A gas-liquid distributor and an upflow hydrogenation reactor and application method thereof

Abstract

A gas-liquid distributor and an upflow hydrogenation reactor and an application method thereof, wherein the distributor riser consists of a gas-liquid inlet section (1), a float dispersion section (2) and a gas-liquid outlet section (5) from bottom to top, wherein the gas-liquid inlet section is open at the bottom, the float dispersion section is provided with a float (7) and upper and lower baffles (3) for limiting the position of the float, the upper and lower baffles are perforated plates, the outer sides of which are fixed to the inner wall of the riser, the side wall of the float dispersion section is provided with a vent (4), and the top of the gas-liquid outlet section is provided with a top outlet (6). The gas-liquid distributor provided by the present invention has a simple structure, and the size and distribution uniformity of the bubbles generated are high. The gas-liquid distributor provided by the present invention can be used in an upflow reactor, and is suitable for a hydrocarbon oil hydrogenation reactor, including a diesel or heavy oil hydrogenation reactor.

Description

Technical Field

[0001] The present invention relates to a reactor internal component and a reactor, and more particularly to a gas-liquid distributor and an upflow hydrogenation reactor. Background Art

[0002] Upflow reactor is a widely used technology in the field of petrochemical industry, such as upflow fixed bed residue oil hydrogenation reactor, fluidized bed hydrogenation reactor and suspended bed hydrogenation reactor. Since the reaction flow flows from bottom to top in the upflow reactor, compared with the traditional downflow fixed bed reactor, the upflow reactor has the advantages of good adaptability to high-metal and low-quality raw materials, high reactor space utilization, and low pressure drop. However, there are also some problems, such as uneven distribution of logistics and easy occurrence of hot spots.

[0003] In an upflow reactor, both the gas phase and the liquid phase of the reactant flow flow in the reactor from bottom to top, the liquid phase at the reactor outlet section is a continuous phase, and the hydrogen is a dispersed phase. Since the hydrogen is provided in the form of dissolved hydrogen, the hydrogen entering the reactor needs to be distributed to generate bubbles with a smaller diameter and a more uniform distribution, so as to ensure a stable hydrogen partial pressure and hydrogen dissolution rate, so that the dissolved hydrogen in the liquid phase is always in a saturated state and a small amount of hydrogen exists in the form of gas.

[0004] A gas-liquid distributor with good bubble distribution is one of the most important components in an upflow reactor. It will be directly related to the uniformity of the initial distribution of the gas-liquid two phases. An unreasonable gas-liquid distributor will cause uneven distribution of the initial materials entering the reactor.

[0005] Microbubbles have the advantages of large specific surface area, high gas content, slow bubble rise speed and fast dissolution. They are widely used in wastewater treatment, winemaking, ore flotation, oil extraction and biological breeding industries.

[0006] The formation of microbubbles is a physical phenomenon of gas-liquid two-phase flow. It is generally believed that the breakup of bubbles in turbulent fields is mainly the result of the combined action of external and internal factors. External factors mainly include flow field characteristics, liquid phase properties and other external conditions, while internal factors mainly include gas phase properties, internal forces of bubbles, etc.

[0007] Gas-liquid distributors are divided into spiral liquid type, jet type, pressure dissolution type and mechanical dispersion type according to the bubble generation method.

[0008] The spiral liquid type gas-liquid distributor uses the centrifugal effect of high-speed rotating liquid to generate microbubbles. Water enters the bottom of the device at a tangential speed through a centrifugal pump, causing the water to form a rotating flow trajectory, forming a vacuum at the center, sucking gas to form microbubbles. This type of gas-liquid distributor has been widely used in water purification and can generate microbubbles of 10-50μm.

[0009] The jet-type gas-liquid distributor uses a design similar to an orifice flowmeter or a venturi tube to increase the flow rate and reduce the pressure of the fluid due to local changes in the pipeline, thereby introducing the gas phase, or using the liquid phase vortex to create a negative pressure area in the center to introduce the gas phase, and then uses the high turbulence and shear generated by the high-speed fluid to cut the gas into microbubbles.

[0010] The pressure-dissolving gas-liquid distributor pressurizes the gas-liquid mixture to a certain pressure and then enters the pressurized tank. The gas is saturated and dissolved in the liquid. The pressure is reduced by the pressure reducing valve, and the pressure is suddenly reduced. The gas saturated and dissolved in the liquid precipitates, causing the gas to generate microbubbles. The size and distribution of the microbubbles depend on the pressure of the pressurized tank.

[0011] The mechanical dispersion gas-liquid distributor introduces water and air into a container at the same time for stirring, and cuts the gas into tiny bubbles during the high-speed shearing and stirring process.

[0012] Although microbubble technology has many advantages, the efficiency and effect of microbubble technology application need to be further improved due to the shortcomings of traditional gas-liquid distributors, such as complex structure, difficult processing and installation, high subsequent maintenance costs, and low uniformity of bubble diameter.

