Production system of perfluoro-4-methyl-2-pentene

Abstract

The utility model discloses a production system of perfluoro-4-methyl-2-pentene, which belongs to the technical field of perfluorohexanone production equipment and comprises a raw material tank for storing hexafluoropropylene, at least one tubular fixed bed reactor, at least one tubular fixed bed reactor and a product liquid storage tank, the raw material tank is connected with a feed port of the first-stage tubular fixed bed reactor through a pipeline I, a discharge port of the last-stage tubular fixed bed reactor is connected with a feed port of the first-stage tubular fixed bed reactor through a pipeline II, and a discharge port of the last-stage tubular fixed bed reactor is connected with the product liquid storage tank through a pipeline III; a plurality of reaction tubes are arranged in the tubular fixed bed reactor and the tubular fixed bed reactor, catalyst fixing mechanisms are arranged in the reaction tubes, and the system can obviously improve the utilization efficiency of a catalyst, reduce the amount of the catalyst entering a rear-end workshop section, obviously improve the reaction rate and reduce the production cost.

Description

Technical Field

[0001] The utility model belongs to the technical field of perfluorohexanone production equipment, and specifically relates to a production system of perfluoro-4-methyl-2-pentene. Background Art

[0002] In the prior art, perfluorohexanone is synthesized using hexafluoropropylene as a raw material, generally comprising four stages: hexafluoropropylene oligomerization, isomerization, epoxidation, and ketonization. The oligomerization and isomerization stages are intended to produce the intermediate perfluoro-4-methyl-2-pentene. To increase the reaction rates in the oligomerization and isomerization stages, a catalyst, such as a fluorine-containing catalyst, is generally added during the reaction. However, in specific implementations, it was discovered that the catalyst utilization efficiency in perfluoro-4-methyl-2-pentene production systems was insufficient, and a certain amount of catalyst entered the next stage along with the material, resulting in a high catalyst loss rate and increasing the difficulty of distilling the product liquid in subsequent stages.

[0003] Therefore, technical personnel in this industry are still exploring and further optimizing the existing perfluorohexanone production system to solve the above technical problems. Utility Model Content

[0004] The utility model aims to solve the above-mentioned technical problems and proposes a production system for perfluoro-4-methyl-2-pentene. The production system can significantly improve the utilization efficiency of the catalyst and reduce the amount of catalyst entering the back-end section. In the production system, the contact area between the catalyst and the reaction raw materials can be increased, thereby significantly improving the reaction rate.

[0005] In order to achieve the above-mentioned purpose of the invention, the technical solution of the present utility model is as follows:

[0006] A perfluoro-4-methyl-2-pentene production system includes a raw material tank for storing hexafluoropropylene, at least one tubular fixed bed reactor, at least one tubular fixed bed reactor, and a product liquid storage tank. The raw material tank is connected to the feed port of the first-stage tubular fixed bed reactor via pipeline I, the discharge port of the last-stage tubular fixed bed reactor is connected to the feed port of the first-stage tubular fixed bed reactor via pipeline II, and the discharge port of the last-stage tubular fixed bed reactor is connected to the product liquid storage tank via pipeline III.

[0007] The shell-and-tube fixed-bed reactor and the tubular fixed-bed reactor are both provided with a plurality of reaction tubes, each of which is equipped with a catalyst fixing mechanism. The catalyst fixing mechanism includes a main fixing frame in a double helical shape, a plurality of brackets for fixing the catalyst are connected between the two main fixing frames, and a plurality of guide bars are provided on the main fixing frame.

[0008] Furthermore, the distal ends of the guide branches face outwards; and the guide branches are evenly distributed.

[0009] Furthermore, adjacent guide branches are arranged in a staggered manner, and the guide branches are welded to the main fixing frame, or the guide branches are connected to the main fixing frame through a threaded structure.

[0010] Furthermore, the support is a mesh or oblique strip structure; the distance between adjacent guide strips is 2 to 8 mm.

