Olefin hydroformylation reactor

Abstract

The invention provides an olefin hydroformylation reactor, and relates to the technical field of stirred tank equipment, the olefin hydroformylation reactor comprises a reactor main body, the reactor main body is provided with a reaction chamber; a gas distributor is arranged in the reaction cavity, and the gas distributor is higher than the outer circulating material outlet; a heat exchanger is arranged in the reaction cavity, and a heat exchange medium outlet and a heat exchange medium inlet which are communicated with the heat exchanger are formed in the reactor main body. According to the olefin hydroformylation reactor provided by the invention, the heat exchanger is arranged in the reaction cavity and can exchange heat with a liquid phase, so that heat generated by reaction in the reactor main body can be taken away in time, the temperature in the reactor main body is effectively reduced, and the temperature is controlled under required reaction conditions; the occurrence of explosion or temperature runaway accidents is avoided; the heat exchanger can also play a baffle role, so that the flow field distribution in the reactor main body is improved, and the stirring effect is improved.

Description

Technical Field

[0001] This invention relates to the technical field of stirred tank equipment, and in particular to an olefin hydroformylation reactor. Background Technology

[0002] Olefin hydroformylation is a typical gas-liquid reaction process in which olefins react with carbon monoxide (CO) and hydrogen (H2) under the catalysis of a transition metal carbonyl complex to produce an aldehyde with one more carbon atom. This reaction is chemically rapid, with the gas phase readily soluble in the liquid phase, making it a gas-liquid mass transfer controlled reaction process. Throughout the reaction, the gas-phase conversion rate can reach over 90%, and the gas phase mass decreases significantly with increasing altitude. Efficient mass transfer between the gas and liquid phases is crucial for initiating and maintaining the olefin hydroformylation reaction.

[0003] Among numerous gas-liquid reactors, stirred tank reactors are widely used due to their advantages, including high mixing efficiency, excellent mass and heat transfer performance, ease of operation, and control. Most gas mass transfer processes are primarily controlled by liquid film resistance. Mechanical stirring can achieve uniform mixing of the gas and liquid phases, enhancing the mass transfer process and thus accelerating chemical reaction rates and improving production efficiency.

[0004] The hydroformylation of olefins is an exothermic reaction, and the heat generated must be removed in a timely manner. The reactor temperature needs to be controlled under the required reaction conditions to avoid explosions or overheating accidents. Further research is needed on how to control the reaction temperature. Summary of the Invention

[0005] The purpose of this invention is to provide an olefin hydroformylation reactor to solve the technical problem that the heat generated in the olefin hydroformylation reaction cannot be effectively dissipated.

[0006] The present invention provides an olefin hydroformylation reactor, comprising a reactor body having a reaction chamber, and an external circulation material outlet and an external circulation material inlet communicating with the reaction chamber, wherein the external circulation material inlet is higher than the external circulation material outlet; A gas distributor is installed inside the reaction chamber, and the height of the gas distributor is higher than the external circulating material outlet. A heat exchanger is provided inside the reaction chamber, and a heat exchange medium outlet and a heat exchange medium inlet are provided on the reactor body, which are connected to the heat exchanger.

[0007] In an optional embodiment, a stirring shaft is provided inside the reactor body, and the upper end of the stirring shaft extends from the upper end of the reactor body. The stirring shaft is provided with a bottom impeller, a middle impeller and a top impeller from bottom to top. The bottom impeller is a parabolic turbine impeller, the middle impeller is a large-disc wide-blade axial flow impeller and the top impeller is an oblique-blade open turbine impeller.

[0008] In an optional embodiment, the stirring shaft is further provided with a secondary top layer impeller, which is disposed between the middle layer impeller and the top layer impeller, and the secondary top layer impeller is an oblique blade open turbine impeller. In an optional embodiment, the heat exchanger includes multiple heat exchanger units arranged circumferentially along the stirring shaft; and the upper ends of the multiple heat exchanger units are connected by an upper connecting pipe and the lower ends are connected by a lower connecting pipe; the upper connecting pipe extends to the outside of the reactor body and forms a heat exchange medium outlet, and the lower connecting pipe extends to the outside of the reactor body and forms a heat exchange medium inlet.

