An apparatus for hydroformylation reaction, a method for hydroformylation, and its applications.

Abstract

This invention discloses an apparatus, a method, and applications for hydroformylation. The apparatus includes a vessel body, a rotating shaft inside the vessel body, and a guide cylinder and a spray grid arranged from top to bottom around the rotating shaft. The guide cylinder is connected to the upper part of the vessel body by a connecting rod. The upper end of the spray grid is connected to the lower part of the guide cylinder. Inside the spray grid and connected to the rotating shaft, a first impeller and a dispersion cylinder are arranged from top to bottom. A second impeller, communicating with the rotating shaft, is arranged inside the dispersion cylinder. The dispersion cylinder is used to cut and disperse the discharged syngas in multiple stages, allowing the syngas to enter the spray grid. The guide cylinder is used to disperse materials into the spray grid under stirring. The spray grid is used to mix and react the syngas and liquid materials to obtain reaction products. The apparatus and method of this invention improve the degree of gas-liquid mixing and achieve rapid and efficient reaction by enhancing mass transfer in the reaction process.

Description

Technical Field

[0001] This invention relates to the field of hydroformylation, and more specifically to an apparatus for hydroformylation reactions, a method for hydroformylation, and its applications. Background Technology

[0002] Hydroformylation is one of the most important catalytic reactions in industry today. It can synthesize aldehydes with high added value with 100% atom utilization, and the aldehydes produced can be further converted into important bulk and fine chemicals such as alcohols, carboxylic acids, esters and aliphatic amines.

[0003] In the olefin hydroformylation process, the syngas is in a gaseous state and must be dissolved in a solvent to come into contact with the active sites of the catalyst and react. In traditional stirred tank reactors, the syngas dissolves slowly, requiring strong stirring to ensure the reaction proceeds normally. Summary of the Invention

[0004] To address the aforementioned problems in the existing technology, the purpose of this invention is to provide an apparatus and method for hydroformylation reactions. The method of this invention can be operated batchwise or continuously, using olefins as the main raw material, and conducting a hydroformylation reaction to synthesize aldehydes in contact with syngas (H2 / CO) under the action of a catalyst. The apparatus and method of this invention improve the degree of gas-liquid mixing, achieving rapid and efficient reaction by enhancing mass transfer in the reaction process.

[0005] The first aspect of the present invention provides an apparatus for a hydroformylation reaction, the apparatus comprising a vessel body 1, a rotating shaft 2 inside the vessel body 1, and a guide vertical cylinder 3 and a spray grid plate 5 arranged from top to bottom around the rotating shaft 2; the guide vertical cylinder 3 is connected to the upper part of the vessel body 1 by a connecting rod, and the side wall of the guide vertical cylinder 3 is provided with holes 31; the spray grid plate 5 is provided below the guide vertical cylinder 3, and the upper end of the spray grid plate 5 is connected to the lower part of the guide vertical cylinder 3; a first impeller 4 and a dispersion cylinder 7 are arranged from top to bottom inside the spray grid plate 5 and connected to the rotating shaft 2; a second impeller 6 communicating with the rotating shaft 2 is provided inside the dispersion cylinder 7; the rotating shaft 2 is provided with an air intake 21; the second impeller 6 is provided with a vent hole 61; the vessel body 1 is provided with an olefin feed inlet 11, a synthesis gas feed inlet 12, a solvent feed inlet 13, and a catalyst feed inlet 14.

[0006] According to some embodiments of the apparatus of the present invention, preferably, the reactor body 1 is used for hydroformylation reaction; the rotating shaft 2 is used to rotate the first impeller 4 and the second impeller 6 to provide stirring, and to draw in the syngas input through the syngas inlet 12 through the air intake 21 of the rotating shaft 2 and to discharge the syngas through the vent hole 61 of the second impeller 6 and into the dispersion cylinder 7; the dispersion cylinder 7 is used to cut and disperse the discharged syngas in multiple stages and to allow the syngas to enter the spray grid plate 5; the guide vertical cylinder 3 is used to disperse the material into the spray grid plate 5 under the stirring action, the material including olefins input through the olefin inlet 11, syngas input through the syngas inlet 12, solvent input through the solvent inlet 13 and catalyst input through the catalyst inlet 14; the spray grid plate 5 is used to mix and react the syngas and the liquid material to obtain reaction products.

[0007] In this invention, the blade 4 and the dispersing cylinder 7 are inside the grid plate but not connected to the grid plate 5, and are both connected to the rotating shaft 2.

