Gas-liquid distributor, reactor for synthesizing methyl isobutyl ketone and method thereof

Abstract

The invention relates to a gas-liquid distributor, a reactor for synthesizing methyl isobutyl ketone and a method thereof. The gas-liquid distributor comprises a distribution plate, liquid discharging holes formed in the distribution plate, and a gas discharging pipe which is arranged on the distribution plate and extends upwards. And by arranging the gas-liquid distributor with the gas descending pipe and the liquid descending hole, redistribution by using a filler is avoided, and the gas phase and the liquid phase are ensured to uniformly enter a tube pass. The gas-liquid distributor is simple in structure and good in distribution effect. Regular packing and honeycomb packing do not need to be arranged any more, and it can be guaranteed that gas-phase and liquid-phase fed materials enter a tube pass and flow is uniform only through the gas-liquid distributor.

Description

[0001] Field

[0002] The invention relates to a reaction device for synthesizing methyl isobutyl ketone, in particular to a gas-liquid distributor; meanwhile, the invention also relates to a reactor and a method for synthesizing methyl isobutyl ketone. Background Art

[0003] Methyl isobutyl ketone (MIBK) is an excellent medium-boiling point solvent with stable chemical properties. It can meet the special requirements of high-end coatings such as solid components, volatilization rate, leveling, coating strength, and appearance. Methyl isobutyl ketone has become the main auxiliary solvent for high-end coatings because of its good solubility, excellent miscibility with other solvents, and suitable boiling point.

[0004] At present, the mainstream technology of methyl isobutyl ketone is the one-step acetone process. The one-step methyl isobutyl ketone production process has the advantages of short process, low investment, high acetone conversion rate, high methyl isobutyl ketone selectivity, low raw material consumption and energy consumption. Among them, the acetone condensation hydrogenation reaction is a gas-liquid-solid three-phase reaction. The reactor structure is complex and the manufacturing requirements are high. The reactor is a shell-and-tube fixed bed reactor with heat transfer medium entering and exiting between the tubes. The tubes are fixed on the tube plate; the tube side is the reaction material, the shell side is the heat transfer medium, and baffles are installed between the tubes. The normal working pressure of the reactor is 3.0MPa, and the reaction temperature is 90-130℃. In order to ensure uniform distribution of materials, a distributor, a structured packing and a honeycomb are arranged in sequence on the upper part of the reactor; the lower part of the reactor is a wedge-shaped support plate, and the catalyst (such as attached) is loaded in the tube and on the support plate. Figure 6 However, the distributor design of this reactor is complicated.

[0005] In view of this, developing a gas-liquid distributor with a simple structure and capable of allowing the gas and liquid phases to enter the pipe evenly has become an urgent problem to be solved by technical personnel in this field. Summary of the invention

[0006] In order to solve the problems existing in the prior art, the present invention provides a gas-liquid distributor with a gas downcomer and a liquid downhole, which avoids redistribution by using fillers and ensures that the gas and liquid phases enter the pipe process evenly.

[0007] One of the objectives of the present invention is to provide a gas-liquid distributor.

[0008] The gas-liquid distributor of the present invention comprises a distribution plate, a lower liquid hole opened on the distribution plate, and a downcomer arranged on the distribution plate and extending upward.

[0009] In a preferred embodiment of the present invention, the distribution plate is in the form of a flat plate, preferably a disc, more preferably a disc; and / or

[0010] There are multiple downcomers, which are preferably evenly distributed on the distribution plate; and / or

[0011] There are multiple downholes, which are preferably evenly distributed on the distribution plate, and more preferably, the downholes are arranged between two adjacent downcomers.

[0012] In a preferred embodiment of the present invention, the inner diameter of the downcomer is 15 to 50 mm, preferably 19 to 44 mm; and / or

[0013] The height of the downcomer is 10 to 50 cm, preferably 20 to 30 cm.