[0009] In an optional embodiment, the external circulation material outlet is located directly below the reactor body, and an anti-swirl assembly is fixedly installed inside the reactor body. The anti-swirl assembly is located above the external circulation material outlet and below the gas distributor.

[0010] In an optional embodiment, the gas distributor includes an outer annular tube, a middle annular tube, and an inner annular tube, with the middle annular tube sleeved on the inner annular tube and the outer annular tube sleeved on the middle annular tube; and the middle annular tube is provided with an inner connecting pipe for communicating with the inner annular tube and an outer connecting pipe for communicating with the outer annular tube. An air inlet pipe is provided on the external connecting pipe, and the air inlet pipe extends outside the reactor body. In an optional embodiment, the outer annular pipe, the middle annular pipe, and the inner annular pipe are all provided with a first air inlet hole, and the first air inlet hole is obliquely downward. In an optional embodiment, the angle between the orientation of the first air inlet and the axial direction of the stirring shaft is between 45° and 60°. In an optional embodiment, the gas distributor includes a main air inlet pipe, and a plurality of spaced-apart branch air inlets are provided along the length of the main air inlet pipe. The gas distributor is provided with a second air inlet hole, which is obliquely downward; the angle between the orientation of the second air inlet hole and the axial direction of the stirring shaft is between 30° and 60°. In an optional embodiment, the reactor body is provided with a liquid raw material inlet, a gas outlet, an overflow port, a thermometer assembly port, and a manhole; the gas outlet is located at the upper end of the reactor body.

[0011] The olefin hydroformylation reactor provided by this invention is equipped with a heat exchanger in the reaction chamber. The heat exchanger can exchange heat with the liquid phase, thereby timely removing the heat generated by the reaction in the reactor body, effectively reducing the temperature in the reactor body, keeping the temperature under the required reaction conditions, and avoiding explosions or overheating accidents. In addition, the heat exchanger can also act as a baffle, improving the flow field distribution in the reactor body and enhancing the stirring effect. Attached Figure Description

[0012] To more clearly illustrate the specific embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the specific embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0013] Figure 1 This is a schematic diagram of the structure of the olefin hydroformylation reactor provided in an embodiment of the present invention; Figure 2 for Figure 1 A schematic diagram of the gas distributor in the olefin hydroformylation reactor shown. Figure 3 for Figure 1 Another schematic diagram of the gas distributor in the olefin hydroformylation reactor shown; Figure 4 for Figure 1 Another schematic diagram of the stirring shaft of the olefin hydroformylation reactor shown.

[0014] Icons: 100-Reactor body; 200-Gas inlet; 300-Gas distributor; 301-Inner annular pipe; 302-Middle annular pipe; 303-Outer annular pipe; 304-External connecting pipe; 305-Inner connecting pipe; 306-First air inlet; 307-Main air inlet; 308-Branch air inlet; 309-Second air inlet; 400-Gas outlet; 500-Liquid raw material inlet; 600-External circulating material outlet; 700-Overflow port; 800-External circulating material inlet; 900-Heat exchanger; 110-Heat exchange medium inlet; 120-Heat exchange medium outlet; 130-Stirring shaft; 140-Bottom layer impeller; 150-Middle layer impeller; 160-Top layer impeller; 170-Thermometer assembly port; 180-Desiccation assembly; 190-Manhole; 210-Reaction chamber; 220-Secondary top layer impeller. Detailed Implementation

[0015] The terms “first,” “second,” “third,” etc., are used only for distinguishing descriptions and do not indicate a sequence number, nor should they be interpreted as indicating or implying relative importance.

[0016] Furthermore, terms such as "horizontal," "vertical," and "sag" do not imply that components must be absolutely horizontal or suspended, but rather that they can be slightly tilted. For example, "horizontal" simply means that its direction is more horizontal relative to "vertical," and does not mean that the structure must be completely horizontal, but can be slightly tilted.

