Heat exchange distribution structure for isononyl alcohol hydroformylation reactor

Abstract

The invention provides a heat exchange distribution structure for an isononyl alcohol hydroformylation reactor, and relates to the technical field of isononyl alcohol hydroformylation reactors, the heat exchange distribution structure comprises: a plurality of heat exchange tubes, the axes of the plurality of heat exchange tubes are parallel to each other, and the plurality of heat exchange tubes are annularly distributed along a plurality of concentric virtual circumferences; the distribution plate is provided with a plurality of positioning through holes and a distribution structure, and the heat exchange tubes are arranged in the through holes in a penetrating mode respectively; the isononyl alcohol hydroformylation reactor solves the problems that gaseous reactants in the isononyl alcohol hydroformylation reactor in the prior art are not uniformly distributed, liquid reactants are easy to form vortexes to cause a backmixing phenomenon, the local concentration stability of the gaseous reactants at different axial positions is poor, and the reaction conversion rate is low.

Description

Technical Field

[0001] The invention belongs to the technical field of isononanol hydroformylation reactors, and more specifically, relates to a heat exchange distribution structure for isononanol hydroformylation reactors. Background Art

[0002] Olefins react with synthesis gas (CO+H2) under the action of transition metal cobalt or rhodium to generate aldehyde compounds with one more carbon atom than olefins. This reaction process is the hydroformylation reaction of olefins, which is the most successful and widely used homogeneous catalytic reaction process in industrial application. The generated aldehydes can be further processed into compounds such as alcohols, esters, ethers, carboxylic acids and amines.

[0003] Isononyl alcohol includes high-branched isononyl alcohol and low-branched isononyl alcohol. Low-branched isononyl alcohol is used to produce plasticizers such as diisononyl phthalate (DINP), diisononyl adipate (DINA) and trihydroxymethyl triisononyl ester (TINTM). These plasticizers have excellent performance and are non-toxic. They are mainly used in polyvinyl chloride, vinyl chloride copolymers, cellulose acetate, ethyl cellulose and synthetic rubber to replace dioctyl phthalate (DOP) which has been banned or restricted in Europe and the United States and is considered to be potentially carcinogenic. High-branched isononyl alcohol (3,5,5-trimethyl-1-hexanol) is a cosmetic additive. Isononyl alcohol uses C8 olefins and synthesis gas as reactants to generate C9 alcohols and C9 aldehydes under a certain temperature, pressure, and homogeneous catalysis of transition metal (Co or Ru) complexes. Side reactions include direct hydrogenation of reactant olefins and aldol condensation to generate heavy substances.

[0004] The reactor used in the hydroformylation reaction is usually an upflow bubbling reactor. This type of reactor is suitable for slow reactions and reactions with high heat release, but the liquid phase has severe axial backmixing, which can be considered as full mixing, so it is difficult for a single reactor to achieve a high conversion rate, so multiple reactors are usually connected in series. It is very complicated for the gas-liquid reaction system of the isononanol hydroformylation reactor to reach a steady state, which is jointly determined by the reaction rate, solubility and mass transfer rate. The gaseous reactants in the existing isononanol hydroformylation reactor are unevenly distributed, which easily causes the liquid reactants to form vortices and then backmixing, and the local concentration stability of the gaseous reactants at different axial positions is poor, and the reaction conversion rate is low. Summary of the invention

[0005] The purpose of the present invention is to provide a heat exchange distribution structure for an isononanol hydroformylation reactor in view of the deficiencies in the prior art, so as to solve the problems that the gaseous reactants in the isononanol hydroformylation reactor in the prior art are unevenly distributed, which easily causes the liquid reactants to form vortices and then back-mixing, and the local concentration stability of the gaseous reactants at different axial positions is poor, and the reaction conversion rate is low.

[0006] In order to achieve the above object, the present invention provides a heat exchange distribution structure for an isononanol hydroformylation reactor, comprising:

[0007] A plurality of heat exchange tubes, wherein the axes of the plurality of heat exchange tubes are parallel to each other, and the plurality of heat exchange tubes are distributed in a ring shape along a plurality of concentric virtual circles;

[0008] At least one distribution plate is provided with a plurality of positioning through holes and a distribution structure, and a plurality of heat exchange tubes are respectively passed through the plurality of positioning through holes.

[0009] Optionally, the heat exchange tube includes an inner tube and an outer tube, and the two ends of the outer tube are respectively provided with a first sealing plate and a second sealing plate, one end of the inner tube is inserted into the outer tube and forms a first gap with the first sealing plate, and the other end of the inner tube passes through the second sealing plate and extends outward to form an extension portion, the outer end of the extension portion forms a heat exchange medium inlet, and a heat exchange medium outlet is opened on the outer wall of the outer tube.