[0013] CN205095759U discloses an upflow gas-liquid distributor, which includes a flow guide tube and a flow mixing piece. The flow mixing piece is arranged above the upper pipe opening of the flow guide tube at intervals, and the mixed fluid passing through the flow guide tube flows out from the upper pipe opening of the flow guide tube and reaches the flow mixing piece. The device strengthens the mixing between the gas and liquid phases through the flow mixing piece, and the technical parameters such as the bubble size and distribution uniformity and the corresponding technical effects are not described.

[0014] CN203737216U discloses an upward gas-liquid distributor for a gas-liquid-solid three-phase reactor, which is composed of a rain cap, a distribution plate, a gas-liquid riser, an air inlet pipe, a connector and a baffle. The distributor has an inhibitory effect on the amount of large bubbles generated, and can improve the efficiency of gas-liquid mass transfer in the reactor, but the distributor has small operational flexibility, a complex structure and is limited to the distribution of gas-liquid mixed materials before the catalyst bed.

[0015] CN202621143U discloses an upward gas-liquid distributor, including a distribution pipe and a distribution plate, wherein the upper end of the distribution pipe is in fluid communication with the distribution plate, and the lower end of the distribution pipe is provided with an angled opening; the gas-liquid distributor also includes a baffle, the angled opening is connected to the baffle, and the baffle covers the angled opening; a gas channel is provided on the wall of the distribution pipe. Compared with the prior art, the invention has the advantages of high uniformity of gas-liquid distribution, high operational flexibility, simple structure, convenient processing and manufacturing, and investment saving. However, the gas-liquid distributor does not have the function of radial diffusion of gas.

[0016] CN 209302719 U discloses an upward gas-liquid distributor for chemical industry. The upward gas-liquid distributor comprises a round tube, which is fixedly mounted on a distribution plate. The round tube is provided with n slide grooves, and the slide grooves are provided with exhaust holes and blocks, wherein the blocks are fixedly connected to the upper cover through a connecting column, and the upper cover is installed on the round tube; the upper cover is connected to the round plate through a thread, and a sliding column is fixedly installed on the round plate, and the lower end of the sliding column passes through a fixing frame, a spring, and a fixing plate in sequence, and is fixedly installed on the circular baffle, wherein the fixing frame is fixedly connected to the inner wall of the round tube, wherein one end of the spring is fixedly mounted on the fixing frame, and the other end thereof is fixedly mounted on the fixing plate, and the fixing plate is fixed on the sliding column; the circular baffle is located in the inner cavity of the gas-liquid riser, and the gas-liquid riser is inserted in the through hole, and the through hole is arranged on the distribution plate. The structure of the gas-liquid distributor is complex. Summary of the invention

[0017] One of the technical problems to be solved by the present invention is to provide a gas-liquid distributor with a simple structure on the basis of the prior art, which has the characteristics of high uniformity of generated bubbles and good radial diffusion of bubbles.

[0018] The second technical problem to be solved by the present invention is to provide an upflow hydrogenation reactor provided with the above-mentioned gas-liquid distributor and an application method thereof.

[0019] The gas-liquid distributor provided by the present invention comprises a distributor riser tube which is composed of a gas-liquid inlet section 1, a float dispersion section 2 and a gas-liquid outlet section 5 from bottom to top, wherein the gas-liquid inlet section is open at the bottom, a float 7 and upper and lower baffles 3 for limiting the position of the float are arranged in the float dispersion section, the upper and lower baffles are perforated plates, the outer sides of which are fixed to the inner wall of the riser tube, a vent hole 4 is arranged on the side wall of the float dispersion section, and a top outlet 6 is arranged at the top of the gas-liquid outlet section.

[0020] The working process of the gas-liquid distributor provided by the present invention is that the liquid phase enters the gas-liquid distributor through the bottom opening of the gas-liquid inlet section, flows upward into the float dispersion section, causing the float to rotate and float up and down; the gas phase enters the gas-liquid distributor through the vent holes on the side wall of the float dispersion section, and the gas and liquid are mixed in the narrow gap between the float and the inner wall of the riser in the float dispersion section. Due to the narrowing of the flow channel, the flow velocity increases, the gas-liquid turbulence is enhanced, and the gas is sheared into multiple small bubbles. After the gas and liquid phases are fully mixed, they flow upward into the gas-liquid outlet section, and the bubbles are diffused and discharged through the top outlet.

[0021] The upflow hydrogenation reactor provided by the present invention comprises a reactor shell, a hydrogenation catalyst bed in the shell, a raw material inlet at the bottom, a hydrogen inlet and a product outlet at the top, a baffle is arranged under the hydrogenation catalyst bed, the baffle is provided with holes, and the above-mentioned gas-liquid distributor is arranged corresponding to the holes, and the hydrogen inlet is located at the lower part of the reactor shell.