[0011] Furthermore, the inner diameter of the reaction tube is set to 30-50 mm, and the guide bar is in contact with the inner wall of the reaction tube.

[0012] Furthermore, the shell and tube fixed bed reactor also includes a shell, with a feed port I provided at the top of the shell; and a discharge port I provided at the bottom. The upper and lower ends of the reaction tube are fixed in the shell through an upper tube plate and a lower tube plate, respectively. A chamber for passing the medium is formed between the shell and the reaction tube, the upper tube plate and the lower tube plate. An inlet communicating with the chamber is provided at the lower part of the shell; and an outlet communicating with the chamber is provided at the upper part of the shell.

[0013] Furthermore, a pressure sensor I and a temperature sensor I are provided on the side of the shell near the feed port I; a pressure sensor II, a temperature sensor II and a liquid level sensor are provided on the side of the shell near the discharge port I.

[0014] Furthermore, the tubular fixed bed reactor includes a tubular body, in which multiple reaction tubes are connected in series through pipelines, the first reaction tube is connected to the feed port II of the tubular body, and the tail of the last reaction tube is connected to the discharge port II of the tubular body.

[0015] Furthermore, a plurality of temperature sensors III are provided on the tubular body; the temperature sensors III are distributed in the first section, the middle section and the tail section of the tubular body.

[0016] Furthermore, a preheater is provided on the pipeline I, and a hexafluoropropylene flowmeter is provided on the pipeline I at the front end of the preheater; and a dimer flowmeter is provided on the pipeline II.

[0017] Beneficial effects of the utility model:

[0018] 1. This utility model proposes a perfluoro-4-methyl-2-pentene production system. This system utilizes novel tubular fixed-bed reactors and tubular fixed-bed reactors, which uniformly load the catalyst and increase the contact area between the catalyst and reactants, thereby improving catalyst utilization and the reaction rate. Furthermore, this system reduces the amount of catalyst entering the back-end process, lowering the processing complexity in these processes (such as the distillation process), improving product purity, and reducing production costs. The perfluoro-4-methyl-2-pentene production system produces a relatively pure perfluoro-4-methyl-2-pentene intermediate, providing an excellent raw material base for the back-end epoxidation and ketonization reactions used to synthesize perfluorohexanone, reducing production complexity and costs, and ultimately improving the quality of perfluorohexanone.

[0019] Second, in the present invention, the distal ends of the diversion branches face outward, facilitating timely transfer of product liquid. Preferably, the diversion branches are evenly distributed. Adjacent diversion branches are staggered for optimal diversion. The diversion branches can be welded to the main mounting frame or connected to the main mounting frame via a threaded structure.

[0020] In this utility model, the bracket serves as the catalyst holder. It can be designed as a mesh or diagonal strip structure, depending on the needs, to facilitate catalyst retention and leave sufficient space for the feed gas to pass through. In actual production, it can be designed as a removable small module fixed to the main bracket, depending on the actual production scale, to facilitate catalyst loading. A single main bracket can accommodate a varying number of small modules as needed. The spacing between adjacent guide strips is preferably 2-8 mm.

[0021] 4. In the present invention, the inner diameter of the reaction tube is set to 30~50mm, and the guide branch is in contact with the inner wall of the reaction tube, so that the generated product liquid can be discharged out of the device along the guide branch and the inner wall of the reaction tube. After the main product is transferred in time, it can be prevented from participating in other reactions and producing other by-products.

