Transesterification reaction device

Abstract

The invention discloses an ester exchange reaction device, and belongs to the technical field of chemical reaction devices. The invention discloses a reactor of an ester exchange reaction device. The reactor comprises a reactor, the reactor comprises a shell and an entrainer distributor for spraying an entrainer into the reactor, and the entrainer distributor is mounted in the shell; one side, close to the shell, of the entrainer distributor is communicated with an entrainer feeding hole, one end, far away from the entrainer distributor, of the entrainer feeding hole penetrates through the shell, extends to the outer side of the shell and is connected with a pipeline for conveying the entrainer, and the entrainer enters the entrainer distributor from the entrainer feeding hole through the pipeline and is sprayed into the reactor from the entrainer distributor.

Description

Technical Field

[0001] The invention relates to an ester exchange reaction device. Background Art

[0002] Transesterification is the process of generating new esters by mixing one ester with another fatty acid, alcohol, or itself and other esters, accompanied by carboxyl exchange or molecular rearrangement. This type of reaction plays an important role in changing the fatty acid and glyceride composition and structure of oils and fats, and can produce oils with completely new structures that natural oils and fats do not have. It is one of the important means of oil modification in the oil industry. In particular, in the process of preparing biodiesel, transesterification (also known as alcoholysis) refers to the use of triglycerides in animal and plant oils and microbial oils to exchange ester groups with low-carbon alcohols under the action of a catalyst, which can change the oil properties without chemically changing the fatty acid composition.

[0003] In the transesterification reaction, macromolecular alcohols are usually replaced by small molecule alcohols to generate new esters and small molecule alcohols. Since the generated small molecule alcohols can be removed by distillation, this helps to drive the reaction in the positive direction. However, due to the reversibility of the transesterification reaction, if the by-products cannot be removed in time, the final conversion rate will be affected. The traditional treatment method is to use reactive distillation. The early processes were mostly intermittent reactions carried out in one kettle and one tower. This intermittent operation has the disadvantages of large fluctuations in materials between batches, increased exhaust emissions due to frequent feeding and discharging, and limited production capacity.

[0004] With the advancement of continuous production, although there are still certain limitations in using a continuous tubular reactor or microreactor alone for transesterification reactions, the industry has developed a continuous reaction system with multiple reactors in series. In such a system, each reactor is equipped with a distillation tower to ensure that by-products can be effectively removed by distillation during the reaction, thereby promoting the reaction to move in the positive direction. Compared with intermittent reactions, this method not only improves the stability of the product, but also increases production capacity. However, this process also faces the challenges of high equipment investment, complex control of operating conditions, and greater difficulty in production operations.

[0005] In order to solve the above problems, the applicant designed an ester exchange reaction device. Summary of the invention

[0006] The purpose of the present invention is to provide an ester exchange reaction device to solve the technical problems mentioned in the above background technology.

[0007] The technical solution for achieving the purpose of the present invention is:

[0008] An ester exchange reaction device comprises a reactor; the reactor comprises a shell and an entrainer distributor for spraying an entrainer into the reactor, the entrainer distributor is installed in the shell; a side of the entrainer distributor close to the shell is connected to an entrainer feed port, an end of the entrainer feed port away from the entrainer distributor passes through the shell and extends to the outside of the shell, and is connected to a pipeline for conveying the entrainer, the entrainer enters the entrainer feed port through the pipeline, and is sprayed into the reactor from the entrainer distributor.

[0009] The ester exchange reaction device of the present invention has an entrainer distributor installed in a reactor, the entrainer distributor is connected with one end of an entrainer feed port, the entrainer enters the entrainer distributor from the entrainer feed port through a pipeline, and is sprayed into the reactor from the entrainer distributor; by installing the entrainer distributor in the reactor, the entrainer is sprayed in the ester exchange reaction process, the entrainer quickly evaporates azeotropically with the by-product alcohol generated by the ester exchange reaction, the by-product alcohol is removed, the esterification reaction is promoted to proceed in the forward direction, the reaction time and reaction efficiency of the esterification reaction are reduced, and the purity of the product is improved. The device has low investment and operation costs, a simplified operation process, and a more stable and easy to control entire production process.