[0017] In the description of this application, it should be noted that the terms "inner", "outer", "left", "right", "upper", "lower", etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings, or the orientation or positional relationship commonly used when the product of this application is in use. They are only for the convenience of describing this application and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this application.

[0018] In the description of this application, unless otherwise expressly specified and limited, the terms “set up,” “install,” “connect,” and “link” shall be interpreted broadly, for example, as a fixed connection, a detachable connection, or an integral connection; as a mechanical connection or an electrical connection; as a direct connection or an indirect connection through an intermediate medium; or as a connection within two components.

[0019] The technical solution of this application will now be clearly and completely described with reference to the accompanying drawings.

[0020] Example Reference Figures 1-4 The present invention provides an olefin hydroformylation reactor, comprising a reactor body 100, wherein the reactor body 100 has a reaction chamber 210, and an external circulation material outlet 600 and an external circulation material inlet 800 communicating with the reaction chamber 210 are provided on the reactor body 100, wherein the external circulation material inlet 800 is higher than the external circulation material outlet 600. A gas distributor 300 is provided inside the reaction chamber 210, and the height of the gas distributor 300 is higher than that of the external circulating material outlet 600. A heat exchanger 900 is provided in the reaction chamber 210, and a heat exchange medium outlet 120 and a heat exchange medium inlet 110 communicating with the heat exchanger 900 are provided on the reactor body 100.

[0021] In some embodiments, the reactor body 100 has a reaction chamber 210, and the reactor body 100 is provided with a liquid raw material inlet 500, a gas outlet 400, an overflow port 700, a thermometer mounting port 170 and a manhole 190 communicating with the reaction chamber 210; the gas outlet 400 is located at the upper end of the reactor body 100; the thermometer mounting port 170 is used to mount a thermometer, thereby realizing the measurement of the temperature inside the reactor body 100.

[0022] The ratio of the height to the inner diameter of the reactor body 100 can be between 1.5 and 2.5. Generally, the ratio of the height to the inner diameter of the straight section of the reactor body 100 is 1.96. The ratio of the maximum aeration level to the normal aeration level is 1.25, and the head shape of the reactor body 100 is a standard ellipsoidal bottom.

[0023] The reactor body 100 is equipped with an external circulation material outlet 600 and an external circulation material inlet 800. The material in the reaction chamber 210 flows out from the external circulation material outlet 600, passes through a pressurization device, and then enters from the external circulation material inlet 800. This allows the material located below the gas distributor 300 to flow back to the top of the gas distributor 300, allowing unreacted material to react with the gas phase. Excess gas and liquid that cannot react in time are discharged from the gas phase outlet 400 and the external circulation material outlet 600, respectively, and the liquid level is controlled through the overflow port 700. The temperature of the material in the reactor is more precisely controlled by the external circulation flow rate, and the heat is distributed more evenly by the fluid flow, thereby reducing the risk of local overheating.

[0024] The heat exchanger 900 is installed inside the reaction chamber 210. The heat exchange medium can be water. The heat exchange medium can enter from the heat exchange medium inlet 110. After heat exchange in the heat exchanger 900, the heat exchange medium flows out from the heat exchange medium outlet 120. In this way, the temperature inside the reaction chamber 210 is reduced by the heat exchanger 900, so that the temperature is controlled within the required reaction conditions, avoiding the occurrence of explosion or overheating accidents. In addition, the heat exchanger 900 can also act as a baffle, improving the flow field distribution within the reactor body 100 and enhancing the stirring effect.

[0025] In some embodiments, the liquid feed inlet 500 and the external circulating material inlet 800 can be combined into a single inlet. Combining inlets reduces the number of pipes and interfaces, thereby simplifying the design and manufacture of the stirred tank; it can reduce the resistance of the fluid entering the reactor body 100, thereby reducing the energy required to pump the fluid; the combined inlet of the liquid phase and circulating material can promote more uniform mixing of the two, as they begin to mix as they enter the reactor body 100; the combined inlet allows for more centralized and precise flow control of the feed and circulating materials, facilitating adjustments by operators; and premixing the material before it enters the reactor body 100 makes it easier to adapt to different operating conditions and material characteristics.