[0010] Optionally, it also includes a first fixed baffle and a second fixed baffle, the first fixed baffle is connected to the extension part, the second fixed baffle is connected to the outer tube, a heat exchange medium inlet space is formed on the side of the first fixed baffle away from the second fixed baffle, a heat exchange medium outflow space is formed between the first fixed baffle and the second fixed baffle, and the heat exchange medium inlet and the heat exchange medium outlet are respectively located in the heat exchange medium inlet space and the heat exchange medium outflow space.

[0011] Optionally, a first tubular structure is provided on a side of the first fixed baffle away from the second fixed baffle, one end of the first tubular structure is connected to the first fixed baffle and forms a heat exchange medium inlet cavity therein, a total heat exchange medium inlet is provided at the other end of the first tubular structure, a second tubular structure is provided between the first fixed baffle and the second fixed baffle, two ends of the second tubular structure are respectively connected to the first fixed baffle and the second fixed baffle and form a heat exchange medium outflow cavity therein, and a total heat exchange medium outlet is provided on the outer wall of the second tubular structure.

[0012] Optionally, the heat exchange medium flowing in the heat exchange tube is deoxygenated water.

[0013] Optionally, at least two distribution plates are provided, and at least two distribution plates are arranged at intervals along the axis of the heat exchange tube, and the spacing between adjacent distribution plates is 500-5000 mm.

[0014] Optionally, the aperture of the positioning through hole is 2-10 mm larger than the outer diameter of the heat exchange tube.

[0015] Optionally, the distribution structure includes a plurality of distribution through holes, and the plurality of distribution through holes are opened on the distribution plate.

[0016] Optionally, the distribution plate is a slit mesh plate, and the slits and / or mesh holes of the slit mesh plate form the distribution structure.

[0017] Optionally, the distribution structure includes a plurality of tubular distributors, a plurality of mounting holes are provided on the distribution plate, and the plurality of tubular distributors are respectively installed on the reaction medium flow side of the distribution plate through the plurality of mounting holes. The tubular distributor includes a tube body and a buffer plate, one end of the tube body is connected to the mounting hole, a plurality of flow holes are provided on the outer wall of the tube body, a plurality of connecting pins are arranged at intervals on the outer periphery of the buffer plate, and the buffer plate is connected to the tube body through the connecting pins.

[0018] The invention provides a heat exchange distribution structure for an isononanol hydroformylation reactor, and the heat exchange distribution structure for the isononanol hydroformylation reactor has the following beneficial effects: the heat exchange distribution structure for the isononanol hydroformylation reactor comprises a plurality of heat exchange tubes and at least one distribution plate, the plurality of heat exchange tubes are distributed in an annular shape along a plurality of concentric virtual circles, so that a gas-liquid reaction medium can flow in the axial direction of the heat exchange tubes, i.e., the axial direction of the reactor, in a stable and flat push form, which is beneficial to the stability of the reaction mass transfer; a plurality of positioning through holes and a distribution structure are arranged on the distribution plate, the positioning through holes can form a positioning for the heat exchange tubes, form a support for the heat exchange tubes, and ensure the support strength for the heat exchange tubes; the distribution structure can distribute the gas-liquid reaction medium, realize a stable and uniform distribution of gas and liquid in the reactor, and improve the reaction conversion rate; the distribution form of the heat exchange tubes and the cooperation of the distribution plate can avoid the reverse mixing phenomenon under the condition of heat extraction of the isononanol hydroformylation reaction.

[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 diagram of a heat exchange distribution structure for an isononanol hydroformylation reactor according to an embodiment of the present invention is shown.

[0022] Figure 2 A schematic diagram of the distribution of heat exchange tubes of a heat exchange distribution structure for an isononanol hydroformylation reactor according to an embodiment of the present invention is shown.

[0023] Figure 3A schematic structural diagram of a heat exchange tube of a heat exchange distribution structure for an isononanol hydroformylation reactor according to an embodiment of the present invention is shown.

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

[0027] Figure 7 A schematic structural diagram of a tubular distributor of a heat exchange distribution structure for an isononanol hydroformylation reactor according to another embodiment of the present invention is shown.

[0028] Figure 8 Shows Figure 7 Schematic diagram of the cross-sectional structure in the A direction.

[0029] Fig. 9 Shows Figure 7 Schematic diagram of the cross-sectional structure in the B direction.