[0022] The application method of the upflow hydrogenation reactor provided by the present invention comprises the following steps: hydrocarbon oil feedstock enters the reactor from a bottom feedstock inlet, enters a gas-liquid distributor through a bottom opening, enters a float dispersion section through a gas-liquid inlet section, hydrogen enters the reactor from a hydrogen inlet, enters the float dispersion section through a vent hole, gas-liquid two-phases are mixed in a narrow gap between the float and the inner wall of a riser tube to generate tiny bubbles, gas-liquid two-phases rise to a gas-liquid outlet section, are dispersed and overflow the gas-liquid distributor through a top outlet, contact with a hydrogenation catalyst bed layer to carry out a hydrogenation reaction, and the post-reaction flow flows out of the reactor through an upper product outlet.

[0023] The gas-liquid distributor provided by the present invention has the following beneficial effects:

[0024] The gas-liquid distributor provided by the present invention has a simple structure, generates bubbles with a small diameter and high distribution uniformity, and has good radial diffusion of the bubbles.

[0025] The upflow hydrogenation reactor and its application method provided by the present invention have the following beneficial effects:

[0026] The upflow hydrogenation reactor provided by the present invention adopts the above-mentioned gas-liquid distributor, which can fully mix hydrogen with hydrocarbon oil raw materials and promote mass transfer of hydrogen in hydrocarbon oil. The upflow hydrogenation reactor is suitable for wax oil, residual oil, diesel or heavy oil hydrogenation process. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] Figure 1 The figure is a schematic structural diagram of an implementation scheme of a gas-liquid distributor.

[0028] Figure 2A , Figure 2B Schematic diagrams of the structures of two implementation modes of the gas-liquid distributor.

[0029] Figure 3 This is a schematic diagram of the top of the gas-liquid distributor.

[0030] Figure 4 This is a cross-sectional view of the gas-liquid distributor.

[0031] Figure 5 Schematic diagram of the structure of the porous float.

[0032] Figure 6 This is a schematic diagram of the structure of installing a gas-liquid distributor in an upflow hydrogenation reactor.

[0033] Figure 7 This is a schematic diagram of the structure of the gas-liquid distributor in Comparative Example 1.

[0034] Description of reference numerals:

[0035] 1. Gas-liquid inlet section; 2-float dispersion section; 3-upper and lower baffles; 4, 13-vents; 5-gas-liquid outlet section, 6, 14-top outlet; 7-float, 8-through hole; 9-baffle; 10-raw material inlet; 11-hydrogen inlet; 12-riser pipe. DETAILED DESCRIPTION

[0036] The specific embodiments of the present invention are described in detail below.

[0037] In the present invention, the directional words used should be appropriately interpreted in conjunction with the context and directions in actual use, wherein "bottom" refers to the position of 0%-10% of the container from bottom to top, "lower" refers to the position of 0%-50% of the container from bottom to top, "upper" refers to the position of 50%-100% of the container from bottom to top, and "top" refers to the position of 90%-100% of the container from bottom to top.

[0038] In the first aspect, the present invention provides a gas-liquid distributor, wherein the distributor riser pipe is composed of a gas-liquid inlet section 1, a float dispersion section 2 and a gas-liquid outlet section 5 from bottom to top, wherein the gas-liquid inlet section is open at the bottom, the float dispersion section is provided with a float 7 and upper and lower baffles 3 for limiting the position of the float, the upper and lower baffles are perforated plates, the outer sides of which are fixed to the inner wall of the riser pipe, the side wall of the float dispersion section is provided with a vent hole 4, and the top of the gas-liquid outlet section is provided with a top outlet 6.

[0039] In the gas-liquid distributor provided by the present invention, the gas-liquid inlet section, the float dispersion section and the gas-liquid outlet section have the same inner diameter, and the height ratio of the gas-liquid inlet section, the float dispersion section and the gas-liquid outlet section is 1-2:2-6:1-3, preferably 1-2:2-5:1-3.

[0040] Preferably, the height of the gas-liquid inlet section is 10-20 mm, the height of the float dispersion section is 20-60 mm, preferably 20-50 mm, and the height of the gas-liquid outlet section is 10-30 mm.

[0041] In the gas-liquid distributor provided by the present invention, one or more groups of upper and lower baffles, floats and vents are arranged axially in the float dispersion section. Preferably, at least two groups of upper and lower baffles, floats and vents are arranged axially in the float dispersion section.

[0042] One or more floats may be provided in each set of upper and lower baffles, floats and vents in the float dispersion section. Preferably, one float is provided in each set of upper and lower baffles, floats and vents.

[0043] The openings on the upper and lower baffles are symmetrical and cooperate with the float to limit the position of the float. Preferably, the diameter of the float is 5-60 mm, the ratio of the distance between the upper and lower baffles to the diameter of the float is 1-5:1, preferably 1-2:1, the ratio of the diameter of the openings of the upper and lower baffles to the diameter of the float is 0.1-0.9:1, preferably 0.3-0.8:1, and the outer diameter of the upper and lower baffles cooperates with the side wall of the float dispersion section.