[0014] In a preferred embodiment of the present invention, the shape of the lower liquid hole is any one of circular, square, rhombus, pentagonal, and hexagonal; preferably, the lower liquid hole is circular, and the inner diameter of the lower liquid hole is 1 to 6 mm, preferably 0.5 to 5 mm.

[0015] In a preferred embodiment of the present invention, the ratio of the distance between the centers of two adjacent downcomers to the inner diameter of the downcomers is 1.2 to 1.5:1; and / or

[0016] The ratio of the hole center distance between two adjacent down-liquid holes to the inner diameter of the downcomer is 1.2-1.5:1.

[0017] A second object of the present invention is to provide a reactor for synthesizing MIBK.

[0018] The reactor of the present invention comprises, from bottom to top, a first tube sheet, a heat exchange tube bundle, a second tube sheet, a gas-liquid distributor according to one of the purposes of the present invention, a feed nozzle arranged on the side wall of the reactor, and a hydrogen feed pipe arranged on the top of the reactor; wherein the distribution plate of the gas-liquid distributor is horizontally arranged in the reactor.

[0019] In a preferred embodiment of the present invention, the distance between the distribution plate and the second tube sheet is 5 to 150 mm, preferably 50 to 100 mm.

[0020] In a preferred embodiment of the present invention, the heat exchange tube bundle includes a plurality of vertically arranged heat exchange tubes, and the plurality of heat exchange tubes correspond vertically to the plurality of lower liquid holes one by one.

[0021] In a preferred embodiment of the present invention, in the horizontal direction, a feed baffle is vertically provided between the feed nozzle and the downcomer, the outer edge of the side of the feed baffle is fixed on the side wall of the reactor, and the lower edge thereof is higher than the distribution plate; the orthographic projection of the feed baffle on the side wall of the reactor covers the feed nozzle;

[0022] Preferably,

[0023] The vertical distance between the lower edge of the feed baffle and the distribution plate is 1 / 15 to 1 / 2 of the height of the downcomer; and / or

[0024] The horizontal distance between the middle of the feed baffle and the feed nozzle is 1 / 4 to 1 of the diameter of the feed nozzle.

[0025] The third object of the present invention is to provide a method for synthesizing MIBK.

[0026] The method for synthesizing methyl isobutyl ketone of the present invention is carried out by using the reactor of the second object of the present invention; preferably, acetone enters the reactor from the feed nozzle, and hydrogen enters the reactor from the hydrogen feed pipe; acetone and hydrogen enter the heat exchange tube bundle from the lower liquid hole and the downcomer respectively to react and obtain a methyl isobutyl ketone product.

[0027] Compared with the prior art, the present invention has the following beneficial effects:

[0028] The present invention avoids redistribution by using fillers by providing a gas-liquid distributor with a gas downcomer and a liquid downhole, thereby ensuring that the gas and liquid phases enter the pipe process uniformly. The gas-liquid distributor of the present invention has a simple structure and a good distribution effect. It is not necessary to provide a structured filler or a honeycomb filler. Only the gas-liquid distributor can ensure that the gas phase and liquid phase feed enter the pipe process with uniform flow. BRIEF DESCRIPTION OF THE DRAWINGS

[0029] Figure 1 A schematic diagram of the main structure of the gas-liquid distributor and the left feed nozzle, the right feed nozzle, the hydrogen feed pipe and the feed baffle as one of the purposes of the present invention;

[0030] Figure 2 A schematic diagram of the top view of the distribution plate, the downcomer, the left feed nozzle and the right feed nozzle in the gas-liquid distributor for one of the purposes of the present invention;

[0031] Figure 3 for Figure 2 A is a partial enlarged schematic diagram;

[0032] Figure 4 A schematic diagram of the main structure of the reactor for the second purpose of the present invention;

[0033] Figure 5 A schematic diagram of a partial top view of the structure of the heat exchange tubes, the center of the tube bridge and the second tube sheet in the reactor according to the second object of the present invention;

[0034] Figure 6 It is a schematic diagram of the main structure of a tubular fixed bed reactor in the prior art;

[0035] In the figure, 1-left feed nozzle; 2-right feed nozzle; 3-feed baffle; 4-downcomer; 5-distribution plate; 6-hydrogen feed pipe; 7-lower liquid hole; 8-heat exchange tube; 9-tube bridge center; 10-second tube sheet. DETAILED DESCRIPTION

[0036] The invention will be further described below in conjunction with the accompanying drawings.