[0030] Description of reference numerals:

[0031] 601, heat exchange tube; 602, distribution plate; 603, positioning through hole; 604, inner tube; 605, outer tube; 606, first sealing plate; 607, second sealing plate; 608, heat exchange medium inlet; 609, heat exchange medium outlet; 610, first fixed baffle; 611, second fixed baffle; 612, heat exchange medium inlet space; 613, heat exchange medium outlet space; 614, heat exchange medium total inlet; 615, heat exchange medium total outlet; 616, distribution through hole; 617, tubular distributor; 618, tube body; 619, buffer plate; 620, connecting pin; 621, flow through hole. DETAILED DESCRIPTION

[0032] 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.

[0033] like Figure 1 and Figure 2 As shown, the present invention provides a heat exchange distribution structure for an isononanol hydroformylation reactor, comprising:

[0034] A plurality of heat exchange tubes 601, wherein the axes of the plurality of heat exchange tubes 601 are parallel to each other, and the plurality of heat exchange tubes 601 are distributed in a ring shape along a plurality of concentric virtual circles;

[0035] At least one distribution plate 602 is provided with a plurality of positioning through holes 603 and a distribution structure, and a plurality of heat exchange tubes 601 are respectively passed through the plurality of positioning through holes 603 .

[0036] Specifically, in order to solve the problems that the gaseous reactants in the isononanol hydroformylation reactor in the prior art are unevenly distributed, which easily causes the liquid reactants to form vortices and then back-mixing, and the local concentration stability of the gaseous reactants at different axial positions is poor, and the reaction conversion rate is low; the heat exchange distribution structure for the isononanol hydroformylation reactor provided by the present invention comprises a plurality of heat exchange tubes 601 and at least one distribution plate 602, and the plurality of heat exchange tubes 601 are annularly distributed along a plurality of concentric virtual circles, so that the gas-liquid reaction medium can be pushed in a stable manner along the axis of the heat exchange tube 601. The axial flow toward the reactor is beneficial to the stability of the reaction mass transfer. A plurality of positioning through holes 603 and a distribution structure are provided on the distribution plate 602. The positioning through holes 603 can position the heat exchange tube 601, form support for the heat exchange tube 601, and ensure the support strength of the heat exchange tube 601. The distribution structure can distribute the gas-liquid reaction medium to achieve stable and uniform distribution of gas and liquid in the reactor and improve the reaction conversion rate. The distribution form of the heat exchange tube 601 and the coordination of the distribution plate 602 can avoid the back mixing phenomenon while meeting the heat extraction conditions of the isononanol hydroformylation reaction.

[0037] Optionally, the heat exchange tube 601 includes an inner tube 604 and an outer tube 605, and the two ends of the outer tube 605 are respectively provided with a first sealing plate 606 and a second sealing plate 607, one end of the inner tube 604 is passed through the outer tube 605 and forms a first gap with the first sealing plate 606, the other end of the inner tube 604 passes through the second sealing plate 607 and extends outward to form an extension portion, the outer end of the extension portion forms a heat exchange medium inlet 608, and a heat exchange medium outlet 609 is opened on the outer wall of the outer tube 605.

[0038] Specifically, Figure 3 As shown, the heat exchange tube 601 includes an inner tube 604 and an outer tube 605. The inner tube 604 and the outer tube 605 form a shell-and-tube heat exchange tube 601 structure. The heat exchange medium enters from the heat exchange medium inlet 608, passes through the inside of the inner tube 604, between the outer tube 605 and the inner tube 604, and then flows out through the heat exchange medium outlet 609, thereby completing the heat exchange inside the reactor. Such a shell-and-tube heat exchange structure can improve the uniformity of heat exchange.

[0039] In this embodiment, the reactor is an isononanol hydroformylation reactor, and the heat exchange medium is a heat extraction medium.

[0040] Optionally, it also includes a first fixed baffle 610 and a second fixed baffle 611, the first fixed baffle 610 is connected to the extension part, the second fixed baffle 611 is connected to the outer tube 605, a heat exchange medium inlet space 612 is formed on the side of the first fixed baffle 610 away from the second fixed baffle 611, a heat exchange medium outflow space 613 is formed between the first fixed baffle 610 and the second fixed baffle 611, and the heat exchange medium inlet 608 and the heat exchange medium outlet 609 are respectively located in the heat exchange medium inlet space 612 and the heat exchange medium outflow space 613.