[0044] Preferably, the diameter of the float ball is 5-30 mm.

[0045] The side wall of the floating ball dispersion section is provided with ventilation holes, and the equivalent diameter of the ventilation holes is 1-10 mm, preferably 2-8 mm. The present invention has no limitation on the number of ventilation holes, and preferably the number of ventilation holes is 2-8.

[0046] Preferably, the float is a porous structure, and the material of the float is selected from one or more of polypropylene, rubber, stainless steel, cast iron and polyvinylidene fluoride. Preferably, a plurality of through holes are opened in the float, and the diameter of the through holes is 1-5 mm, preferably 1-3 mm; the present invention has no limitation on the number of through holes in a single float, and preferably the number of through holes in a single float is 10-50, more preferably 10-30.

[0047] A top outlet is provided at the top of the gas-liquid outlet section, and the top outlet is in the shape of an inverted truncated cone with a small bottom and a large top. The cone angle of the top outlet refers to the cone angle formed by the extension and intersection of the side walls of the truncated cone. Preferably, the top outlet height is 10-40mm, the lower diameter of the top outlet is 1-30mm, the upper diameter of the top outlet is 20-80mm, and the cone angle is 30°-150°. More preferably, the top outlet height is 10-30mm, the lower diameter of the top outlet is 3-20mm, the upper diameter of the top outlet is 20-60mm, and the cone angle is 60°-90°.

[0048] Preferably, a porous plate is provided on the top of the top outlet, and the opening rate of the porous plate is 5%-20%.

[0049] Preferably, the equivalent diameter of the holes on the multi-well plate is 1-10 mm, preferably 1-5 mm.

[0050] The gas-liquid inlet section, the float dispersion section and the top outlet section are movably connected, preferably in a threaded connection.

[0051] In the gas-liquid distributor provided by the present invention, the riser is preferably in a circular tube shape, and the gas-liquid inlet section is a circular tube with an opening at the bottom. Preferably, the bottom of the gas-liquid inlet section is a perforated plate with an opening rate of 5% to 20%, preferably 5%-10%.

[0052] The gas-liquid distributor provided by the present invention has a liquid entering the gas-liquid distributor through the bottom inlet of the gas-liquid inlet section, and flows upward into the float dispersion section. The liquid phase flows upward to cause the float to rotate and float up and down. The gas enters the gas-liquid distributor through the vent holes on the side wall of the float dispersion section. The gas and liquid are mixed in the narrow gap between the float and the inner wall of the riser in the float dispersion section. The gas and liquid bypass the float, and the flow velocity increases due to the narrowing of the flow channel, and the gas-liquid turbulence is enhanced. The gas entering from the vent holes is sheared into a plurality of small bubbles of different sizes under the action of the high-speed liquid flow, and the small bubbles are fully mixed with the liquid phase as the float moves. The gas and liquid flow upward into the gas-liquid outlet section, and the bubbles rise to reach the gas-liquid outlet section and are discharged through the top outlet for diffusion.

[0053] In a second aspect, the present invention provides an upflow hydrogenation reactor, comprising a reactor shell, a hydrogenation catalyst bed in the shell, a raw material inlet at the bottom, a hydrogen inlet and a product outlet at the top, a baffle is arranged under the hydrogenation catalyst bed, the baffle has holes, and the above-mentioned gas-liquid distributor is arranged corresponding to the holes, and the hydrogen inlet is located at the lower part of the reactor shell.

[0054] The present invention provides an upflow hydrogenation reactor, wherein the gas-liquid distributor can be arranged above the baffle plate, or arranged below the baffle plate. When the gas-liquid distributor is located above the baffle plate, the hydrogen inlet can be located above the baffle plate. When the gas-liquid distributor is located below the baffle plate, in order to ensure the passage of hydrogen, the hydrogen inlet must be located below the baffle plate.

[0055] Preferably, the gas-liquid distributor is arranged below the baffle plate, the hydrogen inlet is located at the lower part of the baffle plate, and the top outlet of the gas-liquid distributor is communicated with the opening on the baffle plate.

[0056] In a third aspect, the present invention provides an application method of an upflow hydrogenation reactor, wherein a hydrocarbon oil feedstock enters the reactor from a bottom feedstock inlet, enters a gas-liquid distributor through a bottom opening, and enters a float dispersion section through a gas-liquid inlet section; hydrogen enters the reactor from a hydrogen inlet, and enters a float dispersion section through an air vent; a gas-liquid two-phase mixture is generated in a narrow gap between the float and an inner wall of a riser tube by generating tiny bubbles; the gas-liquid two-phase mixture rises to a gas-liquid outlet section, is dispersed and overflows the gas-liquid distributor through a top outlet, contacts a hydrogenation catalyst bed layer for hydrogenation reaction, and flows out of the reactor through an upper product outlet after the reaction.

