Isononyl alcohol hydroformylation reactor

Abstract

The present invention provides an isononyl alcohol hydroformylation reactor, and relates to the technical field of isononyl alcohol hydroformylation reactors, the isononyl alcohol hydroformylation reactor comprises: a housing, the lower part of the housing is provided with a reactant inlet, and the side wall of the upper part of the housing is provided with a reactant outlet; the distribution device is arranged in the shell and located above the reactant inlet, the distribution device and the reactant inlet are arranged in a spaced mode, and the distribution device is used for evenly distributing the gas-liquid reaction medium; the heat extraction distribution structure is arranged in the shell and located above the distribution device, the heat extraction distribution structure and the distribution device are arranged in a spaced mode, and the heat extraction distribution structure comprises an inner tube box, an outer tube box, a plurality of heat exchange tubes and at least one distribution plate; the problems that in the prior art, a gas-liquid up-flow type bubbling bed reactor is not internally provided with internal components, gas distribution and heat extraction cannot be achieved, and the conversion rate of reaction is low are solved.

Description

Technical Field

[0001] The invention belongs to the technical field of isononanol hydroformylation reactors, and more specifically, relates to an isononanol hydroformylation reactor. Background Art

[0002] In recent years, with the rapid development of the plastics industry and the further improvement of people's environmental protection requirements, the new generation of plasticizer diisononyl phthalate (DINP) has been widely used in toys and wires and cables. As a raw material for the production of DINP, the demand for isononyl alcohol (INA) has also grown rapidly. Isononyl alcohol is generally produced by hydroformylation, that is, it is produced by the hydroformylation reaction of C8 olefins and synthesis gas under high temperature, high pressure and catalyst. At present, the industrialized hydroformylation technology is homogeneous catalytic hydroformylation technology.

[0003] The hydroformylation reaction is a highly exothermic reaction, and because the reaction temperature is strictly controlled, the reaction heat needs to be removed in time. Therefore, it is crucial to design a heat extraction reaction system that can both extract heat and ensure that the reaction temperature is as uniform as possible in space. The existing gas-liquid upflow bubbling bed reactor has no internal components, and cannot distribute gas and extract heat, resulting in a low reaction conversion rate. Summary of the invention

[0004] The purpose of the present invention is to provide an isononanol hydroformylation reactor in view of the deficiencies in the prior art, so as to solve the problem that the gas-liquid upflow bubbling bed reactor in the prior art has no internal components, cannot distribute gas and extract heat, and causes a low reaction conversion rate.

[0005] In order to achieve the above object, the present invention provides an isononanol hydroformylation reactor, comprising:

[0006] A shell, wherein a reactant inlet is disposed at the lower portion of the shell, and a reactant outlet is disposed on the upper side wall of the shell;

[0007] A distribution device, arranged inside the housing and above the reactant inlet, and spaced apart from the reactant inlet, for uniformly distributing the gas-liquid reaction medium;

[0008] A heat distribution structure is arranged inside the shell and above the distribution device, and is spaced apart from the distribution device. The heat distribution structure includes an inner tube box, an outer tube box, a plurality of heat exchange tubes and at least one distribution plate. The inner tube box is arranged inside the outer tube box, a heat medium inlet cavity is formed inside the inner tube box, and a heat medium outflow cavity is formed between the inner tube box and the outer tube box. The heat exchange tube is a U-shaped tube, and the two ends of the heat exchange tube are respectively a heat medium inlet and a heat medium outlet, and the heat medium inlet and the heat medium outlet are respectively connected to the heat medium inlet cavity and the heat medium outflow cavity; a plurality of positioning through holes and a distribution structure are arranged on the distribution plate, and each of the heat exchange tubes passes through two of the positioning through holes.

[0009] Optionally, the inner wall of the upper end of the shell forms the box wall of the outer tube box, and the upper end of the shell is provided with a bottom plate and a cover plate connected to the inner wall of the shell in sequence from bottom to top, the inner tube box includes an inner cylinder, the inner cylinder is coaxially arranged inside the outer tube box and is respectively connected to the bottom plate and the cover plate, the heat medium inlet and the heat medium outlet are connected to the bottom plate, and the cover plate is provided with a heat medium total inlet and a heat medium total outlet respectively connected to the heat medium inlet cavity and the heat medium outlet cavity.