[0022] 5. This utility model proposes a superior structure of a tubular fixed-bed reactor for use in the perfluoro-4-methyl-2-pentene intermediate generation stage (polymerization reaction) of the perfluorohexanone synthesis process. A medium-permeable chamber is formed between the shell, reaction tubes, upper tube sheet, and lower tube sheet. Heat transfer oil can be introduced into the chamber to heat and insulate the materials in the reaction tubes. The materials passing through the reaction tubes react under the action of a catalyst. The catalyst fixing mechanism in the reaction tubes is loaded with a fluorine-containing catalyst. Its double-helical main fixing frame and bracket structure effectively increase the contact area between the catalyst and the reactants. This structure also provides sufficient space for the feed gas to pass smoothly, improving reaction efficiency. Furthermore, multiple reaction tubes are connected in parallel and evenly distributed within the shell, resulting in a large heat exchange area and excellent insulation, which is conducive to obtaining a stable product liquid.

[0023] 6. In the present invention, a shell and tube fixed bed reactor is provided with a pressure sensor I and a temperature sensor I on the side of the shell near the feed port I, which can monitor the pressure and temperature of the upper part of the reactor (i.e., the feed port); a pressure sensor II and a temperature sensor II are provided on the lower part of the shell near the discharge port I, which are used to monitor the pressure and temperature of the lower part of the shell, to assist in judging the reaction situation and to ensure safe and stable operation of the equipment. The liquid level sensor provided on the reactor is used to assist in controlling the discharge rate.

[0024] 7. In the present invention, a superior tubular fixed-bed reactor is used in the production system for the perfluoro-4-methyl-2-pentene intermediate generation section (isomerization reaction) in the perfluorohexanone synthesis process. A plurality of reaction tubes are connected in series in the tubular body through pipes, which can significantly extend the residence time of the reactants in the tubular body and improve the reaction efficiency.

[0025] 8. In the present invention, a plurality of temperature sensors III are provided on the tubular body; the temperature sensors III are distributed in the first section, middle section and tail section of the tubular body to monitor the temperature of each point in the tubular fixed bed reactor to ensure normal and stable reaction.

[0026] 9. In the present invention, a preheater is provided on pipeline I to preheat the reaction materials. A hexafluoropropylene flowmeter is provided on pipeline I at the front end of the preheater to monitor the flow of hexafluoropropylene flowing through pipeline I; a dimer flowmeter is provided on pipeline II to monitor the amount of material flowing through pipeline II, control the material delivery rate in the entire system, and ensure the reaction effect. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] Figure 1 It is a structural diagram of the production system in the utility model.

[0028] Figure 2 It is a schematic diagram of the structure of a reaction tube with a built-in catalyst fixing mechanism.

[0029] Figure 3 It is a structural schematic diagram of a shell-and-tube fixed bed reactor.

[0030] Figure 4 It is a structural schematic diagram of another preferred embodiment of a shell and tube fixed bed reactor.

[0031] Figure 5 It is a structural schematic diagram of a tubular fixed bed reactor.

[0032] Figure 6 It is a structural schematic diagram of another preferred embodiment of a tubular fixed bed reactor.

[0033] Figure 7 It is a structural diagram of another preferred embodiment of the production system in the present utility model.

[0034] Figure 8 It is a structural diagram of another preferred embodiment of the production system in the present utility model.

[0035] Among them, 1. Raw material tank; 2. Shell and tube fixed bed reactor; 3. Tubular fixed bed reactor; 4. Product liquid storage tank; 5. Pipeline I; 6. Pipeline II; 7. Pipeline III; 8. Reaction tube; 9. Catalyst fixing mechanism; 10. Main fixing frame; 11. Bracket; 12. Guide branch; 13. Pressure sensor I; 14. Temperature sensor I; 15. Pressure sensor II; 16. Temperature sensor II; 17. Liquid level sensor; 18. Temperature sensor III; 19. Preheater; 20. Hexafluoropropylene flowmeter; 21. Dimer flowmeter; 22. Feed pump; 2.1. Shell; 2.2. Upper tube sheet; 2.3. Lower tube sheet; 2.4. Chamber; 3.1. Tubular body; 2.1.1. Feed port I; 2.1.2. Discharge port I; 2.1.3. Inlet; 2.1.4. Outlet; 3.1.1. Feed port II; 3.1.2. Discharge port II. DETAILED DESCRIPTION

[0036] The present invention will be further described in detail below with reference to the embodiments, but the embodiments of the present invention are not limited thereto.