[0037] The present invention relates to a gas-liquid distributor, which comprises a distribution plate 5, a lower liquid hole 7 provided on the distribution plate 5, and a downcomer 4 provided on the distribution plate 5 and extending upward. The downcomer 4 is vertically provided on the upper surface of the distribution plate 5. The downcomer 4 is connected from top to bottom (i.e., the lower port of the downcomer 4 is located on the distribution plate 5 and is a through hole, and the upper port and the lower port of the downcomer 4 are unobstructed to form a through pipe), serving as a gas phase channel. The lower liquid hole 7 is connected from top to bottom, serving as a liquid phase channel.

[0038] Further, such as Figures 1 to 3 As shown, the distribution plate 5 is in the shape of a flat plate, preferably a disc, and more preferably a circular disc. On the upper surface of the distribution plate 5, a plurality of downcomers 4 extending upward are vertically arranged. The downcomers 4 are multiple, preferably evenly distributed on the distribution plate 5. A lower liquid hole 7 is opened on the distribution plate 5 and between the downcomers 4. The lower liquid holes 7 are multiple, preferably evenly distributed on the distribution plate 5, and more preferably the lower liquid hole 7 is arranged between two adjacent downcomers 4.

[0039] In order to better achieve uniform entry of the gas-liquid two-phase into the pipe process, in one of the preferred embodiments of the present invention, the flow rate of the gas phase through the downcomer 4 is not more than 10m / s, or the pressure drop when passing through the downcomer 4 does not exceed 0.1kpa. Preferably, the flow rate of the gas phase through the downcomer 4 is 0.001-10m / s, more preferably 0.01-5m / s; or, the pressure drop when the gas passes through the downcomer 4 is preferably 0.01-0.08kpa. Further, the inner diameter of the downcomer 4 is preferably 15-50mm, more preferably 19-44mm. Furthermore, the height of the downcomer 4 is 10-50cm, preferably 20-30cm. The ratio of the tube center distance between two adjacent downcomers 4 to the inner diameter of the downcomer 4 is 1.2-1.5:1.

[0040] In order to better achieve uniform entry of gas and liquid into the pipe side, in one preferred embodiment of the present invention, the shape of the lower liquid hole 7 can be any one of circular, square, diamond, pentagonal, and hexagonal. Furthermore, the preferred shape of the lower liquid hole 7 is circular, and the preferred inner diameter of the lower liquid hole 7 is 1 to 6 mm, preferably 0.5 to 5 mm. The area of ​​the lower liquid hole 7 is related to the height of the downcomer 4 to ensure uniform entry of gas and liquid into the pipe side. It should be noted that Figure 3 The circular lower liquid hole 7 does not constitute a limitation to the present invention, as long as the area of ​​the lower liquid hole 7 can make the flow rate of the liquid phase meet the preset requirements. The flow rate of the liquid phase through the lower liquid hole 7 is 0.1 to 3 m / s, preferably 0.2 to 0.6 m / s. Furthermore, the ratio of the hole center distance between two adjacent lower liquid holes 7 to the inner diameter of the downcomer 4 is 1.2 to 1.5:1.