[0010] The entrainer distributor comprises a plurality of pipes, one ends of which converge to the same connection point and are interconnected at the connection point, and the plurality of pipes are evenly distributed circumferentially around the connection point; a plurality of nozzles are evenly spaced on the upper surface of the pipes, and the entrainer is sprayed from the nozzles; one end of the entrainer feed port is connected to the plurality of pipes through the connection point, and the azeotropic liquid is transported to each pipe.

[0011] The present invention arranges a plurality of interconnected pipes with a plurality of nozzles arranged at equal intervals on the upper surface with the connecting point at which they converge being uniformly distributed in the circumferential direction, so that the sprayed entrainer can be more evenly distributed and can fully contact the reaction materials at various positions in the reactor, so that the by-product alcohol in the reaction materials can be fully evaporated by azeotropy.

[0012] A preheating device is provided on the passage of the pipeline for conveying the entrainer to preheat the entrainer in the pipeline.

[0013] The pipeline for conveying the entrainer is provided with a preheating device to preheat the entrainer in the pipeline, so as to ensure that the entrainer is instantly vaporized after entering the reaction system and fully contacts with the by-product alcohol to remove the by-product alcohol in the reaction system by azeotropic evaporation, so that the reaction proceeds in a forward direction and the conversion rate of the reaction is increased. Moreover, the preheated entrainer sprayed into the reaction system does not affect the temperature in the reaction system, thereby ensuring the temperature stability and reaction efficiency in the reaction system.

[0014] A pressurizing conveying device is provided on the passage of the pipeline for conveying the entrainer to pressurize the entrainer in the pipeline.

[0015] The passage of the pipeline for conveying the entrainer of the present invention is provided with a pressurized conveying device, which can convey the entrainer on the one hand, and exert a certain pressure on the entrainer on the other hand to avoid the entrainer vaporizing after preheating and increasing the pipeline pressure to cause safety hazards.

[0016] The transesterification reaction device further comprises an azeotropic distillation tower and a first gas pipeline; one end of the first gas pipeline is connected to the top of the reactor, and the other end of the first gas pipeline is connected to the azeotropic distillation tower.

[0017] The top of the reactor of the present invention is connected to the azeotropic distillation tower through the first gas pipeline. The evaporated materials in the reaction process enter the azeotropic distillation tower through the first gas pipeline for distillation and separation. The materials include azeotropic agent, by-product alcohol and the like.

[0018] The reactor and the azeotropic distillation tower are further connected with a first reflux pipe, and the first reflux pipe refluxes the liquid phase material after distillation and separation in the azeotropic distillation tower to the reaction tower.

[0019] The unreacted raw material ester, raw material alcohol, etc. in the reactor partially evaporate into the distillation tower during the reaction, resulting in a decrease in the utilization rate of the raw materials for the esterification reaction. The reactor and the azeotropic distillation tower of the present invention are also connected to a first reflux pipe, which refluxes the liquid materials such as the raw material ester and raw material alcohol after distillation separation to the reaction tower.

[0020] A temperature compensator is provided at the bottom of the azeotropic distillation tower.

[0021] The azeotropic distillation tower of the present invention is provided with a temperature compensator at the bottom to heat the reflux liquid at the bottom of the tower, reduce the content of by-product alcohol in the reflux liquid, and avoid the by-product alcohol being mixed in the reflux liquid and refluxed into the reactor to affect the forward progress of the transesterification reaction.

[0022] The transesterification reaction device also includes a condenser, and a second gas phase discharge pipe and a second reflux pipe are connected between the azeotropic distillation tower and the condenser.

[0023] The azeotropic distillation tower of the present invention is connected to the condenser via a second gas phase discharge pipe and a second reflux pipe. The azeotropically evaporated entrainer in the azeotropic distillation tower enters the second gas phase discharge pipe from the top of the tower, and enters the condenser through the second gas phase discharge pipe for condensation separation. The separated upper layer entrainer is refluxed to the azeotropic distillation tower via the second reflux pipe.

[0024] The condenser is also provided with a phase-splitting liquid level meter.