[0010] Optionally, the top projection of the axis of each of the heat exchange tubes is straight, and the top projections of all the heat exchange tubes are divided into a plurality of regions of the same shape, and the plurality of regions have only one endpoint located at the center of a virtual circle, and the virtual circle is concentric with the cross section of the isononanol hydroformylation reactor, and the top projection of the heat exchange tube in each region can overlap with the top projection of the heat exchange tube in an adjacent region when rotated around the center of the circle by a set angle.

[0011] Optionally, the area is a sector-shaped area, and the central angle of each sector-shaped area is 6°-60°.

[0012] Optionally, at least two distribution plates are provided, and at least two distribution plates are arranged vertically at intervals, and the spacing between adjacent distribution plates is 1000-5000 mm.

[0013] Optionally, the distribution structure comprises a plurality of circular first distribution through holes, and the plurality of first distribution through holes are opened on the distribution plate.

[0014] Optionally, the distribution structure comprises a plurality of second distribution through holes in a long waist shape, and the plurality of second distribution through holes are opened on the distribution plate.

[0015] Optionally, the distribution plate is a wedge-shaped bar welded screen plate, and the strip seams of the wedge-shaped bar welded screen plate form the distribution structure.

[0016] Optionally, the distribution device comprises a distribution plate, on which a distribution structure is arranged, and the distribution structure has the same structure as the distribution structure.

[0017] Optionally, the distance between the distribution device and the reactant inlet is 200mm-5000mm.

[0018] The invention provides an isononanol hydroformylation reactor, which has the beneficial effects that: the isononanol hydroformylation reactor is provided with a distribution device and a heat extraction distribution structure in sequence from bottom to top in a shell, and the gas-liquid reaction medium is evenly distributed by the distribution device, thereby improving the uniformity of the distribution of the gas-liquid reaction medium in the shell, and the heat extraction distribution structure comprises an inner tube box and an outer tube box, and the heat extraction medium can enter through the heat extraction medium inlet cavity in the inner tube box and flow out through the heat extraction medium outflow cavity between the outer tube box and the inner tube box, thereby realizing the inner inlet and the outer outlet of the heat extraction medium, and the heat extraction medium inlets of a plurality of heat exchange tubes are all connected to the heat extraction medium inlet cavity, and the heat extraction medium outlets thereof are all connected to the heat extraction medium outflow cavity, so that when the heat extraction medium flows in the heat exchange tube, the heat extraction medium with a lower temperature that has just entered can first extract heat from the inner center of the reactor, and the heat extraction amount is relatively large, and the heat extraction medium with a higher temperature that has completed partial heat exchange can then extract heat from the inner outer ring of the reactor, thereby obtaining a larger amount of heat. The heat is small; and, at least one distribution plate is provided with a plurality of positioning through holes and distribution structures, the positioning through holes can position the heat exchange tube, form support for the heat exchange tube, ensure the support strength of the heat exchange tube, the distribution structure can distribute the gas-liquid reaction medium, and can also play a role of redistribution after the distribution device has been evenly distributed once, further improving the uniformity of the distribution of the gas-liquid reaction medium in the reactor, achieving stable and uniform distribution of gas and liquid in the reactor, improving the reaction conversion rate, and reducing the occurrence of reverse mixing phenomenon; the gas-liquid reaction residence time of the isononanol hydroformylation reactor is relatively long, and the setting of the distribution plate reduces the reverse mixing phenomenon, and the reactor radially presents the characteristics of hot in the middle and cold on the periphery, so through the radial arrangement of the heat exchange tubes in the heat extraction distribution structure for the isononanol hydroformylation reactor, the uneven temperature distribution in the radial direction of the reactor can be reduced as much as possible, which is conducive to the reaction and can improve the conversion rate. In addition, the present invention can also be applied to other gas-liquid exothermic reaction systems for simultaneously distributing gas and extracting heat.