[0041] Figure 4 A reactor including the aforementioned gas-liquid distributor is shown, and the reactor includes, from bottom to top, a first tube sheet, a heat exchange tube bundle, a second tube sheet 10, the aforementioned gas-liquid distributor, a feed nozzle arranged on the side wall of the reactor, and a hydrogen feed pipe 6 arranged on the top of the reactor. Among them, the gas-liquid distributor is horizontally arranged in the reactor and is located at the upper part of the reactor. Specifically, the outer edge of the distribution plate 5 is connected to the inner wall of the reactor, and its outer edge and the inner wall of the reactor are tightly fitted. The gas phase enters the reactor through the hydrogen feed pipe 6. The feed nozzles include a left feed nozzle 1 and a right feed nozzle 2, both of which are arranged at the same height on the side of the reactor and are arranged opposite to each other. The liquid phase enters the reactor through the left feed nozzle 1 and the right feed nozzle 2. In the vertical direction, the height of the lower edge of the left feed nozzle 1 and the right feed nozzle 2 is not lower than the height of the distribution plate 5.

[0042] In the horizontal direction, a feed baffle 3 is vertically arranged between the feed nozzle and the downcomer 4, and the outer edge of the side of the feed baffle 3 is fixed on the side wall of the reactor, and its lower edge is higher than the distribution plate 5; the orthographic projection of the feed baffle 3 on the side wall of the reactor covers the feed nozzle. Taking the left side as an example, in the horizontal direction, a feed baffle 3 is vertically arranged between the left feed nozzle 1 and the downcomer 4 to prevent the liquid phase from entering the gas phase channel from the top surface of the downcomer 4 when entering the reactor from the left feed nozzle 1. The orthographic projection of the feed baffle 3 on the side wall of the reactor is sufficient to cover the orthographic projection of the left feed nozzle 1 on the side wall of the reactor. Preferably, the feed baffle 3 is arc-shaped, and the position and area of ​​the feed baffle 3 are sufficient to cover the nozzle opening of the left feed nozzle 1. In the horizontal direction, the left and right outer edges of the feed baffle 3 are connected to the inner wall of the reactor on the left and right sides of the left feed nozzle 1. In the vertical direction, the height of the upper edge of the feed baffle 3 is higher than the upper edge of the left feed nozzle 1 and higher than the upper edge of the downcomer 4; the height of the lower edge of the feed baffle 3 is lower than the lower edge of the left feed nozzle 1 and lower than the upper edge of the upcomer 4; the height of the lower edge of the feed baffle 3 is higher than the height of the distribution plate 5, so that the liquid phase entering from the left feed nozzle 1 falls on the distribution plate 5 and forms a liquid level of a certain height. More preferably, the vertical distance between the lower edge of the feed baffle 3 and the distribution plate 5 is 1 / 15 to 1 / 2 of the height of the downcomer 4, and the horizontal distance between the middle of the feed baffle 3 and the middle of the left feed nozzle 1 is 1 / 4 to 1 of the diameter of the left feed nozzle 1. It should be noted that the downcomer 4 here is the downcomer 4 closest to the left feed nozzle 1. Similarly, a similar feed baffle 3 is provided between the right feed nozzle 2 and the downcomer 4 closest thereto, and the specific descriptions are the same as those on the left side above.

[0043] In the actual MIBK production process, hydrogen enters the reactor through the hydrogen feed pipe 6. Acetone enters the reactor through the left feed nozzle 1 and the right feed nozzle 2. After acetone enters the reactor, it is deflected by the feed baffle 3, and the liquid phase falls on the distribution plate 5 to form a certain liquid level and a certain static pressure head. It should be noted that the liquid level formed by the liquid phase is located in the middle of the downcomer 4, and its liquid level is automatically controlled by a flow meter. Liquid phase acetone moves downward from the lower liquid hole 7. By reasonably setting the inner diameter of the downcomer 4, the flow rate of hydrogen moving downward can be controlled. Similarly, the flow rate of acetone moving downward can be controlled by setting the area of ​​the lower liquid hole 7, so that it matches the flow rate of the gas phase moving downward. Since the height of the downcomer 4 determines the maximum height of the acetone liquid layer on the distribution plate 5 and the static pressure head formed by the acetone liquid layer, the area of ​​the lower liquid hole 7 can be determined, so that the acetone flows downward evenly and matches the flow rate of the gas phase moving downward.

