and the air holes are preferably uniformly distributed on the wall of the tube body;

preferably, the main pipe air hole is arranged on the pipe wall of the main pipe, and is preferably arranged on the pipe wall of the main pipe upwards along the central axis;

preferably, the main pipe air holes are at least 1 row, preferably 1-6 rows, and the height of the main pipe air holes is lower than the height of the liquid phase outlet;

preferably, the number of the air holes of the main pipe in each row is 1-12, and the air holes are preferably uniformly distributed on the pipe wall of the main pipe.

3. The ascending gas-liquid dispenser according to claim 1 or 2, wherein the tube comprises: the lower pipe and the upper pipe are communicated, wherein the inner pipe air holes are respectively arranged on the pipe walls of the lower pipe and the upper pipe;

preferably, the outlet diameter of the lower tube < the outlet diameter of the upper tube, or the outlet diameter of the lower tube = the outlet diameter of the upper tube, or the outlet diameter of the lower tube > the outlet diameter of the upper tube;

preferably, the outlet diameter ratio of the lower tube to the upper tube is from 0.1 to 10:1, preferably from 0.1 to 5:1, more preferably from 0.5 to 2:1;

Preferably, the height ratio of the lower tube to the upper tube is 0.1-10:1, preferably 0.2-3:1.

4. The ascending gas-liquid dispenser of claim 3, wherein the inner tube further comprises: a baffle connecting the lower tube and the liquid phase inlet;

preferably, the included angle alpha between the liquid phase inlet and the baffle is less than or equal to 90 degrees, and preferably 60-90 degrees;

preferably, the side part of the baffle is provided with a hole-I, and the aperture ratio is 10-80%;

preferably, the level of the liquid phase inlet is provided with holes-II and the opening ratio is 5-30%.

5. An upward gas-liquid distributor according to claim 4, wherein the diameter ratio of the lower pipe and the main pipe is 1:2-25, preferably 1:2-10;

preferably, the diameter of the pipe body is 0.2-10mm, and the diameter of the main pipe is 20-50mm;

preferably, the ratio of the height of the pipe body part extending into the main pipe to the height of the main pipe is 0.01-0.8:1, preferably 0.1-0.5:1;

preferably, the portion of the tubular body extending into the main tube is selected from at least part of the upper tube and optionally part of the lower tube, preferably from the upper tube.

6. An ascending gas-liquid dispenser according to any one of claims 1-5 wherein the number of stages of gas-liquid dispersing elements is 1-5 stages, preferably 1-3 stages;

Preferably, the gas-liquid dispersing part comprises, from bottom to top: the connecting section-I, the reducing section, the connecting section-II and the expanding section are communicated in sequence;

preferably, the ratio of the inner diameter of the reducing section to the inner diameter of the main pipe is 0.1-0.8:1, preferably 0.2-0.6:1; the inner diameter ratio of the expanding section to the main pipe is 1-3:1, preferably 1-2:1;

preferably, the height ratio of the gas-liquid dispersion member and the main pipe of each stage is 0.1-0.5:1, preferably 0.2-0.3:1;

preferably, in each stage of the gas-liquid dispersing member, the height ratio of the diameter-reducing section and the diameter-enlarging section is 1:0.2-3, preferably 1:0.6-2.

7. The ascending gas-liquid distributor according to claim 6, wherein the interior of the expanded section is provided with a first hole portion, preferably selected from the group consisting of a packing and/or a perforated plate;

preferably, the porosity of the first hole part is more than or equal to 20%, preferably 50-99%; specific surface area is more than or equal to 200m ^-1 Preferably 200-2000m ^-1 。

8. The ascending gas-liquid dispenser according to any one of claims 1-7, wherein the gas-liquid diffusion component comprises: the connecting section-III and the bubble cap body are sequentially communicated, and a top outlet is arranged on the bubble cap body;

preferably, the blister body is formed by a mesh and/or screen; further preferably, the interior of the blister body is provided with a second aperture, preferably selected from the group consisting of a filler and/or a porous plate;

Preferably, the porosity of the second hole part is more than or equal to 20%, preferably 50-99%; specific surface area is more than or equal to 200m ^-1 Preferably 200-2000m ^-1 。

9. A method of gas-liquid distribution, characterized in that the method performs gas-liquid distribution in an up-going gas-liquid distributor according to any one of claims 1-8;

10. The method of claim 9, wherein the m is ³ The sum of the liquid phases is calculated as m ³ The flow ratio of the gas phase is 0.1-5:2-30, preferably 0.2-1:3-10;

preferably, the liquid phase is fed at a rate of 0.2 to 1m ³ Preferably 0.2-0.5m ³ /h；

Preferably, the gas phase has a space velocity of from 2 to 15 hours ^-1 Preferably 3-5h ^-1 ；

Preferably, the flow ratio of the gas phase through the inner pipe gas hole to the main pipe gas hole is 0.1-2:3-10, preferably 0.5-1:3-5.

11. An upgoing reactor, the upgoing reactor comprising: at least one distribution tray, an upward-type gas-liquid distributor according to any one of claims 1 to 8;

12. An upgoing reactor according to claim 11, wherein the number of distribution trays is 1-5, preferably 1-3;

preferably, the vertical distance between two adjacent distribution plates and the height ratio of the upward gas-liquid distributor are 1-50:1, preferably 2-20:1;

preferably, the height ratio of the distributor tray to the ascending gas-liquid distributor is 0.01-0.5:1, preferably 0.05-0.5:1.

13. An upward reactor according to claim 11 or 12, wherein the number of holes-III is 1-10, preferably 1-5;

preferably, the holes-III are uniformly distributed on the lower surface of the distribution plate;

preferably, the upgoing reactor further comprises: a raw material inlet and a raw material outlet, wherein the raw material inlet is arranged at the bottom of the upward reactor, and the raw material outlet is arranged at the top of the upward reactor.

14. Use of an upgoing reactor according to any of claims 11 to 13 in hydrogenation reactions.

15. An upward-type hydrogenation reactor, characterized in that the upward-type hydrogenation reactor comprises: an upgoing reactor according to any one of claims 11 to 13.