[0008] According to some embodiments of the apparatus of the present invention, preferably, a discharge port 15 is provided at the bottom of the vessel for discharging reaction products.

[0009] According to some embodiments of the device of the present invention, preferably, the sidewall of the spray grid plate 5 is provided with spray holes 51 for cutting and dispersing the reaction materials.

[0010] According to some embodiments of the device of the present invention, preferably, the top of the rotating shaft 2 is connected to the transmission component 8, the transmission component 8 being used to provide kinetic energy to cause the rotating shaft 2 to rotate.

[0011] According to some embodiments of the device of the present invention, preferably, the rotating shaft 2 has a hollow structure inside.

[0012] According to some embodiments of the device of the present invention, preferably, a heat exchange jacket 16 is provided on the outside of the vessel body 1.

[0013] According to some embodiments of the device described in this invention, the device further includes one or more sets of blades, as needed, for the purpose of enabling thorough mixing of materials.

[0014] According to some embodiments of the apparatus described in this invention, the vessel is in a sealed state during the reaction process.

[0015] A second aspect of the present invention provides a method for hydroformylation using the above-described apparatus, comprising the following steps:

[0016] Step a: The solvent is introduced into the vessel 1 of the device through the solvent inlet 13; under the action of stirring, the solvent is dispersed into the spray grid plate 5 through the holes 31 of the guide vertical cylinder 3 and the action of the first blade 4 to form a liquid phase;

[0017] Step b: Syngas is introduced into the vessel body 1 of the device through the syngas inlet 12. Syngas in the upper part of the vessel body 1 is introduced into the rotating shaft 2 through the air intake 21 on the rotating shaft 2, and then sprayed out through the vent hole 61 on the second blade 6. Syngas enters the dispersion cylinder 7. The dispersion cylinder 7 cuts and disperses the discharged syngas in multiple stages and makes the syngas enter the spray grid plate 5. Syngas comes into contact with the liquid phase obtained in step a and mixes for the first time to obtain a mixed liquid.

[0018] Step c: The catalyst is introduced into the vessel body (1) of the device through the catalyst inlet 14; under the action of stirring, the catalyst is dispersed into the spray grid plate 5 through the holes (31) of the guide vertical cylinder 3 and the action of the first blade 4, and comes into contact with the mixed liquid obtained in step b and is mixed for the second time to obtain a mixed liquid containing the catalyst.

[0019] Step d: The olefins are introduced into the vessel body 1 of the device through the olefin inlet 11; under the action of stirring, the olefins are dispersed into the spray grid plate 5 through the holes 31 of the guide vertical cylinder 3 and the action of the first blade 4, and come into contact with the catalyst-containing mixed liquid obtained in step c and react.

[0020] In this invention, under the action of stirring, the material near the paddle is thrown out, forming a slightly negative pressure state. Then, external material is continuously replenished, so the overall material is uniform. The function of the guide vertical cylinder is to continuously draw in the material from the upper part under the action of stirring, and then mix it around the grid plate (not only gas, but also liquid) before throwing it out.

[0021] According to some embodiments of the method described in this invention, the synthesis gas is mainly composed of carbon monoxide and hydrogen (H2 / CO).

[0022] According to some embodiments of the method described in this invention, preferably, the reaction temperature is 60-140°C, more preferably 70-100°C.

[0023] According to some embodiments of the method described according to the present invention, preferably, the pressure of the reaction is 0-20 MPa, more preferably 1-7 MPa.

[0024] According to some embodiments of the method of the present invention, preferably, the first mixing time is 1-30 min, more preferably 15-25 min.

[0025] According to some embodiments of the method of the present invention, preferably, the second mixing time is 0.1-20 min, more preferably 1-10 min.

[0026] In some embodiments of the method according to the present invention, preferably, the amount of catalyst used is 0.01-2% by weight of the amount of solvent used.

[0027] According to some embodiments of the method of the present invention, preferably, the reaction product is sprayed through the injection hole 51 to the discharge port 15.

[0028] According to some embodiments of the method described in this invention, preferably, the transmission component 8 provides kinetic energy to cause the rotating shaft 2 to rotate.

[0029] According to some embodiments of the method described in this invention, preferably, a heat exchange jacket 16 is provided on the outside of the vessel body 1.

[0030] According to some embodiments of the method described in this invention, preferably, the solvent is selected from at least one of aldehydes, ketones, benzene, substituted benzene compounds, alkanes, and substituted alkanes, more preferably from at least one of butyraldehyde, pentanal, hexanal, heptanal, octanal, nonanal, methyl isobutyl ketone, acetylbenzene, toluene, xylene, chlorobenzene, and heptane, and more preferably from toluene and / or nonanal. In this invention, the solvent and reaction system are under anhydrous and oxygen-free conditions.