[0037] Example 1

[0038] A production system of perfluoro-4-methyl-2-pentene belongs to the technical field of hexafluoropropylene isomer production equipment. In this embodiment, a production system designed with a tubular fixed bed reactor 2 and a tubular fixed bed reactor 3 is taken as an example to further illustrate this solution.

[0039] The production system includes a raw material tank 1 for storing hexafluoropropylene, a tubular fixed bed reactor 2, a tubular fixed bed reactor 3 and a product liquid storage tank 4. Figure 1 The raw material tank 1 is connected to the feed port Ⅰ2.1.1 of the shell and tube fixed bed reactor 2 through pipeline Ⅰ5, the discharge port Ⅰ2.1.2 of the shell and tube fixed bed reactor 2 is connected to the feed port Ⅱ3.1.1 of the tubular fixed bed reactor 3 through pipeline Ⅱ6, and the discharge port Ⅱ3.1.2 of the tubular fixed bed reactor 3 is connected to the product liquid storage tank 4 through pipeline Ⅲ7.

[0040] The tubular fixed bed reactor 2 and the tubular fixed bed reactor 3 are both provided with a plurality of reaction tubes 8, each of which is provided with a catalyst fixing mechanism 9. The catalyst fixing mechanism 9 comprises a main fixing frame 10 in a double helical shape, a plurality of brackets 11 for fixing the catalyst are connected between the two main fixing frames 10, a plurality of guide bars 12 are provided on the main fixing frames 10, and the structure of the reaction tube 8 with the catalyst fixing mechanism 9 is shown in FIG. Figure 2 .

[0041] This embodiment is the most basic implementation method. The hexafluoropropylene material in the raw material tank 1 is pumped into the tubular fixed bed reactor 2 through the feed port I 2.1.1. The hexafluoropropylene material enters the reaction tube 8 loaded with a fluorine-containing catalyst and equipped with a catalyst fixing mechanism 9. The temperature in the tubular fixed bed reactor 2 is controlled within a preset value. Under the action of the catalyst, the hexafluoropropylene material reacts to initially produce the target isomeric hexafluoropropylene product liquid. The incompletely reacted material is further fed to the tubular fixed bed reactor 3 for further reaction, ultimately obtaining the target isomeric hexafluoropropylene product liquid. The product liquid is temporarily stored in the product liquid storage tank 4 pending the next step of distillation.

[0042] In actual production, the shell-and-tube fixed bed reactor 2 and the tubular fixed bed reactor 3 can be designed into a system in which multiple stages of shell-and-tube fixed bed reactors 2 and multiple stages of tubular fixed bed reactors 3 are connected in series according to the production scale and process requirements. Of course, in order to ensure the continuous operation of the system, multiple shell-and-tube fixed bed reactors 2 and / or multiple tubular fixed bed reactors 3 can also be connected in parallel in the production system (such as one in use and one in standby, etc.) to ensure continuous and efficient operation of the system.

[0043] Example 2

[0044] This embodiment is a further optimization of embodiment 1. The difference is that Figure 2 The distal ends of the guide branches 12 face outwards; the guide branches 12 are evenly distributed.

[0045] Example 3

[0046] The difference between this embodiment and embodiment 1-2 is that, Figure 2 Adjacent guide branches 12 are staggered, and the guide branches 12 are welded to the main fixing frame 10, or the guide branches 12 are connected to the main fixing frame 10 through a threaded structure.

[0047] Example 4

[0048] The difference between this embodiment and embodiments 1-3 is that the bracket 11 is a mesh or oblique strip structure. Figure 2 , Figure 2 The support 11 in the apparatus is a diagonal strip structure. Adjacent guide bars 12 are preferably spaced 2-8 mm apart. In actual production, the support 11 can be designed as a mesh or diagonal strip structure, forming "small modules" filled with catalyst, for ease of assembly and disassembly. Furthermore, the mesh or diagonal strip structure facilitates catalyst fixation and leaves ample space for the feed gas to pass through.