[0025] The condenser of the present invention is also provided with a phase-splitting liquid level meter to detect the interface between the two liquid phases in the condenser.

[0026] The ester exchange reaction device also includes a heat exchanger; a second feed pipe and a first discharge pipe are connected between the heat exchanger and the reactor, the first discharge port of the heat exchanger is connected to the feed port of the reactor through the second feed pipe, and the second feed port of the heat exchanger is connected to the discharge port of the reactor through the first discharge pipe.

[0027] The ester exchange reaction device of the present invention is also provided with a heat exchanger, and a second feed pipe and a first discharge pipe are connected between the heat exchanger and the reactor. The raw materials preheated by the heat exchanger enter the reactor through the second feed pipe for reaction, and the materials after the reaction enter the heat exchanger from the first discharge pipe to exchange heat with the raw materials, thereby preheating the raw materials, thereby preventing raw materials with a temperature far lower than that of the materials in the reactor from entering the reactor to affect the temperature stability of the materials in the reactor and the reaction efficiency, and at the same time effectively saving energy.

[0028] A plurality of stirring units are arranged in the reactor, and the stirring units are evenly distributed above the nozzle pipeline of the entrainer distributor to stir and disperse the injected entrainer.

[0029] By adopting the above technical solution, the present invention has the following beneficial effects:

[0030] (1) The ester exchange reaction device of the present invention is provided with an entrainer distributor in the reactor, the entrainer distributor is connected to one end of the azeotropic agent feed port, and the other end of the azeotropic agent feed port is connected to a pipeline for conveying the azeotropic agent outside the reactor shell, wherein a fluid pump is provided on the pipeline for conveying the azeotropic agent, and the fluid pump increases the pressure of the entrainer to a required pressure, and inputs the pressure into the entrainer distributor through the pipeline for conveying the azeotropic agent, and sprays the entrainer from the entrainer distributor into the reactor; by installing the entrainer distributor in the reactor, the entrainer is sprayed into the reactor during the ester exchange reaction, the entrainer quickly evaporates by azeotropy with the by-product alcohol generated by the ester exchange reaction, the by-product alcohol is removed, and the esterification reaction is promoted to proceed in the forward direction, thereby reducing the reaction time of the esterification reaction, improving the reaction efficiency, reducing the occurrence of side reactions, and improving the purity of the product. The investment and operation costs of the device are low, the operation process is simplified, and the entire production process is more stable and easy to control.

[0031] (2) The top of the reactor of the present invention is connected to the azeotropic distillation tower through the first gas pipeline. The evaporated materials in the reaction process enter the azeotropic distillation tower through the first gas pipeline for distillation and separation. The materials include the entrainer, by-product alcohol and a small amount of raw materials.

[0032] (3) The reactor and the azeotropic distillation tower of the present invention are also connected to a first reflux pipe, and the first reflux pipe refluxes the liquid phase materials after distillation and separation in the azeotropic distillation tower to the reaction tower; the unreacted raw material ester, raw material alcohol, etc. in the reactor partially evaporate and enter the distillation tower during the reaction process, resulting in a decrease in the utilization rate of the raw materials for the esterification reaction. The reactor and the azeotropic distillation tower of the present invention are also connected to a first reflux pipe, and the first reflux pipe refluxes the liquid phase materials such as the raw material ester, raw material alcohol, etc. after distillation and separation to the reaction tower.

[0033] (4) A temperature compensator is provided at the bottom of the azeotropic distillation tower of the present invention to heat the reflux liquid at the bottom of the tower, thereby reducing the content of by-product alcohol in the reflux liquid and preventing the by-product alcohol from being mixed in the reflux liquid and refluxed into the reactor, thereby affecting the forward progress of the transesterification reaction.