[0031] According to some embodiments of the method described in this invention, preferably, the hydroformylation catalyst used in this application can be a conventional catalyst system for catalyzing the hydroformylation of olefins, including cobalt-based catalysts and rhodium-based catalysts, preferably a rhodium-based catalyst system, comprising a rhodium-containing chemical as a catalyst precursor and an organophosphorus compound as a ligand. A co-catalyst may or may not be added to this rhodium-based catalyst system.

[0032] According to some embodiments of the method of the present invention, preferably, the amount of rhodium catalyst added is 50-400 ppm based on metallic rhodium; and / or the molar ratio of organophosphorus compound to metallic rhodium in rhodium catalyst is (0.5-200):1; and / or the molar ratio of olefin to metallic rhodium in rhodium catalyst is 100000:1-500:1, preferably 10000:1-1000:1; and / or the molar ratio of CO and H2 is 1:1.

[0033] According to some specific embodiments of the present invention, the method of hydroformylation includes:

[0034] Based on the requirements of the reaction, determine the operating parameters such as reaction temperature, reaction pressure, and reaction time.

[0035] Open the material inlet valve and add solvent at a certain flow rate. Start the transmission device to drive the rotating shaft to rotate. Open the synthesis gas (H2 / CO) inlet valve and gradually adjust the gas flow rate to the reaction pressure. Stir for a period of time. Open the catalyst inlet valve and add the prepared catalyst into the reactor. Stir for a period of time. Open the olefin inlet valve and add the raw material olefin into the reactor.

[0036] As the amount of material in the reactor increases, when the liquid in the reactor reaches the set volume, the feed flow rate is adjusted according to the reaction requirements. When the feed and discharge gradually reach equilibrium, continuous operation is achieved.

[0037] If the reaction is a batch operation, the feed valve is closed when the liquid in the reactor reaches the set volume. After the reaction is completed, the synthesis gas (H2 / CO) feed valve is closed, the pressure is released, and the material is discharged from the bottom of the reactor.

[0038] The third aspect of the present invention provides the application of the above-described apparatus or the above-described hydroformylation method in the hydroformylation process of olefins.

[0039] The beneficial effects of this invention are:

[0040] The apparatus and method of the present invention achieve rapid and efficient reaction by enhancing mass transfer in the reaction process. Specifically, there are two liquid circulations within the reactor body. In the lower part of the reactor, after the slurry is thrown out by the second blade below the rotating shaft to create negative pressure, it is replenished by backflow due to the pressure difference of the slurry, thus forming a liquid circulation in the lower part of the reactor body. In addition, using the guide vertical cylinder set above the center of the apparatus, since the slurry below the guide vertical cylinder is thrown out, resulting in a slurry loss, the slurry around the guide vertical cylinder is replenished from the surrounding area to the center of the guide vertical cylinder (the guide vertical cylinder is provided with holes), thereby forming a material flow movement in the upper part.

[0041] In the gas phase, the upper part of the reactor's synthesis gas (H2 / CO) is introduced into the lower space of the reactor through the air intake at the upper end of the rotating shaft. Under the combined action of the second impeller and the dispersion cylinder, the gas undergoes multi-stage cutting, dispersion, and mixing with the liquid. After the gas-liquid mixture passes through the spray grid, it undergoes multiple actions such as collision and shearing, significantly improving the mixing of the gas and liquid two-phase materials. The synthesis gas (H2 / CO) consumed during the reaction is replenished in a timely manner through the air inlet. Attached Figure Description

[0042] Figure 1 This is a schematic diagram of the apparatus for hydroformylation reaction provided in Embodiment 1 of the present invention.

[0043] Figure 2 This is a schematic diagram of the apparatus used for the hydroformylation reaction in Comparative Example 1 and Comparative Example 2.

[0044] Explanation of reference numerals in the attached figures

[0045] 1. Reactor body; 11. Olefin feed inlet; 12. Syngas feed inlet

[0046] 13. Solvent inlet 14. Catalyst inlet 15. Outlet

[0047] 16. Heat exchange jacket 2, Rotary shaft 21, Air intake port

[0048] 3. Guide vertical cylinder 31, hole 4, first blade

[0049] 5. Injection grid plate 51, Injection hole 6, Second blade

[0050] 61. Ventilation hole; 7. Dispersion cylinder; 8. Transmission components Detailed Implementation

[0051] To make the present invention easier to understand, the present invention will be described in detail below with reference to embodiments. These embodiments are for illustrative purposes only and are not limited to the scope of application of the present invention.