[0026] In an optional embodiment, a stirring shaft 130 is provided inside the reactor body 100, and the upper end of the stirring shaft 130 extends from the upper end of the reactor body 100. The stirring shaft 130 is provided with a bottom impeller 140, a middle impeller 150 and a top impeller 160 arranged sequentially from bottom to top. The bottom impeller 140 is a parabolic turbine impeller, the middle impeller 150 is a large-disc wide-blade axial flow impeller, and the top impeller 160 is an oblique-blade open turbine impeller.

[0027] In an optional embodiment, a secondary top-layer impeller 220 is further provided on the stirring shaft 130, and the secondary top-layer impeller 220 is disposed between the middle layer impeller 150 and the top layer impeller 160, and the secondary top-layer impeller 220 is an oblique blade open turbine impeller.

[0028] The stirring shaft 130 can rotate from 80 rpm to 120 rpm depending on the motor model selected. However, considering power consumption and stirring efficiency, the speed is mainly controlled at 108 rpm. Reference Figure 1 and Figure 4 The stirring shaft 130 has two different blade combination configurations with varying numbers of blade layers. Each blade combination includes at least three blade layers, which can be increased to four, while maintaining a constant distance between the bottom blade 140 and the top blade 160, and consistent spacing between blades. The blade diameter is slightly reduced while ensuring minimal power variation. In the three-blade configuration, the bottom blade 140 is a parabolic turbine blade capable of generating radial flow, reducing power consumption and minimizing the volume of the wake vortex while enhancing the retention effect on the gas phase. The middle blade 150 is a large-disk, wide-blade axial flow blade capable of generating strong axial circulation, further pressing down and breaking up bubbles. The top blade 160 is an open-blade turbine blade, controlling the circulation structure while further reducing power consumption. In the four-blade configuration, a second-to-top blade 220 is added. The bottom blade 140 to the top blade 160 are sequentially configured as a parabolic turbine blade, a large-disk, wide-blade axial flow blade, an open-blade turbine blade, and an open-blade turbine blade.

[0029] In some embodiments, the stirring shaft 130 may be vertically mounted into the reactor body 100 from the top center, and the multi-layered impeller may be configured with 3 or 4 layers depending on the annual production demand or the normal operating liquid level within the reactor body 100. The diameter of the impeller may be 0.33 to 0.4 times the inner diameter of the reactor body 100, and the distance between two adjacent sets of impellers may be 0.8 to 1.2 times the diameter of the impeller blades.

[0030] In an optional embodiment, the heat exchanger 900 includes a plurality of individual heat exchanger units 900, which are arranged circumferentially along the stirring shaft 130; and the upper ends of the plurality of individual heat exchanger units 900 are connected by an upper connecting pipe and the lower ends are connected by a lower connecting pipe; the upper connecting pipe extends to the outside of the reactor body 100 and forms a heat exchange medium outlet 120, and the lower connecting pipe extends to the outside of the reactor body 100 and forms a heat exchange medium inlet 110.

[0031] In some embodiments, the height of the heat exchange medium outlet 120 is higher than that of the heat exchange medium inlet 110, and the heat exchange medium inlet 110 is located at the lowest point of the heat exchanger 900, while the heat exchange medium outlet 120 is located at the highest point of the heat exchanger 900. The heat exchanger 900 units are uniformly arranged circumferentially along the stirring shaft 130. Each heat exchanger 900 unit can act as a baffle to improve the flow field distribution in the reaction chamber 210 and enhance the stirring effect.

[0032] In an optional embodiment, the external circulation material outlet 600 is located directly below the reactor body 100, and an anti-swirl assembly 180 is fixedly installed inside the reactor body 100. The anti-swirl assembly 180 is located above the external circulation material outlet 600 and below the gas distributor 300.