[0034] (5) The azeotropic distillation tower of the present invention is connected to the condenser via a second gas phase discharge pipe and a second reflux pipe. The azeotropically evaporated entrainer in the azeotropic distillation tower enters the second gas phase discharge pipe from the top of the tower, and enters the condenser through the second gas phase discharge pipe for condensation and stratification. The upper entrainer phase after stratification is refluxed to the azeotropic distillation tower through the second reflux pipe, azeotropes with the by-product alcohol in the distillation tower, breaks the azeotropic system of the raw material ester and the by-product alcohol, ensures that no raw material ester enters the condenser from the top of the distillation tower, and the lower alcohol phase is extracted from the reaction system. This process effectively reduces the return of the by-product alcohol to the reaction system, improves the reaction efficiency and reduces energy consumption.

[0035] (6) The ester exchange reaction device of the present invention is also provided with a heat exchanger, and a second feed pipe and a first discharge pipe are connected between the heat exchanger and the reactor. The raw materials preheated by the heat exchanger enter the reactor through the second feed pipe for reaction, and the materials after the reaction enter the heat exchanger from the first discharge pipe to exchange heat with the raw materials, and the energy of the materials after the reaction is recovered and utilized to preheat the raw materials, so as to avoid raw materials with a temperature far lower than that of the materials in the reactor from entering the reactor to affect the temperature stability and reaction efficiency of the materials in the reactor, so as to make the mixing and dissolution between the raw materials more complete, and at the same time effectively save energy.

[0036] (7) The present invention arranges a plurality of interconnected pipes with a plurality of nozzles arranged at equal intervals on the upper surface, and the pipes are evenly distributed in the circumferential direction with the connecting point at which the pipes converge as the center, so that the sprayed entrainer can be more evenly distributed and can fully contact the reaction materials at various positions in the reactor, so that the by-product alcohol in the reaction materials can fully evaporate by azeotropy.

[0037] (8) The pipeline for conveying the entrainer of the present invention is provided with a preheating device to preheat the entrainer in the pipeline, thereby ensuring that the entrainer is instantly vaporized after entering the reaction system and fully contacts with the by-product alcohol to remove the by-product alcohol in the reaction system by azeotropic evaporation, so that the reaction proceeds in the forward direction and the conversion rate of the reaction is increased. In addition, the injection of the preheated entrainer into the reaction system does not affect the temperature in the reaction system, thereby ensuring the temperature stability and reaction efficiency in the reaction system.

[0038] (9) The passage of the pipeline for conveying the entrainer of the present invention is provided with a pressurized conveying device, which can convey the entrainer on the one hand, and exert a certain pressure on the entrainer on the other hand to avoid the entrainer vaporizing after preheating and increasing the pipeline pressure to cause safety hazards.

[0039] (10) The condenser of the present invention is also provided with a phase-separation liquid level meter to detect the interface between the two liquid phases in the condenser. BRIEF DESCRIPTION OF THE DRAWINGS

[0040] In order to make the content of the present invention more clearly understood, the present invention is further described in detail below according to specific embodiments and in conjunction with the accompanying drawings, wherein

[0041] Figure 1 The present invention is a schematic structural diagram of an ester exchange reaction device according to an embodiment of the present invention.

[0042] Figure 2 FIG. 1 is a top view of a reactor according to an embodiment of the present invention.

[0043] Figure 3 The figure is a schematic structural diagram of an azeotropic agent distributor according to an embodiment of the present invention.

[0044] The reference numerals in the accompanying drawings are: reactor 10, stirrer 11, entrainer distributor 12, partition 13, entrainer feed port 14, stirring motor 15; pipeline 12-1, connection point 12-3, nozzle 12-2;

[0045] Heat exchanger 20, first feed pipe 21, second feed pipe 22, first discharge pipe 23, second discharge pipe 24;

[0046] Azeotropic distillation tower 30, temperature compensator 31, first reflux pipe 32, temperature compensator exhaust valve 33, first gas phase pipeline 34, inhibitor feed port 35, second gas phase discharge pipe 36;

[0047] Condenser 40 , condensed water inlet 42 , condensed water outlet 41 , phase-separation liquid level meter 43 , second reflux pipe 45 , condenser discharge pipe 44 . DETAILED DESCRIPTION

[0048] In order to better understand the above technical solution, the above technical solution will be described in detail below in conjunction with the accompanying drawings and specific implementation methods.