[0019] Other features and advantages of the present invention will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] The above and other objects, features and advantages of the present invention will become more apparent through a more detailed description of exemplary embodiments of the present invention in conjunction with the accompanying drawings, wherein like reference numerals generally represent like components throughout the exemplary embodiments of the present invention.

[0021] Figure 1 A schematic structural diagram of an isononanol hydroformylation reactor according to an embodiment of the present invention is shown.

[0022] Figure 2 A schematic diagram of a top view projection of heat exchange tubes in a sector-shaped area of ​​a heat extraction distribution structure of an isononanol hydroformylation reactor according to an embodiment of the present invention is shown.

[0023] Figure 3 A schematic diagram of a top projection of heat exchange tubes in a sector-shaped area of ​​a heat extraction distribution structure of an isononanol hydroformylation reactor according to another embodiment of the present invention is shown.

[0024] Figure 4 A schematic structural diagram of a distribution plate of a heat extraction distribution structure of an isononanol hydroformylation reactor according to an embodiment of the present invention is shown.

[0025] Figure 5 A schematic structural diagram of a distribution plate of a heat extraction distribution structure of an isononanol hydroformylation reactor according to other embodiments of the present invention is shown.

[0026] Figure 6 A schematic structural diagram of a distribution plate of a heat extraction distribution structure of an isononanol hydroformylation reactor according to other embodiments of the present invention is shown.

[0027] Figure 7 A schematic diagram of positioning through holes on a distribution plate of a heat extraction distribution structure of an isononanol hydroformylation reactor according to an embodiment of the present invention is shown.

[0028] Description of reference numerals:

[0029] 1. Shell; 2. Reactant inlet; 3. Reactant outlet; 4. Distribution device; 5. Heat distribution structure; 501. Inner tube box; 502. Outer tube box; 503. Heat exchange tube; 504. Heat medium inlet; 505. Heat medium outlet; 506. Distribution plate; 507. Positioning through hole; 508. Bottom plate; 509. Cover plate; 510. Heat medium total inlet; 511. Heat medium total outlet; 512. Fan-shaped area; 513. First distribution through hole; 514. Second distribution through hole; 515. Wedge-shaped bar welded screen plate. DETAILED DESCRIPTION

[0030] The preferred embodiments of the present invention will be described in more detail below. Although the preferred embodiments of the present invention are described below, it should be understood that the present invention can be implemented in various forms and should not be limited by the embodiments set forth herein. On the contrary, these embodiments are provided to make the present invention more thorough and complete, and to fully convey the scope of the present invention to those skilled in the art.

[0031] like Figure 1 As shown, the present invention provides an isononanol hydroformylation reactor, comprising:

[0032] A shell 1, a reactant inlet 2 is provided at the lower portion of the shell 1, and a reactant outlet 3 is provided on the upper side wall of the shell 1;

[0033] The distribution device 4 is arranged inside the housing 1 and above the reactant inlet 2, and is spaced apart from the reactant inlet 2, and is used to evenly distribute the gas-liquid reaction medium;

[0034] The heat distribution structure 5 is arranged inside the shell 1 and above the distribution device 4, and is spaced apart from the distribution device 4. The heat distribution structure 5 includes an inner tube box 501, an outer tube box 502, a plurality of heat exchange tubes 503 and at least one distribution plate 506. The inner tube box 501 is arranged inside the outer tube box 502. A heat medium inlet cavity is formed inside the inner tube box 501, and a heat medium outflow cavity is formed between the inner tube box 501 and the outer tube box 502. The heat exchange tube 503 is a U-shaped tube. The two ends of the heat exchange tube 503 are a heat medium inlet 504 and a heat medium outlet 505, respectively. The heat medium inlet 504 and the heat medium outlet 505 are connected to the heat medium inlet cavity and the heat medium outflow cavity, respectively. The distribution plate 506 is provided with a plurality of positioning through holes 507 and a distribution structure, and each heat exchange tube 503 passes through two positioning through holes 507.