[0033] An anti-swirl assembly 180 is installed inside the reaction chamber 210. The anti-swirl assembly 180 is installed directly below the gas distributor 300. The radial jet generated by the radial paddle discharge action is highly symmetrical. The fluid flow in the area directly below the stirring shaft 130 is very weak. The anti-swirl assembly 180 can eliminate vortices that are not conducive to fluid flow and reaction. The anti-swirl assembly 180 does not affect the flow of liquid phase into the external circulation material outlet 600. The anti-swirl assembly 180 is spaced from the inner wall of the reaction chamber 210, or the anti-swirl assembly 180 is provided with holes for liquid phase flow.

[0034] Reference Figure 2 In an optional embodiment, the gas distributor 300 includes an outer annular tube 303, a middle annular tube 302, and an inner annular tube 301. The middle annular tube 302 is sleeved on the inner annular tube 301, and the outer annular tube 303 is sleeved on the middle annular tube 302. The middle annular tube 302 is provided with an inner connecting tube 305 for communicating with the inner annular tube 301 and an outer connecting tube 304 for communicating with the outer annular tube 303. An air inlet pipe is provided on the external connecting pipe 304, and the air inlet pipe extends outside the reactor body 100. In an optional embodiment, the outer annular pipe 303, the middle annular pipe 302 and the inner annular pipe 301 are all provided with a first air inlet hole 306, and the first air inlet hole 306 is arranged obliquely downward. In an optional embodiment, the angle between the orientation of the first air inlet 306 and the axial direction of the stirring shaft 130 is between 45° and 60°. The annular gas distributor 300 has advantages such as simple structure, improved mass transfer performance of the reactor by adjusting the orifice direction, diameter, and installation height, and facilitates uniform gas distribution within a specific area. In different embodiments, the annular gas distributor 300 consists of an outer annular pipe 303, a middle annular pipe 302, and an inner annular pipe 301 that are interconnected. The gas phase inlet 200 enters from the outer connecting pipe 304 that connects the outer annular pipe 303 and the middle annular pipe 302. The gas phase is distributed to the outer annular pipe 303, the middle annular pipe 302, and the inner annular pipe 301 through the outer connecting pipe 304. The vertical pipe connecting the outer annular pipe 303, the middle annular pipe 302, and the inner annular pipe 301 mainly serves a supporting and fixing function. The outer annular tube 303, the middle annular tube 302 and the inner annular tube 301 are evenly distributed with multiple first air inlet holes 306 at an angle of 45-60° to the outside. The gas distributor 300 has 100 to 160 circular first air inlet holes 306, and the diameter of the first air inlet holes 306 can be between 4 and 8 mm.

[0035] Reference Figure 3 In an optional embodiment, the gas distributor 300 includes a main air intake pipe 307, and a plurality of branch air intake pipes 308 are provided at intervals along the length of the main air intake pipe 307. The gas distributor 300 is provided with a second air inlet 309, and the second air inlet 309 is obliquely downward; the angle between the orientation of the second air inlet 309 and the axial direction of the stirring shaft 130 is between 30° and 60°. The main inlet pipe 307 is connected to several symmetrical branch inlet pipes 308. The length of the branch inlet pipes 308 decreases as the distance from the center of the reactor body 100 increases. The outer contour of the entire gas distributor 300 is circular. Two second inlet holes 309 on the main inlet pipe 307 and the branch inlet pipes 308 are arranged at equal intervals. The spacing of the second inlet holes 309 is determined according to the length of the branch inlet pipes 308. The direction of the second inlet holes 309 is obliquely downward and outward at 30-60°. The gas distributor 300 has 100 to 160 circular second inlet holes 309, and the diameter of the second inlet holes 309 can be between 4 and 8 mm.

[0036] The olefin hydroformylation reactor provided by the present invention is equipped with a heat exchanger 900 in the reaction chamber 210. The heat exchanger 900 can exchange heat with the liquid phase, thereby timely removing the heat generated by the reaction in the reactor body 100, effectively reducing the temperature in the reactor body 100, keeping the temperature under the required reaction conditions, and avoiding explosions or overheating accidents. In addition, the heat exchanger 900 can also act as a baffle, improving the flow field distribution in the reactor body 100 and enhancing the stirring effect.