[0049] In order to make the purpose, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are part of the embodiments of the present invention, not all of the embodiments. Generally, the components of the embodiments of the present invention described and shown in the drawings here can be arranged and designed in various different configurations.

[0050] Therefore, the following detailed description of the embodiments of the present invention provided in the accompanying drawings is not intended to limit the scope of the invention claimed for protection, but merely represents selected embodiments of the present invention. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0051] It should be noted that similar reference numerals and letters denote similar items in the following drawings, and therefore, once an item is defined in one drawing, further definition and explanation thereof is not required in subsequent drawings.

[0052] In the description of the embodiments of the present invention, it should be understood that the terms "center", "up", "down", "left", "right", "vertical", "horizontal", "inside", "outside", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the accompanying drawings, or are the orientations or positional relationships in which the inventive product is conventionally placed when used, or are the orientations or positional relationships conventionally understood by those skilled in the art. They are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as a limitation on the present invention.

[0053] In the description of the embodiments of the present invention, it is also necessary to explain that, unless otherwise clearly specified and limited, the terms "set", "installed", "connected" and "connected" should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral connection; it can be directly connected, or indirectly connected through an intermediate medium, or it can be the internal connection of two components. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances. The present invention is further described below in conjunction with the accompanying drawings. The following embodiments are only used to more clearly illustrate the technical solution of the present invention, and cannot be used to limit the scope of protection of the present invention.

[0054] (Example 1)

[0055] See Figures 1 to 3 , an ester exchange reaction device, comprising a reactor 10, a heat exchanger 20, an azeotropic distillation tower 30, and a condenser 40;

[0056] The reactor 10 includes a shell, in which a plurality of reaction units are arranged, a partition 13 is arranged between two adjacent reaction units, and an entrainer distributor 12 and a stirring unit are arranged at the bottom of each reaction unit; the stirring unit includes a stirring paddle 11 and a stirring motor 15 which is transmission-connected to the stirring paddle 11, and the stirring motor drives the stirring paddle 11 to stir; the stirring units are evenly distributed above the nozzle pipeline of the entrainer distributor 12 to stir and disperse the injected entrainer.

[0057] The entrainer distributor 12 includes a plurality of pipes 12-1, one end of which converges to the same connection point 12-3 and is interconnected at the connection point 12-3. The plurality of pipes 12-1 are evenly distributed circumferentially around the connection point 12-3 to form a cross-shaped structure. A plurality of nozzles 12-2 are evenly spaced on the upper surface of the pipe 12-1, and the entrainer is sprayed from the nozzles.

[0058] The side of the connection point of the entrainer distributor 12 close to the bottom of the shell is connected to an entrainer feed port 14, and the end of the entrainer feed port 14 away from the entrainer distributor 12 extends through the shell to the outside of the shell and is connected to the pipeline for conveying the entrainer; a preheating device and a pressurized conveying device are provided on the passage of the pipeline for conveying the entrainer; the pressurized conveying device pressurizes the entrainer and conveys it to the entrainer distributor 12, where it flows through the preheating device during conveyance and then enters the entrainer feed port 14 for preheating, and conveys the azeotropic liquid to each pipeline 12-1 through the connection point 12-3, and is sprayed into the reactor from the nozzle on the pipeline.

[0059] The reactor 10 and the azeotropic distillation tower 30 are connected by a first gas pipeline 34 and a first reflux pipe 32; one end of the first gas pipeline 34 is connected to the top of the reactor 10, and the other end of the first gas pipeline 34 is connected to the azeotropic distillation tower 30. The evaporated material in the reaction process enters the azeotropic distillation tower through the first gas pipeline for distillation and separation; one end of the first reflux pipe 32 is connected to the bottom of the azeotropic distillation tower 30, and the other end of the first reflux pipe 32 is connected to the reactor 10. The first reflux pipe 32 refluxes the liquid phase material after distillation and separation in the azeotropic distillation tower 30 to the reaction tower;

[0060] A temperature compensator 31 is provided at the bottom of the azeotropic distillation tower 30. The temperature compensator 31 is heated to raise the temperature of the bottom of the azeotropic distillation tower 30 to 100° C., and the reflux liquid at the bottom of the tower is heated to reduce the by-product alcohol content in the reflux liquid from 0.8% to below 0.1%;

[0061] A temperature compensator drain valve 33 is provided at the bottom of the temperature compensator 31 .