[0057] The hydrocarbon oil raw material is preferably one or more of gasoline, diesel, residual oil, wax oil and lubricating oil.

[0058] The above content describes in detail the preferred embodiments of the present invention. However, the present invention is not limited to the specific details in the above embodiments. Within the technical concept of the present invention, the technical solution of the present invention can be subjected to a variety of simple modifications, and these simple modifications all belong to the protection scope of the present invention.

[0059] The structure and effect of the gas-liquid distributor and upflow hydrogenation reactor provided by the present invention are described below with reference to the accompanying drawings.

[0060] Attached Figure 1 The schematic diagram of the structure of an embodiment of the gas-liquid distributor provided by the present invention. The liquid riser of the gas-liquid distributor is composed of a gas-liquid inlet section 1, a float dispersion section 2 and a gas-liquid outlet section 5 from bottom to top, wherein the gas-liquid inlet section is open at the bottom, and the float dispersion section is provided with a float 7 and upper and lower baffles 3 for limiting the position of the float. The upper and lower baffles are orifice plates with a central opening, and the outer side is fixed to the inner wall of the liquid riser. Figure 1 In the embodiment, a float is provided in the float dispersion section, a vent 4 is provided on the side wall of the riser between the upper and lower baffles 3, and an inverted truncated cone-shaped top outlet 6 is provided on the top of the gas-liquid outlet section 5.

[0061] Attached Figure 2A , attached Figure 2B The following are structural schematic diagrams of two embodiments of the gas-liquid distributor provided by the present invention. Figure 2A As shown, the float dispersion section is provided with two groups of upper and lower baffles 3, floats 7 and vents 4 along the axial direction, and the floats 7 in each group of structures are respectively restricted by the upper and lower baffles 3 in a relatively fixed position. Figure 2B In the illustrated embodiment, three groups of upper and lower baffles 3, floats 7 and vents 4 are axially arranged in the float dispersion section, and the floats 7 in each group of structures are respectively restricted by the upper and lower baffles 3 in relatively fixed positions.

[0062] Attached Figure 3 This is a schematic diagram of the top structure of the gas-liquid distributor. Figure 3 As shown, a porous plate is provided at the top of the top outlet 6 of the gas-liquid distributor, and holes are opened on the porous plate, and the opening rate is 5-20%.

[0063] Attached Figure 4 This is a cross-sectional view of the gas-liquid distributor. Figure 4 It can be seen that in the float dispersion section 2, the float 7 is confined between the upper and lower baffles 3, and the distance between the upper and lower baffles is greater than the diameter of the float. The top of the gas-liquid outlet section 5 is provided with an inverted truncated cone-shaped top outlet 6.

[0064] Attached Figure 5 The structure diagram of the porous float is shown in FIG. The float is provided with a plurality of evenly distributed through holes 8, and the diameter of the through holes is 1-5 mm.

[0065] Attached Figure 6 This is a schematic diagram of the structure of the gas-liquid distributor installed in the upflow hydrogenation reactor. Figure 6 It can be seen that a baffle plate 9 is arranged at the lower part of the shell of the upflow hydrogenation reactor, and a hole is opened on the baffle plate. Any of the above-mentioned gas-liquid distributors is arranged corresponding to the hole. A raw material inlet 10 is arranged at the bottom of the shell of the upflow hydrogenation reactor, and the raw material inlet is located below the baffle plate 9. The hydrogen inlet is also located below the baffle plate 9.

[0066] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner without contradiction. In order to avoid unnecessary repetition, the present invention will not further describe various possible combinations.

[0067] The structure and effect of the gas-liquid distributor and hydrocarbon oil hydrogenation reactor provided by the present invention are further illustrated by examples below, but the present invention is not limited thereto.

[0068] Comparative Example 1

[0069] The gas-liquid distributor in the prior art is used as a comparison benchmark. Figure 7 .Depend on Figure 7 It can be seen that the structure of the gas-liquid distributor includes a gas-liquid phase inlet 11, a riser 12, a middle opening 13 and a top porous plate 14. The gas-liquid distributor tube has an inner diameter of 50 mm and a length of 100 mm. Two vents with a diameter of 5 mm are opened in the middle of the tube. The top structure of the riser is a porous plate structure with 20 holes and a diameter of 3 mm.

[0070] Gas-liquid distribution method in comparative example 1: the liquid phase of the gas-liquid distributor directly enters the riser from the lower port, and the gas phase enters from the side of the tube. After the two are mixed, they move upward, and bubbles are formed at the middle opening and overflow directly from the top into the upflow reactor.