[0044] A disc-shaped tube sheet is provided under the distributor, preferably a disc-shaped tube sheet; its outer edge is connected to the inner wall of the reactor and is arranged horizontally, and the outer edge of the tube sheet and the inner wall of the reactor are closely fitted. Figure 4 As shown, the tube sheet includes a second tube sheet 10 adjacent to the lower edge of the gas-liquid distributor and a first tube sheet adjacent to the bottom of the reactor. The first tube sheet and the second tube sheet 10 are evenly provided with a plurality of through holes that can accommodate heat exchange tube bundles. The heat exchange tube bundles are composed of a plurality of vertically arranged heat exchange tubes 8. The arrangement of the through holes is the same as that of the heat exchange tubes 8, so as to allow a plurality of the heat exchange tubes 8 to pass through respectively. The distance between the distribution plate 5 and the second tube sheet 10 is 5 to 150 mm, preferably 50 to 100 mm. The inner diameter of the heat exchange tube 8 is 15 to 50 mm, preferably 19 to 44 mm. The ratio of the tube center distance between two adjacent heat exchange tubes 8 to the inner diameter of the heat exchange tube 8 is 1.2 to 1.5:1.

[0045] The plurality of heat exchange tubes 8 correspond vertically to the plurality of lower liquid holes 7, respectively, and the number of the heat exchange tubes 8 is the same as the number of the lower liquid holes 7. Preferably, the lower liquid holes 7 are coaxially arranged with the heat exchange tubes 8, the inner diameter of the lower liquid holes 7 is smaller than the inner diameter of the corresponding heat exchange tubes 8, and the center of the orthographic projection of the lower liquid holes 7 on the horizontal plane coincides with the center of the orthographic projection of the heat exchange tubes 8 on the horizontal plane. The liquid phase moving downward through the lower liquid holes 7 drips at a uniform speed into the heat exchange tubes 8 located below them.

[0046] The portion of the tube sheet connecting the adjacent heat exchange tubes 8 is the tube bridge. Figure 5 As shown, the heat exchange tubes 8 are arranged in an angular equilateral triangle. Taking three adjacent heat exchange tubes 8 as an example, the centers of the three heat exchange tubes 8 are connected together to form a triangular area, and the center of the triangular area is the tube bridge center 9. Preferably, the downcomer 4 and the tube bridge center 9 may correspond vertically; more preferably, each tube bridge center 9 corresponds to a downcomer 4. That is, the center of the orthographic projection of the downcomer 4 on the horizontal plane coincides with the tube bridge center 9. It should be noted that since it is easier for the gas phase to change direction, the number of the downcomers 4 does not necessarily have to be the same as the number of the heat exchange tubes 8, and the center of the orthographic projection of the downcomer 4 on the horizontal plane does not necessarily coincide with the tube bridge center 9. The fact that the center of the orthographic projection of the downcomer 4 on the horizontal plane coincides with the tube bridge center 9 is merely an exemplary description and does not constitute a new limitation on the present invention. Similarly, Figure 5 The arrangement of the plurality of heat exchange tubes 8 on the tube sheet is also only an exemplary description, which does not limit the arrangement of the heat exchange tubes 8, and other polygonal arrangements are also possible.

[0047] Hydrogen and acetone flow downward uniformly from the downcomer 4 and the lower liquid hole 7, respectively. Acetone enters the heat exchange tube 8, and hydrogen also enters the heat exchange tube 8. This is because although the center of the orthographic projection of the downcomer 4 on the horizontal plane coincides with the center of the pipe bridge 9, due to the obstruction of the pipe bridge, part of the hydrogen located above the pipe bridge cannot continue to move downward along the pipe bridge, so part of the hydrogen located above the pipe bridge also changes direction and enters the heat exchange tube 8 near the center of the pipe bridge 9 and continues to move downward. The hydrogen moves uniformly downward into the heat exchange tube 8 through the downcomer 4, and the acetone on the distribution plate 5 moves uniformly downward into the heat exchange tube 8 through the lower liquid hole 7, so as to ensure that the gas-liquid two-phases evenly enter each heat exchange tube 8. The gas-liquid two-phases react under the catalytic action of the catalyst in the heat exchange tube 8 to obtain MIBK.