[0052] In the following examples and comparative examples, catalyst activity and selectivity were characterized by olefin conversion and aldehyde selectivity, which were calculated using the following formulas:

[0053]

[0054]

[0055]

Example 1

[0056] Adopting such Figure 1The apparatus shown is for a hydroformylation reaction. The apparatus includes a vessel body 1, a rotating shaft 2 inside the vessel body 1, and a guide column 3 and a spray grid 5 arranged from top to bottom around the rotating shaft 2. The guide column 3 is connected to the upper part of the vessel body 1 by a connecting rod, and the side wall of the guide column 3 has holes 31. The spray grid 5 is located below the guide column 3, and its upper end is connected to the lower part of the guide column 3. Inside the spray grid 5 and connected to the rotating shaft 2, a first impeller 4 and a dispersion cylinder 7 are arranged from top to bottom. A second impeller 6, communicating with the rotating shaft 2, is located inside the dispersion cylinder 7. The rotating shaft 2 has an intake port 21. The second impeller 6 has vent holes 61. The vessel body 1 has an olefin inlet 11, a syngas inlet 12, a solvent inlet 13, and a catalyst inlet 14. In this process, the reactor body 1 is used for hydroformylation reaction; the rotating shaft 2 is used to rotate the first impeller 4 and the second impeller 6 to provide stirring, and to draw in the syngas input from the syngas inlet 12 through the air intake 21 of the rotating shaft 2 and to discharge the syngas through the vent hole 61 of the second impeller 6 and into the dispersion cylinder 7; the dispersion cylinder 7 is used to cut and disperse the discharged syngas in multiple stages and to allow the syngas to enter the spray grid plate 5; the guide vertical cylinder 3 is used to disperse the materials into the spray grid plate 5 under the stirring action, the materials including olefins input from the olefin inlet 11, syngas input from the syngas inlet 12, solvent input from the solvent inlet 13 and catalyst input from the catalyst inlet 14; the spray grid plate 5 is used to mix and react the syngas and the liquid materials to obtain reaction products. The bottom of the vessel body is provided with a discharge port 15 for discharging reaction products; the side wall of the spray grid plate 5 is provided with spray holes 51, through which the reaction products are sprayed to the discharge port 15; the top of the rotating shaft 2 is connected to the transmission component 8, which provides kinetic energy to make the rotating shaft 2 rotate; the interior of the rotating shaft 2 is a hollow structure. A heat exchange jacket 1 is provided on the outside of the vessel body 1.

[0057]

Example 2

[0058] The hydroformylation reaction was carried out using the apparatus for the hydroformylation reaction described in Example 1. Operating parameters such as reaction temperature, reaction pressure, and reaction time were determined based on the desired reaction requirements.

[0059] Open the material inlet valve and add solvent at a certain flow rate. Start the transmission device to drive the rotating shaft to rotate. Open the synthesis gas (H2 / CO) inlet valve and gradually adjust the gas flow rate to the reaction pressure. Stir for a period of time. Open the catalyst inlet valve and add the prepared catalyst into the reactor. Stir for a period of time. Open the olefin inlet valve and add the raw material olefin into the reactor.

[0060] As the amount of material in the reactor increases, when the liquid in the reactor reaches the set volume, the feed flow rate is adjusted according to the reaction requirements. When the feed and discharge gradually reach equilibrium, continuous operation is achieved.

[0061] If the reaction is a batch operation, the feed valve is closed when the liquid in the reactor reaches the set volume. After the reaction is complete, the synthesis gas (H2 / CO) feed valve is closed, the pressure is released, and the gas is discharged from the bottom of the reactor. Specifically:

[0062] Rhodium dicarbonyl acetylacetone was used as the catalyst precursor, and 2,2-bis[(diphenylphosphino)methyl]-1,1-biphenyl (BISBI) was used as the ligand. The molar ratio of 1-octene to Rh was 1000:1, and the concentration of Rh was 1.6 mmol / L. The reaction apparatus was purged with N2, then purged several times with syngas (CO:H2 = 1:1), and the system temperature control system was turned on to maintain the overall system temperature at 80°C. Toluene solvent and syngas (CO:H2 = 1:1) were introduced into the reactor, and the reactor pressure was maintained at 1.5 MPa. After stirring for 20 min, the catalyst inlet was opened to introduce the catalyst. The catalyst was thoroughly mixed with the toluene mixed with syngas (CO:H2 = 1:1) to begin pre-activation for 5 min. 1-Octene was introduced into the reactor through the olefin inlet, where it came into contact with a mixture of catalyst, CO, H2, and solvent to initiate a hydroformylation reaction. The reaction was carried out for 60 minutes, and the reacted material was discharged through the product outlet. The material was sampled and analyzed, and the reaction results were as follows: octene conversion rate: 93.1%, aldehyde selectivity: 96.1%.