[0071] (1) Cold mold test process:

[0072] The bubble diameter of the liquid in the cross section is measured and the distribution unevenness factor M is used f To indicate the difference in the distribution of bubble diameter in the cross section. The uneven distribution factor M f The calculation formula is as follows:

[0073]

[0074] Where n is the number of conductivity probe measurement points; a i is the bubble diameter at the i-th probe measurement point, and a is the average bubble diameter at n probe measurement points. f The calculation results are shown in Table 1.

[0075] (2) Gas holdup measurement process: The volume expansion method is used to measure the initial liquid level and the liquid level after bubbling, and the gas holdup E in the liquid phase is calculated. a , the calculation formula is as follows:

[0076]

[0077] Among them, H i is the initial liquid level height; H n is the liquid level after bubbling; gas holdup E a The results are shown in Table 2.

[0078] (3) Bubble diameter measurement process

[0079] The bubble diameter of the liquid on the cross section was measured, and the average bubble diameter was used to represent the mixing effect between the gas and liquid phases. The results are shown in Table 3.

[0080] (4) Bubble rise rate measurement process

[0081] The bubble rise rate of the liquid on the cross section was measured and used to represent the mixing effect of the gas-liquid two phases. The results are shown in Table 4.

[0082] Example 1

[0083] A baffle is provided at the lower part of the upflow reactor, and a hole is formed on the baffle. The gas-liquid distributor is provided corresponding to the hole. The raw material inlet is located at the bottom of the reactor, and the gas phase inlet is located below the baffle. The float dispersion section of the gas-liquid distributor has a float along the axial direction, and the structure is as shown in the attached figure. Figure 1 As shown, the diameter of the riser is 20mm and the length is 100mm. The distributor riser consists of a gas-liquid inlet section 1, a float dispersion section 2 and a gas-liquid outlet section 5 from bottom to top, and the heights of each section are 10mm, 50mm and 20mm respectively. The float dispersion section is provided with a float 7 and upper and lower baffles 3 that limit the position of the float. The float dispersion section has a porous float, which is made of stainless steel. Each float structure is fixed within a certain range by two baffles. The distance between each set of upper and lower baffles is 10mm, and the diameter of the baffle opening is 2mm. The float diameter is 5mm, the float through hole diameter is 1mm, the number of openings is 10 and is evenly distributed on the sphere, and the tube wall between the upper and lower baffles is provided with two vents with a diameter of 2mm. The lower diameter of the top outlet of the gas-liquid outlet section is 4mm, the upper diameter is 20mm, the top outlet height is 12mm, and the cone angle is about 67°. The gas enters from the vent in the middle of the riser.

[0084] Gas-liquid distribution method:

[0085] The liquid phase of the gas-liquid distributor enters the riser from the bottom opening, and the gas phase enters from the air holes on the side wall of the float segment. The gas and liquid phases are preliminarily mixed after passing through the float, and then move upward after mixing, reaching the top outlet of the gas-liquid outlet segment and overflowing into the upflow reactor.

[0086] Example 2

[0087] The structure of the upflow reactor is the same as that of Example 1. The gas-liquid distributor adopts a float dispersion section with two floats along the axial direction. The structure is as shown in the attached figure. Figure 2A As shown, the diameter of the riser is 20 mm, the length is 90 mm, and there are two groups of porous float structures in the middle. The floats are made of polypropylene. Each float structure is fixed within a certain range by two baffles. The distance between each group of baffle structures is 15 mm, and the diameter of the baffle opening is 6 mm. The float has a diameter of 10 mm, and there are through holes in the float. The through hole diameter is 2 mm. The number of openings is 10 and evenly distributed throughout the sphere. There are two 2 mm diameter vents on the side wall of the float dispersion section in the middle of the riser. The lower diameter of the top outlet of the gas-liquid outlet section is 3 mm, the upper diameter is 20 mm, the top outlet height is 12 mm, and the cone angle is about 70°.

[0088] Gas-liquid distribution method:

[0089] The liquid phase of the gas-liquid distributor directly enters the riser from the lower port, and the gas phase enters from the side of the tube. The gas and liquid phases are preliminarily mixed after passing through the first float. After that, the two phases move upward to the second float after mixing, and are dispersed and mixed again with the gas entering from the second vent, and then directly overflow into the upflow reactor when they reach the top opening.

[0090] The cold mold test process is the same as that of comparative example 1, and the uneven distribution factor M f The measurement and calculation methods are the same as those in Comparative Example 1. The calculation results are shown in Table 1. Gas holdup E a The results are shown in Table 2.