[0048] The other parts of the reactor for synthesizing MIBK of the present invention can adopt the conventional design of the reactor for synthesizing MIBK in the prior art.

[0049] Example 1

[0050] In a preferred embodiment of the present invention, the Figures 1 to 5 The reactor with the gas-liquid distributor of the structure shown is used for MIBK synthesis reaction. The reactor has a diameter of 1900 mm, wherein the heat exchange tube bundle is provided with 1216 heat exchange tubes 8; the outer diameter of the heat exchange tube 8 is 38 mm, the inner diameter is 32 mm, and the height is 9 m; the tube center distance between two adjacent heat exchange tubes 8 is 47.5 mm. The lower end of the heat exchange tube is arranged in the first tube sheet, and the upper end is arranged in the second tube sheet 10. The distribution plate 5 of the gas-liquid distributor of the present invention is arranged 100 mm above the second tube sheet 10, and the distribution plate 5 is provided with 1216 downward gas pipes 4 extending upward, the outer diameter of the downward gas pipe 4 is 38 mm, the inner diameter is 32 mm, and the height is 30 cm, and the tube center distance between two adjacent downward gas pipes 4 is 47.5 mm. The multiple downward gas pipes 4 correspond vertically to the multiple tube bridge centers 9 one by one. The distribution plate 5 is provided with 1216 lower liquid holes 7, the inner diameter of the lower liquid hole 7 is 3mm, and the hole center distance between two adjacent lower liquid holes is 47.5mm. The multiple heat exchange tubes 8 correspond to the multiple lower liquid holes 7 one by one vertically and are coaxially arranged. The flow rate of hydrogen in the downcomer 4 is 0.015m / s, and the flow rate of acetone in the lower liquid hole 7 is 9m / s. The feed nozzle is arranged higher than the distribution plate 5, and includes a left feed nozzle 1 and a right feed nozzle 2, which are arranged at the same height on the side of the reactor and are arranged oppositely. The diameter of the feed nozzle is 80mm. The feed baffle 3 consists of two pieces, which are respectively arranged between the feed nozzle and the downcomer closest to the inner wall of the reactor; the distance between the middle of the feed baffle 3 and the feed nozzle is 80mm. The height of the feed baffle 3 is 30cm, and the distance between the lower edge of the feed baffle 3 and the distribution plate is 54mm.

[0051] Comparative Example 1

[0052] like Figure 6 The prior art tubular fixed bed reactor shown in the figure has a liquid distributor, structured filler and honeycomb arranged in sequence at the top of the reactor; a wedge-shaped support plate is arranged at the bottom of the reactor, and catalyst is loaded in the tube and on the support plate. The distributor of the reactor is complex in design.

[0053] Compared with the prior art of comparative example 1, the gas-liquid distributor structure of embodiment 1 of the present invention can make the gas-liquid two-phase enter the heat exchange tube more evenly. This is because the prior art distributor is provided with random packing and honeycomb packing below, and the packing will inevitably have wall effect and channel flow, and the smaller the packing height, the more obvious the wall effect. The gas-liquid distributor of embodiment 1 of the present invention ensures that the flow rate of the liquid phase dripping from each lower liquid hole 7 is consistent through the uniform liquid level and static pressure head distribution on the distribution plate 5, that is, the liquid phase flow rate entering each heat exchange tube 8 is consistent. At the same time, a downcomer 4 is provided to ensure that the gas phase can pass through the distribution plate 5 evenly and enter each heat exchange tube 8 evenly. In comparative example 1, the selectivity of the MIBK synthesis reaction is 94%, and the life of the catalyst is 7200h. In embodiment 1, since the gas-liquid two-phase enters the heat exchange tube 8 evenly, on the one hand, the selectivity of the reaction will be improved to 94.2%; on the other hand, the hot spot temperature is easier to control, and the reactor is not prone to temperature runaway. In addition, the uniform entry of the gas-liquid two-phase into the heat exchange tube 8 will also extend the life of the catalyst. In this embodiment, the life of the catalyst can reach 8000 hours.