[0041] Specifically, the outer periphery of the first fixed baffle 610 and the second fixed baffle 611 can be used to connect to the reactor, and the heat exchange medium can be first injected into the heat exchange medium entering space 612, and then enter the heat exchange medium inlet 608 of the multiple heat exchange tubes 601. After the heat exchange is completed, it flows out from the heat exchange medium outlet 609 and enters the heat exchange medium outflow space 613.

[0042] Optionally, a first tubular structure is provided on the side of the first fixed baffle 610 away from the second fixed baffle 611, one end of the first tubular structure is connected to the first fixed baffle 610 and forms a heat exchange medium inlet cavity therein, a total heat exchange medium inlet 614 is provided at the other end of the first tubular structure, a second tubular structure is provided between the first fixed baffle 610 and the second fixed baffle 611, two ends of the second tubular structure are respectively connected to the first fixed baffle 610 and the second fixed baffle 611 and form a heat exchange medium outflow cavity therein, and a total heat exchange medium outlet 615 is provided on the outer wall of the second tubular structure.

[0043] Specifically, a cover plate is provided at the other end of the first cylindrical structure, and a heat exchange medium main inlet 614 is provided in the middle of the cover plate for connecting with the heat exchange medium injection pipe. The setting of the heat exchange medium inlet cavity can accommodate the heat exchange medium and allow the heat exchange medium to evenly enter each heat exchange tube 601, thereby further improving the uniformity of heat exchange. The heat exchange and outflowing heat exchange medium first enters the heat exchange medium outflow cavity, and then is uniformly discharged through the heat exchange medium main outlet 615.

[0044] Optionally, the heat exchange medium flowing in the heat exchange tube 601 is deoxygenated water.

[0045] 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.

[0046] In this embodiment, the diameter of the inner tube 604 is 10-80 mm, the diameter of the outer tube 605 is 30-100 mm, and the wall thickness of the inner tube 604 and the outer tube is 1-5 mm.

[0047] Optionally, at least two distribution plates 602 are provided, and at least two distribution plates 602 are arranged at intervals along the axis of the heat exchange tube 601, and the interval between adjacent distribution plates 602 is 500-5000 mm.

[0048] Specifically, the periphery of the distribution plate 602 can be connected to the reactor, and the distribution plate 602 can not only support and position the multiple heat exchange tubes 601, but also promote the mixing and uniform distribution of the gas-liquid reaction medium; the number of distribution plates 602 can be set according to the actual reaction process parameters.

[0049] Optionally, the aperture of the positioning through hole 603 is 2-10 mm larger than the outer diameter of the heat exchange tube 601 .

[0050] Specifically, the positioning through hole 603 is slightly larger than the heat exchange tube 601 inserted therein.

[0051] In this embodiment, the distribution structure includes a plurality of distribution through holes 616 , and the plurality of distribution through holes 616 are opened on the distribution plate 602 .

[0052] Specifically, Figure 4 As shown, the shape of the distribution through holes 616 can be circular, square, diamond, polygonal, etc. The equivalent diameter of the distribution through holes 616 is 20-50 mm, and the opening rate is more than 20%. The distribution through holes 616 can be evenly distributed on the distribution plate 602, or distributed between adjacent positioning through holes 603. The distribution through holes 616 allow the gas-liquid reaction medium to pass through, so as to evenly distribute the gas-liquid reaction medium.

[0053] In another embodiment, the distribution plate 602 is a slit mesh plate, and the slits and / or meshes of the slit mesh plate form a distribution structure.

[0054] Specifically, Figure 5 As shown, the slit mesh plate is provided with slits and / or mesh holes. Preferably, a wedge-shaped welded screen plate, i.e. a wedge-shaped welded screen plate, can be used as the distribution plate 602, thereby forming a distribution plate 602 with a distribution structure, which has a mixing effect of compressing and expanding the lower incoming flow.

[0055] In another other embodiment, the distribution structure includes a plurality of tubular distributors 617, a plurality of mounting holes are opened on the distribution plate 602, and the plurality of tubular distributors 617 are respectively installed on the reaction medium inflow side of the distribution plate 602 through the plurality of mounting holes. The tubular distributor 617 includes a tube body 618 and a buffer plate 619, one end of the tube body 618 is connected to the mounting hole, a plurality of flow holes 621 are opened on the outer wall of the tube body 618, a plurality of connecting pins 620 are arranged at intervals on the outer periphery of the buffer plate 619, and the buffer plate 619 is connected to the tube body 618 through the connecting pins 620.