[0035] Specifically, in order to solve the problem that there is no internal component in the gas-liquid upflow bubbling bed reactor in the prior art, it is impossible to distribute gas and take heat, resulting in a low reaction conversion rate; the isononanol hydroformylation reactor provided by the present invention is provided with a distribution device 4 and a heat distribution structure 5 in sequence from bottom to top inside the shell 1, and the gas-liquid reaction medium is evenly distributed by the distribution device 4, thereby improving the uniformity of the distribution of the gas-liquid reaction medium in the shell 1, and the heat distribution structure 5 has an inner pipe box 501 and an outer pipe box 502, and the heat medium can be taken through The heat medium in the inner tube box 501 enters the heat medium inlet cavity and flows out through the heat medium outflow cavity between the outer tube box 502 and the inner tube box 501, so that the heat medium can enter and exit from the inner tube box 502. The heat medium inlets 504 of the multiple heat exchange tubes 503 are all connected to the heat medium inlet cavity, and the heat medium outlets 505 are all connected to the heat medium outflow cavity. In this way, when the heat medium flows in the heat exchange tubes 503, the heat medium with a lower temperature that has just entered can first take heat from the inner center of the reactor, and the heat taken is larger, while the temperature after completing the partial heat exchange is higher. The heat medium then takes heat from the inner outer ring of the reactor, and the amount of heat taken is small; and, since at least one distribution plate 506 is provided with a plurality of positioning through holes 507 and a distribution structure, the positioning through holes 507 can position the heat exchange tube 503, form support for the heat exchange tube 503, and ensure the support strength of the heat exchange tube 503, and the distribution structure can distribute the gas-liquid reaction medium, and can also play a role of redistribution after the distribution device 4 has performed a uniform distribution, further improving the uniformity of the distribution of the gas-liquid reaction medium in the reactor, achieving a stable and uniform distribution of gas and liquid in the reactor, improving the reaction conversion rate, and reducing the occurrence of back mixing; the gas-liquid reaction residence time of the isononanol hydroformylation reactor is relatively long, and the setting of the distribution plate 506 reduces the back mixing phenomenon. In the radial direction, the reactor presents the characteristics of being hot in the middle and cold on the periphery. Therefore, through the radial arrangement of the heat distribution structure 5U-shaped heat exchange tube 503 used for the isononanol hydroformylation reactor, the uneven temperature distribution in the radial direction of the reactor can be minimized as much as possible, which is conducive to the reaction and can improve the conversion rate.

[0036] Furthermore, the U-shaped heat exchange tube 503 in the present invention is simple to manufacture and low in cost, and the multiple heat exchange tubes 503 can include a number of spare heat exchange tubes 503, both ends of the spare heat exchange tube 503 are blocked by pipe plugs. When some of the heat exchange tubes 503 are damaged, the inner tube box 501 and the outer tube box 502 can be opened to block both ends of the damaged heat exchange tube 503, and then the pipe plugs of the same number of spare heat exchange tubes 503 can be opened, thereby realizing very convenient maintenance.

[0037] Optionally, the inner wall of the upper end of the shell 1 forms the box wall of the outer tube box 502, and the upper end of the shell 1 is provided with a bottom plate 508 and a cover plate 509 connected to the inner wall of the shell 1 in sequence from bottom to top. The inner tube box 501 includes an inner cylinder, which is coaxially arranged inside the outer tube box 502 and is respectively connected to the bottom plate 508 and the cover plate 509. The heat medium inlet 504 and the heat medium outlet 505 are connected to the bottom plate 508, and the cover plate 509 is provided with a heat medium total inlet 510 and a heat medium total outlet 511 which are respectively connected to the heat medium inlet cavity and the heat medium outlet cavity.

[0038] Specifically, the outer tube box 502 can directly use part of the inner wall of the reactor as its outer cylinder, and the inner cylinder is coaxially arranged inside the outer cylinder. The bottom plate 508 and the cover plate 509 block the heat medium inlet chamber and the heat medium outlet chamber, and a plurality of connecting holes are provided on the bottom plate 508, half of the plurality of connecting holes are connected to the heat medium inlet chamber, and the other half are connected to the heat medium outlet chamber; the heat medium first enters the heat medium inlet chamber through the heat medium main inlet 510, and then is distributed into a plurality of heat exchange tubes 503, and then flows into the heat medium outlet chamber, and uniformly flows out through the heat medium main outlet 511.