Claims

1. A gas-liquid distributor, characterized in that: The utility model comprises a distribution plate, a lower liquid hole opened on the distribution plate, and an air downcomer arranged on the distribution plate and extending upward.

2. The gas-liquid distributor according to claim 1, characterized in that: The distribution plate is in the form of a flat plate, preferably a disc, more preferably a disk; and / or There are multiple downcomers, which are preferably evenly distributed on the distribution plate; and / or There are multiple downholes, which are preferably evenly distributed on the distribution plate, and more preferably, the downholes are arranged between two adjacent downcomers.

3. The gas-liquid distributor according to claim 1, characterized in that: The inner diameter of the downcomer is 15 to 50 mm, preferably 19 to 44 mm; and / or The height of the downcomer is 10 to 50 cm, preferably 20 to 30 cm.

4. The gas-liquid distributor according to claim 2, characterized in that: The shape of the lower liquid hole is any one of circular, square, rhombus, pentagon and hexagon; Preferably, the lower liquid hole is circular, and the inner diameter of the lower liquid hole is 1 to 6 mm, preferably 0.5 to 5 mm.

5. The gas-liquid distributor according to any one of claims 1 to 4, characterized in that: The ratio of the distance between the centers of two adjacent downcomers to the inner diameter of the downcomers is 1.2 to 1.5:1; and / or The ratio of the hole center distance between two adjacent down-liquid holes to the inner diameter of the downcomer is 1.2-1.5:

1.

6. A reactor for synthesizing MIBK, characterized in that: The reactor comprises, from bottom to top, a first tube sheet, a heat exchange tube bundle, a second tube sheet, a gas-liquid distributor according to any one of claims 1 to 5, a feed nozzle arranged on the side wall of the reactor, and a hydrogen feed pipe arranged on the top of the reactor; wherein the distribution plate of the gas-liquid distributor is horizontally arranged in the reactor.

7. The reactor according to claim 6, characterized in that: The distance between the distribution plate and the second tube plate is 5 to 150 mm, preferably 50 to 100 mm.

8. The reactor according to claim 6, characterized in that: The heat exchange tube bundle includes a plurality of vertically arranged heat exchange tubes, and the plurality of heat exchange tubes correspond vertically to the plurality of lower liquid holes one by one.

9. The reactor according to claim 6, characterized in that: In the horizontal direction, a feed baffle is vertically provided between the feed nozzle and the downcomer, the outer edge of the side of the feed baffle is fixed on the side wall of the reactor, and the lower edge thereof is higher than the distribution plate; the orthographic projection of the feed baffle on the side wall of the reactor covers the feed nozzle; Preferably, The vertical distance between the lower edge of the feed baffle and the distribution plate is 1 / 15 to 1 / 2 of the height of the downcomer; and / or The horizontal distance between the middle of the feed baffle and the feed nozzle is 1 / 4 to 1 of the diameter of the feed nozzle.

10. A method for synthesizing methyl isobutyl ketone, characterized in that: The reactor according to any one of claims 6 to 9 is used; preferably, acetone enters the reactor from the feed nozzle, and hydrogen enters the reactor from the hydrogen feed pipe; acetone and hydrogen enter the heat exchange tube bundle from the lower liquid hole and the downcomer, respectively, to react to obtain a methyl isobutyl ketone product.

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