[0091] Example 3

[0092] The structure of the upflow reactor is the same as that of Example 1. The gas-liquid distributor has three floats in the float dispersion section along the axial direction. Figure 2BAs shown in the figure, the gas-liquid distributor has a diameter of 30 mm and a length of 100 mm. There are three porous float structures in the middle. The floats are made of stainless steel. Each float structure is fixed within a certain range by two baffles. The distance between each set of upper and lower baffle structures is 15 mm, and the diameter of the baffle opening is 12 mm. The float has a diameter of 15 mm, and the float has a through hole with a diameter of 2 mm. The number of openings is 20 and is evenly distributed throughout the sphere. There are two vents with a diameter of 4 mm on the side wall of the float dispersion section. The lower diameter of the top outlet of the gas-liquid outlet section is 5.6 mm, the upper diameter is 30 mm, the top outlet height is 12 mm, and the cone angle is about 90°.

[0093] Gas-liquid distribution method:

[0094] The liquid phase of the gas-liquid distributor directly enters the riser from the lower port, and the gas phase enters from the first vent hole on the side wall of the tube. The gas and liquid phases are preliminarily mixed after passing through the first float, and then move upward to the second float after mixing, and are dispersed and mixed again with the gas entering from the second vent, and then continue to mix and disperse with the gas and liquid phases in the third float, and finally reach the top opening and directly overflow into the upflow reactor.

[0095] The cold mold test process is the same as that of comparative example 1, and the uneven distribution factor M f The measurement and calculation methods are the same as those in Comparative Example 1. The calculation results are shown in Table 1. Gas holdup E a The results are shown in Table 2.

[0096] Table 1

[0097] Examples <![CDATA[Distribution non-uniformity factor M f > Comparative Example 1 0.201 Example 1 0.135 Example 2 0.121 Example 3 0.107

[0098] The uneven distribution factor indicates the gas-liquid two-phase distribution effect, and the smaller the value, the more uniform the distribution. As can be seen from Table 1, compared with Comparative Example 1, the uneven distribution factor of the gas-liquid distributor provided by the present invention is smaller than that of the comparative example, indicating that it has better distribution performance.

[0099] Table 2

[0100] Examples <![CDATA[Gas holdup E a , %]]> Comparative Example 1 4.683 Example 1 6.472 Example 2 6.895 Example 3 7.268

[0101] Generally speaking, the greater the gas content, the better the fluid distribution performance. As can be seen from Table 2, compared with Comparative Example 1, the float structure of the gas-liquid distributor provided by the present invention can provide a greater mass transfer driving force, thereby increasing the mass transfer rate. Compared with Comparative Example 1, the gas content of Examples 1-3 of the gas-liquid distributor provided by the present invention is higher. It can be seen that compared with the prior art, the gas-liquid distributor of the present invention has a larger gas content and therefore has better distribution performance.

[0102] Table 3

[0103] Examples Average bubble diameter d / mm Comparative Example 1 7.95 Example 1 7.82 Example 2 6.26 Example 3 5.14

[0104] According to Table 3, the average bubble diameter of the gas-liquid distributor in Comparative Example 1 is 7.95 mm, while the bubble diameters of the gas-liquid distributors in Examples 1-3 are smaller. This indicates that the mixing effect of the gas-liquid distributor provided by the present invention is slightly better than that of the gas-liquid distributor in Comparative Example 1, and the increase in the number of floating balls can effectively enhance the mixing effect between the gas and liquid phases, making the generated bubble diameter smaller. Compared with the prior art, the gas-liquid distributor of the present invention has a smaller bubble diameter and therefore has better mixing performance.

[0105] Table 4

[0106] Examples Average bubble rising speed um / s Comparative Example 1 0.702 Example 1 0.351 Example 2 0.241 Example 3 0.167

[0107] Compared with the comparative example, the gas-liquid distributor provided by the present invention has a smaller bubble rising rate, and the bubble residence time is longer, resulting in a larger gas-liquid two-phase contact area, and thus has better mixing performance.

[0108] In the process of gas-liquid co-current upward flow and reaction, generally speaking, a smaller bubble diameter is conducive to increasing the gas-liquid mass transfer surface area and extending the bubble residence time, both of which are conducive to enhancing the mass transfer effect. For hydrogenation reactions, it is equivalent to increasing the contact time between hydrogen and oil materials, achieving the effect of further improving the mass transfer and reaction rate between the gas and liquid phases. Therefore, no matter from which aspect, minimizing the bubble size is beneficial for the upflow or all-liquid phase hydrogenation reaction process.

Claims

1. A gas-liquid distributor, characterized in that: The distributor riser pipe is composed of a gas-liquid inlet section (1), a float dispersion section (2) and a gas-liquid outlet section (5) from bottom to top, wherein the gas-liquid inlet section is open at the bottom, the float dispersion section is provided with a float (7) and upper and lower baffles (3) for limiting the position of the float, the upper and lower baffles are perforated plates, the outer sides of which are fixed to the inner wall of the riser pipe, the side wall of the float dispersion section is provided with a vent hole (4), and the top of the gas-liquid outlet section is provided with a top outlet (6); The height ratio of the gas-liquid inlet section, the float dispersion section and the gas-liquid outlet section is 1-2:2-6:1-3; the ratio of the distance between the upper and lower baffles to the float diameter is 1-5:1, and the ratio of the opening aperture on the upper and lower baffles to the float diameter is 0.1-0.9:1; a through hole is provided in the float.