[0039] Optionally, the top projection of the axis of each heat exchange tube 503 is a straight line, and the top projections of all the heat exchange tubes 503 are divided into multiple regions of the same shape, and the multiple regions have only one endpoint located at the center of a virtual circle, and the virtual circle is concentric with the cross-section of the isononanol hydroformylation reactor. The top projection of the heat exchange tube 503 in each region can overlap with the top projection of the heat exchange tube 503 in the adjacent region when it is rotated around the center of the circle by a set angle.

[0040] Specifically, the plurality of regions are rotationally symmetrical figures relative to the center of the circle.

[0041] In this embodiment, the top projection of the axis of each heat exchange tube 503 is a straight line, and the top projections of all the heat exchange tubes 503 are divided into a plurality of sector-shaped areas 512. The plurality of sector-shaped areas 512 are concentric and can form a circle. The top projection of the heat exchange tube 503 in each sector-shaped area 512 can coincide with the top projection of the heat exchange tube 503 in the adjacent sector-shaped area 512 when the heat exchange tube 503 is rotated around the center of the circle at the same angle as the central angle of the circle.

[0042] Specifically, the heat exchange tubes 503 are arranged vertically inside the reactor, and their top projections are straight. The top projections of the multiple heat exchange tubes 503 are divided into multiple fan-shaped areas 512. A number of heat exchange tubes 503 are distributed in each fan-shaped area 512. When a fan-shaped area 512 rotates around the center of the circle at an angle equal to the central angle of the fan-shaped area 512, the top projection of the heat exchange tubes 503 in the fan-shaped area 512 coincides with the top projection of the heat exchange tubes 503 in the adjacent fan-shaped area 512. Then, the multiple fan-shaped areas 512 form a circular array arrangement. Such an arrangement makes the distribution of the multiple heat exchange tubes 503 in the circumferential direction more uniform, which is conducive to uniform heat extraction.

[0043] Optionally, the area is a sector-shaped area 512, and the central angle of each sector-shaped area 512 is 6°-60°.

[0044] Specifically, in theory, any integer equally divided angle of 360° can be used as the center angle of the above-mentioned fan-shaped area 512. However, due to the difficulty of engineering manufacturing and other reasons, 6°-60° is selected as the center angle of the above-mentioned fan-shaped area 512. A too small center angle will cause the heat exchange tubes 503 in the fan-shaped area 512 to be distributed too densely, which is not conducive to construction. A too large center angle will cause the heat exchange tubes 503 to have poor distribution uniformity, which is not conducive to uniform heat exchange.

[0045] In one embodiment, Figure 2 As shown, the central angle of each sector-shaped area 512 is 6°, and the complete top-view projection circle is divided into 60 sector-shaped areas 512 .

[0046] In another embodiment, Figure 3 As shown, the central angle of each sector-shaped area 512 is 60°, and the complete top-view projection circle is divided into 6 sector-shaped areas 512 .

[0047] Optionally, the heat exchange medium flowing in the heat exchange tube 503 is deoxygenated water.

[0048] Specifically, the heat exchange medium is deoxygenated water, which can generate steam latent heat to extract heat, or directly generate sensible heat to extract heat.

[0049] Optionally, at least two distribution plates 506 are provided, and the at least two distribution plates 506 are arranged at intervals in the vertical direction, and the interval between adjacent distribution plates 506 is 1000-5000 mm.

[0050] Specifically, according to the different flow rates of the gas-liquid reaction medium on the reaction side, the spacing of the distribution plates 506 is set to 1000mm-5000mm. Too small a spacing will lead to excessive pressure drop of the gas-liquid reaction medium flow, while too large a spacing will cause the heat distribution structure 5 to vibrate.

[0051] Optionally, the aperture of the positioning through hole 507 matches the outer diameter of the heat exchange tube 503 .

[0052] Specifically, the heat exchange tube 503 is inserted into the positioning through hole 507 , and the positioning through hole 507 supports and positions the heat exchange tube 503 , thereby improving the overall strength and stability of the heat extraction distribution structure 5 .

[0053] In this embodiment, the distribution structure includes a plurality of circular first distribution through holes 513 , and the plurality of first distribution through holes 513 are opened on the distribution plate 506 .