[0037] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, and not to limit them; although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some or all of the technical features; and these modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. An olefin hydroformylation reactor, characterized in that, The reactor body (100) includes a reaction chamber (210), and an external circulation material outlet (600) and an external circulation material inlet (800) communicating with the reaction chamber (210) are provided on the reactor body (100), and the external circulation material inlet (800) is higher than the external circulation material outlet (600). A gas distributor (300) is provided inside the reaction chamber (210), and the height of the gas distributor (300) is higher than that of the external circulating material outlet (600). A heat exchanger (900) is provided in the reaction chamber (210), and a heat exchange medium outlet (120) and a heat exchange medium inlet (110) communicating with the heat exchanger (900) are provided on the reactor body (100).

2. The olefin hydroformylation reactor according to claim 1, characterized in that, A stirring shaft (130) is provided inside the reactor body (100), and the upper end of the stirring shaft (130) extends from the upper end of the reactor body (100). The stirring shaft (130) is provided with a bottom impeller (140), a middle impeller (150) and a top impeller (160) arranged from bottom to top. The bottom impeller (140) is a parabolic turbine impeller, the middle impeller (150) is a large-disc wide-blade axial flow impeller, and the top impeller (160) is an oblique-blade open turbine impeller.

3. The olefin hydroformylation reactor according to claim 2, characterized in that, The stirring shaft (130) is also provided with a secondary top layer impeller (220), and the secondary top layer impeller (220) is located between the middle layer impeller (150) and the top layer impeller (160), and the secondary top layer impeller (220) is an oblique blade open turbine impeller.

4. The olefin hydroformylation reactor according to claim 2, characterized in that, The heat exchanger (900) includes multiple heat exchanger (900) units, which are arranged circumferentially along the stirring shaft (130); and the upper ends of the multiple heat exchanger (900) units are connected by an upper connecting pipe and the lower ends are connected by a lower connecting pipe; the upper connecting pipe extends to the outside of the reactor body (100) and forms a heat exchange medium outlet (120), and the lower connecting pipe extends to the outside of the reactor body (100) and forms a heat exchange medium inlet (110).

5. The olefin hydroformylation reactor according to claim 1, characterized in that, The external circulation material outlet (600) is located directly below the reactor body (100). An anti-swirl assembly (180) is fixedly installed inside the reactor body (100). The anti-swirl assembly (180) is located above the external circulation material outlet (600) and below the gas distributor (300).

6. The olefin hydroformylation reactor according to claim 2, characterized in that, The gas distributor (300) includes an outer annular tube (303), a middle annular tube (302), and an inner annular tube (301). The middle annular tube (302) is sleeved on the inner annular tube (301), and the outer annular tube (303) is sleeved on the middle annular tube (302). The middle annular tube (302) is provided with an inner connecting tube (305) for communicating with the inner annular tube (301) and an outer connecting tube (304) for communicating with the outer annular tube (303). An air inlet pipe is provided on the external connecting pipe (304), and the air inlet pipe extends outside the reactor body (100).

7. The olefin hydroformylation reactor according to claim 6, characterized in that, The outer annular pipe (303), the middle annular pipe (302) and the inner annular pipe (301) are each provided with a first air inlet hole (306), and the first air inlet hole (306) is arranged obliquely downward.

8. The olefin hydroformylation reactor according to claim 7, characterized in that, The angle between the orientation of the first air inlet (306) and the axial direction of the stirring shaft (130) is between 45° and 60°.

9. The olefin hydroformylation reactor according to claim 2, characterized in that, The gas distributor (300) includes a main intake pipe (307), and a plurality of branch intake pipes (308) are provided at intervals along the length of the main intake pipe (307). The gas distributor (300) is provided with a second air inlet (309), and the second air inlet (309) is obliquely downward; the angle between the orientation of the second air inlet (309) and the axial direction of the stirring shaft (130) is between 30° and 60°.

10. The olefin hydroformylation reactor according to claim 1, characterized in that, The reactor body (100) is provided with a liquid raw material inlet (500), a gas outlet (400), an overflow port (700), a thermometer assembly port (170), and a manhole (190); the gas outlet (400) is located at the upper end of the reactor body (100).

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