2. The gas-liquid distributor according to claim 1, characterized in that: The inner diameters of the gas-liquid inlet section, the float dispersion section and the gas-liquid outlet section are equal; The height of the gas-liquid inlet section is 10-20 mm, the height of the float dispersion section is 20-60 mm, and the height of the gas-liquid outlet section is 10-30 mm.

3. The gas-liquid distributor according to claim 1 or 2, characterized in that: At least two groups of upper and lower baffles, floating balls and vent holes are arranged in the axial direction in the floating ball dispersion section (2).

4. The gas-liquid distributor according to claim 3, characterized in that: A float is arranged in each group of the upper and lower baffles, the float and the vent hole structure of the float dispersion section (2).

5. The gas-liquid distributor according to claim 1 or 2, characterized in that: The ratio of the distance between the upper and lower baffles to the diameter of the float is 1-2:1, and the ratio of the aperture of the openings on the upper and lower baffles to the diameter of the float is 0.3-0.8:

1.

6. The gas-liquid distributor according to claim 1 or 2, characterized in that: The diameter of the float ball is 5 to 60 mm.

7. The gas-liquid distributor according to claim 6, characterized in that: The diameter of the float ball is 5-30 mm.

8. The gas-liquid distributor according to claim 1 or 2, characterized in that: The equivalent diameter of the vent hole is 1 to 10 mm.

9. The gas-liquid distributor according to claim 8, characterized in that: The equivalent diameter of the vent hole is 2 to 8 mm.

10. The gas-liquid distributor according to claim 8, characterized in that: The number of the vent holes on the side wall of the riser pipe between each section of the upper and lower baffles is 2-8.

11. The gas-liquid distributor according to claim 1 or 2, characterized in that: The float ball has a porous structure; the material of the float ball is selected from one or more of polypropylene, rubber, stainless steel, cast iron and polyvinylidene fluoride.

12. The gas-liquid distributor according to claim 1 or 2, characterized in that: The diameter of the through holes in the float ball is 1-5 mm, and the number of through holes in a single float ball is 10-50.

13. The gas-liquid distributor according to claim 12, characterized in that: The diameter of the through hole is 1-3 mm, and the number of through holes in a single float is 10-30.

14. The gas-liquid distributor according to claim 1 or 2, characterized in that: The height of the top outlet is 10-40 mm, the diameter of the lower part of the top outlet is 1-30 mm, the diameter of the upper part of the top outlet is 20-80 mm, and the cone angle is 30°-150°.

15. The gas-liquid distributor according to claim 14, characterized in that: The height of the top outlet is 10-30 mm, the diameter of the lower part of the top outlet is 3-20 mm, the diameter of the upper part of the top outlet is 20-60 mm, and the cone angle is 60° to 90°.

16. The gas-liquid distributor according to claim 1 or 2, characterized in that: A porous plate is arranged on the top of the top outlet, and the opening rate of the porous plate is 5%-20%.

17. The gas-liquid distributor according to claim 1 or 2, characterized in that: The gas-liquid inlet section, the float dispersion section and the gas-liquid outlet section are movably connected.

18. An upflow hydrogenation reactor, characterized in that: The invention comprises a reactor shell, a hydrogenation catalyst bed in the shell, a raw material inlet at the bottom, a hydrogen inlet and a product outlet at the top, a baffle is arranged under the hydrogenation catalyst bed, the baffle has holes, and a gas-liquid distributor according to any one of claims 1 to 17 is arranged corresponding to the holes, and the hydrogen inlet is located at the lower part of the reactor shell.

19. The upflow hydrogenation reactor according to claim 18, characterized in that: The gas-liquid distributor is arranged at the lower part of the baffle plate, and the hydrogen inlet is located at the lower part of the baffle plate.

20. The method for applying the upflow hydrogenation reactor according to claim 18 or 19, characterized in that: The hydrocarbon oil feedstock enters the reactor from the bottom feedstock inlet, enters the gas-liquid distributor through the bottom opening, and enters the float dispersion section through the gas-liquid inlet section. Hydrogen enters the reactor from the hydrogen inlet and enters the float dispersion section through the vent. The gas and liquid phases mix in the narrow gap between the float and the inner wall of the riser to generate tiny bubbles. The gas and liquid phases rise to the gas-liquid outlet section, overflow the gas-liquid distributor through the top outlet, contact the hydrogenation catalyst bed to carry out hydrogenation reaction, and the post-reaction flow flows out of the reactor through the upper product outlet.

21. The method for applying the upflow hydrogenation reactor according to claim 20, characterized in that: The hydrocarbon oil raw material is one of gasoline, diesel, residual oil, wax oil and lubricating oil, or a mixture of several of them.

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