[0062] The azeotropic distillation tower 30 is also provided with an inhibitor feed port 35 for adding the inhibitor to prevent some unsaturated raw alcohols and unsaturated raw esters from self-polymerizing after entering the azeotropic distillation tower 30 together with the entrainer, thereby affecting the utilization rate of the raw materials.

[0063] A second gas phase discharge pipe 36 and a second reflux pipe 45 are connected between the azeotropic distillation tower 30 and the condenser 40. One end of the second gas phase discharge pipe 36 is connected to the top of the azeotropic distillation tower 30, and the other end of the second gas phase discharge pipe 36 is connected to the top of the condenser 40. The azeotropic gas in the azeotropic distillation tower 30 enters the condensation tower for condensation and separation through the second gas phase discharge pipe; one end of the second reflux pipe 45 is connected to the condenser 40, and the other end of the second reflux pipe 45 is connected to the azeotropic distillation tower 30, and the separated upper layer entrainer is refluxed to the azeotropic distillation tower through the second reflux pipe.

[0064] The bottom of the condenser 40 is connected to a condenser discharge pipe 44 for discharging the lower layer liquid.

[0065] The condenser 40 is provided with a phase-splitting liquid level meter 43 , and the condenser 40 has a condensate water inlet 42 and a condensate water outlet 41 , wherein the condensate water inlet 42 is arranged below the condensate water outlet 41 .

[0066] A second feed pipe 22 and a first discharge pipe 23 are connected between the heat exchanger 20 and the reactor 10. The first discharge port of the heat exchanger is connected to the feed port of the reactor through the second feed pipe 22, and the second feed port of the heat exchanger is connected to the discharge port of the reactor through the first discharge pipe 23. The reacted material enters the heat exchanger from the first discharge pipe to exchange heat with the raw material, and the raw material is preheated to prevent raw material with a temperature far lower than that of the material in the reactor from entering the reactor and affecting the temperature stability of the material in the reactor.

[0067] The heat exchanger 20 is also connected to a first feed pipe 21 for feeding and a second discharge pipe 24 for discharging.

[0068] For ease of understanding, the operation process of the ester exchange reaction device of this embodiment will be described below in conjunction with an ester exchange reaction:

[0069] The raw material ester of the transesterification reaction is methyl methacrylate, and the raw material alcohol is dimethylethanolamine. The reaction mechanism of the transesterification reaction is as follows:

[0070]

[0071] The specific process is as follows: methyl methacrylate, dimethylethanolamine, catalyst dibutyltin dilaurate, and inhibitor phenothiazine are respectively fed into the heat exchanger through the first feed pipe 21 at 1450 kg / h, 900 kg / h, 36 kg / h, and 2.0 kg / h, and then fed into the reactor 10 through the second feed pipe 22 for reaction. The reaction temperature is controlled at 100-123° C. During the reaction, the pressurized conveying device pressurizes the entrainer n-hexane to 0.05-0.3 MPa and flows through the preheating device to be preheated to 90° C. and then transported to the entrainer distributor 12, and sprayed into the reactor 1 from the nozzle 12-2 of the azeotropic distributor 12 at 700 kg / h. 0, the entrainer enters the reactor and contacts fully with the materials in the reactor, and forms an azeotropic mixture with the by-product methanol. The azeotropic mixture with a low boiling point is azeotropically evaporated at the reaction temperature and enters the azeotropic distillation tower 30 for azeotropic separation through the first gas phase pipeline 34. The separated raw ester enters the reactor through the first reflux pipe 32 to participate in the reaction. The azeotropic mixture composed of the separated entrainer and the by-product alcohol enters the condenser 40 from the top of the distillation tower through the second gas phase discharge pipe 36 to condense and separate the entrainer and the by-product alcohol. The separated entrainer enters the azeotropic distillation tower through the second reflux pipe 45 to continue azeotropic separation. The separated by-product alcohol is discharged through the condenser discharge pipe 44.