[0054] Specifically, Figure 4 As shown, the distribution structure is a plurality of first distribution through holes 513, which are circular holes and are staggeredly distributed on the distribution plate 506. The opening rate of the first distribution holes is 5%-20%. The first distribution holes are for gas-liquid reaction medium to pass through, and can evenly distribute the gas-liquid reaction medium in the reactor.

[0055] In another embodiment, the distribution structure includes a plurality of second distribution through holes 514 in a long waist shape, and the plurality of second distribution through holes 514 are opened on the distribution plate 506 .

[0056] Specifically, Figure 5 As shown, the distribution structure is a plurality of second distribution through holes 514, which are long waist holes and are distributed in a rectangular array on the distribution plate 506. The opening rate of the second distribution holes is 5%-20%, and the second distribution holes are for gas-liquid reaction medium to pass through, so as to evenly distribute the gas-liquid reaction medium in the reactor.

[0057] In another embodiment, the distribution plate 506 is a wedge-shaped bar welded mesh plate 515, and the strips of the wedge-shaped bar welded mesh plate 515 form a distribution structure.

[0058] Specifically, Figure 6 As shown, a wedge-shaped bar welded screen plate 515 is used as the distribution plate 506, and the strip seams of the wedge-shaped bar welded screen plate 515 form a distribution structure, which has a mixing effect of compressing and expanding the lower incoming flow.

[0059] Further, according to the distribution requirements of the gas-liquid reaction medium, 1-3 layers of distribution plates 506 may be provided, including but not limited to the following solutions: using a single layer such as Figure 4 The distribution plate 506 with the first distribution through hole 513 shown in FIG. Figure 5 The distribution plate 506 with the second distribution through hole 514 shown in FIG. Figure 6 The wedge-shaped bar welded screen plate 515 shown is used as the distribution plate 506, any two of the above three distribution plates 506 are used in combination, and the above three distribution plates 506 are used in combination.

[0060] Optionally, the distribution device 4 comprises a distribution plate, on which a distribution structure is arranged, the distribution structure is the same as the distribution structure, and the distribution structure and the distribution structure are arranged alternately.

[0061] Specifically, the outer periphery of the distribution plate is connected to the inner wall of the shell 1, and the distribution structure on the distribution plate is the same as the distribution structure on the distribution plate 506, and can have three different structural forms, namely, a structure of multiple circular first distribution through holes, a structure of multiple long waist-shaped second distribution through holes, and a wedge-shaped bar welded screen plate 515 as a distribution plate to form a distribution structure. No matter which structural form is adopted, in order to improve the distribution and redistribution effects, the distribution structure and the distribution structure are arranged alternately, that is, the distribution structure and the distribution structure do not correspond to each other in the vertical direction.

[0062] Optionally, the distance between the distribution device 4 and the reactant inlet 2 is 200 mm-5000 mm.

[0063] Specifically, based on the physical properties of the gas and liquid, such as viscosity, flow rate, and surface tension, it was found through cold mold tests that a distance between the distribution device 4 and the reactant inlet 2 of 200mm-1500mm can meet the gas distribution requirements; for most gas-liquid reaction medium systems, the distance between the distribution device 4 and the reactant inlet 2 is optimally between 300mm-800mm. Too large a distance wastes the internal space of the reactor, and too small a distance cannot fully disperse the gas-liquid reaction medium flow at the reactant inlet 2.

[0064] In summary, when the isononanol hydroformylation reactor provided by the present invention is used, the gas-liquid two-phase reaction medium to be reacted enters the reactor from the reactant inlet 2 at the bottom of the reactor, and the gas-liquid reaction medium passes through the distribution device 4 upward to be evenly dispersed; then the gas-liquid reaction medium passes through the heat extraction distribution structure 5, and extracts heat through multiple U-shaped tube-type heat exchange tubes 503, so that the heat extraction medium with a lower temperature that has just entered can first extract heat from the inner center of the reactor, and the amount of heat extracted is large, and the heat extraction medium with a higher temperature after completing partial heat exchange can then extract heat from the inner outer ring of the reactor, and the amount of heat extracted is small; thereby, the uneven temperature distribution in the radial direction of the reactor can be minimized as much as possible, which is beneficial to the reaction and can improve the conversion rate; the gas-liquid reaction medium that has completely reacted leaves the reactor from the reactant outlet 3 located on the upper side wall of the reactor.