[0063]

Example 3

[0064] The hydroformylation reaction was carried out using the apparatus for the hydroformylation reaction described in Example 1. Operating parameters such as reaction temperature, reaction pressure, and reaction time were determined based on the desired reaction requirements.

[0065] Open the material inlet valve and add solvent at a certain flow rate. Start the transmission device to drive the rotating shaft to rotate. Open the synthesis gas (H2 / CO) inlet valve and gradually adjust the gas flow rate to the reaction pressure. Stir for a period of time. Open the catalyst inlet valve and add the prepared catalyst into the reactor. Stir for a period of time. Open the olefin inlet valve and add the raw material olefin into the reactor.

[0066] As the amount of material in the reactor increases, when the liquid in the reactor reaches the set volume, the feed flow rate is adjusted according to the reaction requirements. When the feed and discharge gradually reach equilibrium, continuous operation is achieved.

[0067] If the reaction is a batch operation, the feed valve is closed when the liquid in the reactor reaches the set volume. After the reaction is complete, the synthesis gas (H2 / CO) feed valve is closed, the pressure is released, and the gas is discharged from the bottom of the reactor. Specifically:

[0068] Rhodium supported on graphene oxide was used as the catalyst (Rh loading 1 wt%), with a catalyst concentration of 0.5 wt%. The molar ratio of mixed octene (2,4,4-trimethyl-1-pentene and 2,4,4-trimethyl-2-pentene):Rh was 1000:1 based on the total molar amount. The reactor was purged with N2, then purged several times with syngas (CO:H2 = 1:1), and the system temperature control system was activated to maintain the entire system temperature at 100°C. Toluene solvent and syngas (CO:H2 = 1:1) were introduced into the reactor, and the reactor pressure was maintained at 6 MPa. After stirring for 20 min, the catalyst inlet was opened to introduce the catalyst, allowing it to fully mix with the toluene mixed with syngas (CO:H2 = 1:1) to begin pre-activation for 5 min. Mixed octene was introduced into the reactor through the olefin inlet, where it came into contact with a mixture of catalyst, CO, H2, and solvent to initiate a hydroformylation reaction. The reaction lasted for 240 minutes, and the reacted material was discharged through the product outlet. Samples were taken and analyzed, and the reaction results were as follows: mixed octene conversion rate: 79.3%, aldehyde selectivity: 98.7%.

[0069]

Example 4

[0070] The experimental method was the same as in Example 2, except that the solvent toluene and synthesis gas (CO:H2 = 1:1) were introduced into the reactor and the pressure in the reactor was maintained at 1.5 MPa. The stirring time was changed to 10 min, and the other reaction conditions remained unchanged. The experimental results were: octene conversion rate: 87.6%, aldehyde selectivity: 92.1%.

[0071]

Example 5

[0072] The experimental method was the same as in Example 2, except that toluene solvent and syngas (CO:H2 = 1:1) were introduced into the reactor and the pressure in the reactor was maintained at 1.5 MPa. The stirring time was changed to 30 min, and the other reaction conditions remained unchanged. The experimental results were: octene conversion rate: 91.2%, aldehyde selectivity: 96.4%.

[0073]

Example 6

[0074] The experimental method was the same as in Example 2, except that the catalyst was thoroughly mixed with toluene mixed with syngas (CO:H2 = 1:1) to begin pre-activation, and the pre-activation time was changed to 2 min. The other reaction conditions remained unchanged. The experimental results were: octene conversion rate: 88.4%, aldehyde selectivity: 94.6%.

[0075]

Example 7

[0076] The experimental method was the same as in Example 2, except that the catalyst was thoroughly mixed with toluene mixed with syngas (CO:H2 = 1:1) to begin pre-activation, and the pre-activation time was changed to 10 min. The other reaction conditions remained unchanged. The experimental results were: octene conversion rate: 85.5%, aldehyde selectivity: 92.1%.