[0056] Specifically, Figures 6 to 9As shown, a plurality of tubular distributors 617 can also be provided on the distribution plate 602 as a distribution structure. The plurality of tubular distributors 617 are respectively mounted on a plurality of mounting holes on the distribution plate 602. The plurality of tubular distributors 617 can be evenly distributed on the distribution plate 602 or distributed between adjacent positioning holes 603. The lower portion of the tubular distributor 617 is a buffer plate 619. The buffer plate 619 is connected to the lower end of the tube body 618 via a connecting pin 620 extending axially along the tube body 618, and an opening is formed between adjacent connecting pins 620. Symmetrically distributed flow holes 621 are provided on the tube body 618, and most of the gas-liquid reaction medium passes through the above-mentioned opening between the buffer plate 619 and the tube body 618. The structure of the flow holes 621 can be a slit or a hole to ensure that the gas phase will not accumulate under the distribution plate 602 to form an air cushion layer.

[0057] 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. A heat exchange distribution structure for an isononanol hydroformylation reactor, characterized in that: include: A plurality of heat exchange tubes, wherein the axes of the plurality of heat exchange tubes are parallel to each other, and the plurality of heat exchange tubes are distributed in a ring shape along a plurality of concentric virtual circles; At least one distribution plate is provided with a plurality of positioning through holes and a distribution structure, and a plurality of heat exchange tubes are respectively passed through the plurality of positioning through holes.

2. The heat exchange distribution structure for isononanol hydroformylation reactor according to claim 1, characterized in that: The heat exchange tube includes an inner tube and an outer tube, and the two ends of the outer tube are respectively provided with a first sealing plate and a second sealing plate. One end of the inner tube is inserted into the outer tube and forms a first gap with the first sealing plate. The other end of the inner tube passes through the second sealing plate and extends outward to form an extension portion. The outer end of the extension portion forms a heat exchange medium inlet. A heat exchange medium outlet is opened on the outer wall of the outer tube.

3. The heat exchange distribution structure for isononanol hydroformylation reactor according to claim 2, characterized in that: It also includes a first fixed baffle and a second fixed baffle, the first fixed baffle is connected to the extension portion, the second fixed baffle is connected to the outer tube, a heat exchange medium inlet space is formed on the side of the first fixed baffle away from the second fixed baffle, a heat exchange medium outflow space is formed between the first fixed baffle and the second fixed baffle, and the heat exchange medium inlet and the heat exchange medium outlet are respectively located in the heat exchange medium inlet space and the heat exchange medium outflow space.

4. The heat exchange distribution structure for isononanol hydroformylation reactor according to claim 3, characterized in that: A first tubular structure is provided on the side of the first fixed baffle away from the second fixed baffle, one end of the first tubular structure is connected to the first fixed baffle and forms a heat exchange medium inlet cavity therein, the other end of the first tubular structure is provided with a heat exchange medium main inlet, a second tubular structure is provided between the first fixed baffle and the second fixed baffle, both ends of the second tubular structure are respectively connected to the first fixed baffle and the second fixed baffle and form a heat exchange medium outflow cavity therein, and a heat exchange medium main outlet is provided on the outer wall of the second tubular structure.

5. The heat exchange distribution structure for isononanol hydroformylation reactor according to claim 2, characterized in that: The heat exchange medium flowing in the heat exchange tube is deoxygenated water.

6. The heat exchange distribution structure for 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 along the axis of the heat exchange tube, and the spacing between adjacent distribution plates is 500-5000 mm.

7. The heat exchange distribution structure for isononanol hydroformylation reactor according to claim 1, characterized in that: The aperture of the positioning through hole is 2-10 mm larger than the outer diameter of the heat exchange tube.

8. The heat exchange distribution structure for isononanol hydroformylation reactor according to claim 1, characterized in that: The distribution structure includes a plurality of distribution through holes, and the plurality of distribution through holes are opened on the distribution plate.

9. The heat exchange distribution structure for isononanol hydroformylation reactor according to claim 1, characterized in that: The distribution plate is a slit mesh plate, and the slits and / or mesh holes of the slit mesh plate form the distribution structure.

10. The heat exchange distribution structure for isononanol hydroformylation reactor according to claim 1, characterized in that: The distribution structure includes a plurality of tubular distributors, a plurality of mounting holes are provided on the distribution plate, and the plurality of tubular distributors are respectively installed on the reaction medium inflow side of the distribution plate through the plurality of mounting holes. The tubular distributor includes a tube body and a buffer plate, one end of the tube body is connected to the mounting hole, a plurality of flow through holes are provided on the outer wall of the tube body, a plurality of connecting pins are arranged at intervals on the outer periphery of the buffer plate, and the buffer plate is connected to the tube body through the connecting pins.

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