[0072] The preheating device of this embodiment adopts a shell-and-tube heat exchanger, and steam is introduced into the shell-and-tube heat exchanger to preheat the entrainer;

[0073] The pressurized delivery device of this embodiment adopts a pump.

[0074] After the continuous reaction is carried out for 6 hours, the reacted material is discharged from the first discharge pipe 23 and enters the heat exchanger 20 to exchange heat with the raw material and then discharged from the second discharge pipe 24.

[0075] The specific embodiments described above further illustrate the objectives, technical solutions and beneficial effects of the present invention in detail. It should be understood that the above description is only a specific embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention should be included in the protection scope of the present invention.

Claims

1. A transesterification reaction device, characterized in that: The invention comprises a reactor (10); the reactor (10) comprises a shell, an entrainer distributor (12) for spraying an entrainer into the reactor, and the entrainer distributor (12) is installed in the shell; a side of the entrainer distributor (12) close to the shell is connected to an entrainer feed port (14), an end of the entrainer feed port (14) away from the entrainer distributor (12) passes through the shell and extends to the outside of the shell, and is connected to a pipeline for conveying the entrainer; the entrainer enters the entrainer distributor (12) from the entrainer feed port (14) through the pipeline, and is sprayed from the entrainer distributor (12) into the reactor (10).

2. The transesterification reaction device according to claim 1, characterized in that: The entrainer distributor (12) comprises a plurality of pipes (12-1), one end of the plurality of pipes (12-1) converges to a common connection point (12-3) and is interconnected at the connection point (12-3), and the plurality of pipes (12-1) are evenly distributed in the circumferential direction with the connection point (12-3) as the center; a plurality of nozzles (12-2) are evenly spaced on the upper surface of the pipe (12-1), and the entrainer is sprayed from the nozzles; one end of the entrainer feed port (14) is connected to the plurality of pipes (12-1) through the connection point (12-3), and the azeotropic liquid is transported to each pipe (12-1).

3. The transesterification reaction device according to claim 1, characterized in that: A preheating device is provided on the passage of the pipeline for conveying the entrainer to preheat the entrainer in the pipeline.

4. The transesterification reaction device according to claim 1, characterized in that: A pressurizing conveying device is provided on the passage of the pipeline for conveying the entrainer to pressurize the entrainer in the pipeline.

5. The transesterification reaction device according to claim 1, characterized in that: The transesterification reaction device further comprises an azeotropic distillation tower (30) and a first gas pipeline (34); one end of the first gas pipeline (34) is connected to the top of the reactor (10), and the other end of the first gas pipeline (34) is connected to the azeotropic distillation tower (30); the reactor (10) and the azeotropic distillation tower (30) are also connected to a first reflux pipe (32), and the first reflux pipe (32) refluxes the liquid phase material after distillation and separation in the azeotropic distillation tower (30) to the reaction tower.

6. The transesterification reaction device according to claim 5, characterized in that: A temperature compensator (31) is provided at the bottom of the azeotropic distillation tower (30).

7. The transesterification reaction device according to claim 5, characterized in that: The transesterification reaction device further comprises a condenser (40), and a second gas phase discharge pipe (36) and a second reflux pipe (45) are connected between the azeotropic distillation tower (30) and the condenser (40).

8. The transesterification reaction device according to claim 7, characterized in that: The condenser (40) is also provided with a phase-separation liquid level meter (43).

9. The transesterification reaction device according to claim 1, characterized in that: The transesterification reaction device further comprises a heat exchanger (20); a second feed pipe (22) and a first discharge pipe (23) are connected between the heat exchanger (20) and the reactor (10); the first discharge port of the heat exchanger is connected to the feed port of the reactor via the second feed pipe (22), and the second feed port of the heat exchanger is connected to the discharge port of the reactor via the first discharge pipe.

10. The transesterification reaction device according to claim 1, characterized in that: A plurality of stirring units are arranged in the reactor, and the stirring units are evenly distributed above the nozzle pipeline of the entrainer distributor to stir and disperse the injected entrainer.

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