[0065] The embodiments of the present invention have been described above, and the above description is exemplary, not exhaustive, and is not limited to the disclosed embodiments. Many modifications and changes will be apparent to those skilled in the art without departing from the scope and spirit of the described embodiments.

Claims

1. An isononanol hydroformylation reactor, characterized in that: include: A shell, wherein a reactant inlet is disposed at the lower portion of the shell, and a reactant outlet is disposed on the upper side wall of the shell; A distribution device, arranged inside the housing and above the reactant inlet, and spaced apart from the reactant inlet, for uniformly distributing the gas-liquid reaction medium; A heat distribution structure is arranged inside the shell and above the distribution device, and is spaced apart from the distribution device. The heat distribution structure includes an inner tube box, an outer tube box, a plurality of heat exchange tubes and at least one distribution plate. The inner tube box is arranged inside the outer tube box, a heat medium inlet cavity is formed inside the inner tube box, and a heat medium outflow cavity is formed between the inner tube box and the outer tube box. The heat exchange tube is a U-shaped tube, and the two ends of the heat exchange tube are respectively a heat medium inlet and a heat medium outlet, and the heat medium inlet and the heat medium outlet are respectively connected to the heat medium inlet cavity and the heat medium outflow cavity; a plurality of positioning through holes and a distribution structure are arranged on the distribution plate, and each of the heat exchange tubes passes through two of the positioning through holes.

2. The isononanol hydroformylation reactor according to claim 1, characterized in that: The inner wall of the upper end of the shell forms the box wall of the outer tube box. The upper end of the shell is provided with a bottom plate and a cover plate connected to the inner wall of the shell in sequence from bottom to top. The inner tube box includes an inner cylinder, which is coaxially arranged inside the outer tube box and connected to the bottom plate and the cover plate respectively. The heat medium inlet and the heat medium outlet are connected to the bottom plate. The cover plate is provided with a heat medium total inlet and a heat medium total outlet respectively connected to the heat medium inlet cavity and the heat medium outlet cavity.

3. The isononanol hydroformylation reactor according to claim 1, characterized in that: The top projection of the axis of each heat exchange tube is a straight line, and the top projections of all the heat exchange tubes are divided into a plurality of regions of the same shape, and the plurality of regions have only one endpoint located at the center of a virtual circle, and the virtual circle is concentric with the cross section of the isononanol hydroformylation reactor, and the top projection of the heat exchange tube in each region can overlap with the top projection of the heat exchange tube in an adjacent region when rotating around the center of the circle by a set angle.

4. The isononanol hydroformylation reactor according to claim 3, characterized in that: The area is a sector-shaped area, and the central angle of each sector-shaped area is 6°-60°.

5. The isononanol hydroformylation reactor according to claim 1, characterized in that: At least two distribution plates are provided, and at least two distribution plates are arranged at intervals in the vertical direction, and the spacing between adjacent distribution plates is 1000-5000 mm.

6. The isononanol hydroformylation reactor according to claim 1, characterized in that: The distribution structure comprises a plurality of circular first distribution through holes, and the plurality of first distribution through holes are opened on the distribution plate.

7. The isononanol hydroformylation reactor according to claim 1, characterized in that: The distribution structure comprises a plurality of second distribution through holes in a long waist shape, and the plurality of second distribution through holes are arranged on the distribution plate.

8. The isononanol hydroformylation reactor according to claim 1, characterized in that: The distribution plate is a wedge-shaped bar welded screen plate, and the strip seams of the wedge-shaped bar welded screen plate form the distribution structure.

9. The isononanol hydroformylation reactor according to any one of claims 6 to 8, characterized in that: The distribution device comprises a distribution plate, on which a distribution structure is arranged, and the distribution structure has the same structure as the distribution structure.

10. The isononanol hydroformylation reactor according to claim 1, characterized in that: The distance between the distribution device and the reactant inlet is 200mm-5000mm.

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