[0077] Comparative Example 1

[0078] Using a traditional mixing tank ( Figure 2 As shown in the figure, the remaining reaction conditions were the same as in Example 2. The experimental results were as follows: octene conversion rate: 80.4%, aldehyde selectivity: 94.8%.

[0079] Comparative Example 2

[0080] Using a traditional mixing tank ( Figure 2 As shown in the figure, the remaining reaction conditions were the same as in Example 2. The experimental results were as follows: mixed octene conversion rate: 63.8%, aldehyde selectivity: 98.1%.

[0081] The above description is merely a preferred embodiment of the present invention. It should be noted that, for those skilled in the art, based on the technical teachings provided by the present invention and as common knowledge in the field, other equivalent modifications and improvements can be made, and these should also be considered within the scope of protection of the present invention.

Claims

1. A process for hydroformylation using a hydroformylation reaction apparatus, characterized by, The device includes a vessel body (1), a rotating shaft (2) inside the vessel body (1), and a guide vertical cylinder (3) and a spray grid plate (5) arranged from top to bottom around the rotating shaft (2); the rotating shaft (2) has a hollow structure inside; the guide vertical cylinder (3) is connected to the upper part of the vessel body (1) by a connecting rod, and the side wall of the guide vertical cylinder (3) is provided with holes (31); a spray grid plate (5) is provided below the guide vertical cylinder (3), and the upper end of the spray grid plate (5) is connected to the lower part of the guide vertical cylinder (3). The spray grid plate (5) is provided with a first impeller (4) and a dispersion cylinder (7) connected to the rotating shaft (2) from top to bottom; the dispersion cylinder (7) is provided with a second impeller (6) connected to the rotating shaft (2); the rotating shaft (2) is provided with an air intake (21); the second impeller (6) is provided with a small ventilation hole (61); the reactor body (1) is provided with an olefin feed inlet (11), a synthesis gas feed inlet (12), a solvent feed inlet (13) and a catalyst feed inlet (14); The hydroformylation method includes the following steps: Step a: The solvent is introduced into the vessel body (1) of the device through the solvent inlet (13); under the action of stirring, the solvent is dispersed into the spray grid plate (5) through the holes (31) of the guide vertical cylinder (3) and the action of the first blade (4) to form a liquid phase; Step b: Syngas is introduced into the vessel body (1) of the device through the syngas inlet (12). Syngas in the upper part of the vessel body (1) is introduced into the rotating shaft (2) through the suction port (21) on the rotating shaft (2). Then, the syngas is sprayed out through the small ventilation hole (61) on the second blade (6). The syngas enters the dispersion cylinder (7). The dispersion cylinder (7) cuts and disperses the discharged syngas in multiple stages and makes the syngas enter the spray grid plate (5). The syngas comes into contact with the liquid phase obtained in step a and undergoes the first mixing to obtain a mixed liquid. Step c: The catalyst is introduced into the vessel body (1) of the device through the catalyst inlet (14); under the action of stirring, the catalyst is dispersed into the spray grid plate (5) through the holes (31) of the guide vertical cylinder (3) and the action of the first blade (4), and comes into contact with the mixed liquid obtained in step b and undergoes a second mixing to obtain a catalyst-containing mixed liquid; Step d: The olefins are introduced into the vessel body (1) of the device through the olefin inlet (11); under the action of stirring, the olefins are dispersed into the spray grid plate (5) through the holes (31) of the guide vertical cylinder (3) and the action of the first blade (4), and come into contact with the catalyst-containing mixed liquid obtained in step c and react. The reaction temperature is 60-140℃; the reaction pressure is 0-20MPa. The first mixing time is 1-30 min; the second mixing time is 0.1-20 min.

2. The method of claim 1, wherein, The bottom of the reactor body is provided with a discharge port (15) for discharging reaction products.

3. The method according to claim 1 or 2, characterized in that, The sidewall of the spray grid plate (5) is provided with spray holes (51) for cutting and dispersing the reaction materials.

4. The method according to claim 1 or 2, characterized in that, The top of the rotating shaft (2) is connected to the transmission component (8), which provides kinetic energy to make the rotating shaft (2) rotate.

5. The method according to claim 1 or 2, characterized in that, The vessel body (1) is provided with a heat exchange jacket (16) on the outside.

6. The method of claim 1 or 2, wherein, The reaction temperature is 70-100℃; and / or the reaction pressure is 1-7MPa.

7. The method of claim 1 or 2, wherein, The first mixing time is 15-25 min; and / or, the second mixing time is 1-10 min.

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