[0049] Example 5

[0050] Compared with Examples 1-4, the present embodiment differs in that the inner diameter of the reaction tube 8 is preferably set to 30-50 mm, and the guide branch 12 is in contact with the inner wall of the reaction tube 8, that is, the maximum diameter of the catalyst fixing mechanism 9 is preferably the same as the inner diameter of the reaction tube 8.

[0051] Example 6

[0052] The difference between this embodiment and embodiments 1-5 is that the tubular fixed bed reactor 2 further includes a shell 2.1. Figure 3 The shell 2.1 is provided with a feed port I 2.1.1 at the top and a discharge port I 2.1.2 at the bottom. The upper and lower ends of the reaction tube 8 are fixed in the shell 2.1 via an upper tube sheet 2.2 and a lower tube sheet 2.3 respectively. A chamber 2.4 for medium flow is formed between the shell 2.1 and the reaction tube 8, the upper tube sheet 2.2 and the lower tube sheet 2.3. The lower portion of the shell 2.1 is provided with an inlet 2.1.3 communicating with the chamber 2.4; the upper portion of the shell 2.1 is provided with an outlet 2.1.4 communicating with the chamber 2.4.

[0053] During operation, heat transfer oil is added to chamber 2.4 through inlet 2.1.3 to maintain the temperature within the shell-and-tube fixed-bed reactor 2 within a preset range. The heat-exchanged medium is then discharged through outlet 2.1.4. This structure of the shell-and-tube fixed-bed reactor 2 provides a relatively large heat exchange area for the medium, resulting in better thermal insulation.

[0054] Example 7

[0055] The difference between this embodiment and embodiment 1-6 is that, Figure 4 A pressure sensor I 13 and a temperature sensor I 14 are provided on the shell 2.1 near the feed port I 2.1.1; a pressure sensor II 15, a temperature sensor II 16 and a liquid level sensor 17 are provided on the shell 2.1 near the discharge port I 2.1.2.

[0056] Example 8

[0057] The difference between this embodiment and embodiments 1-7 is that the tubular fixed bed reactor 3 includes a tubular body 3.1, Figure 5 , Figure 5 The example shown here shows a structure in which two reaction tubes 8 are connected in series within a tubular body 3.1. The first reaction tube 8 is connected to the feed port II 3.1.1 of the tubular body 3.1, and the tail end of the second reaction tube 8 is connected to the discharge port II 3.1.2 of the tubular body 3.1. In use, this effectively increases the residence time of the reactants in the tubular fixed-bed reactor 3, improving reaction efficiency. This structure can also be used to pass a heat exchange medium through the interlayer between the tubular body 3.1 and the reaction tubes 8, allowing the materials to react under relatively stable temperature conditions.

[0058] Of course, in actual production, multiple reaction tubes 8 can be connected in series through pipelines in the tubular body 3.1 according to actual conditions, with the first reaction tube 8 connected to the feed port II3.1.1 of the tubular body 3.1, and the tail of the last reaction tube 8 connected to the discharge port II3.1.2 of the tubular body 3.1.

[0059] Example 9

[0060] The difference between this embodiment and embodiment 1-8 is that, Figure 6 The tubular body 3.1 is provided with a plurality of temperature sensors III18; the temperature sensors III18 are distributed in the first section, the middle section and the tail section of the tubular body 3.1, and monitor the temperature conditions inside the tubular body 3.1 from multiple locations.

[0061] Example 10

[0062] Compared with Examples 1-9, this embodiment differs in that a preheater 19 is provided on the pipeline I5, a hexafluoropropylene flowmeter 20 is provided on the pipeline I5 at the front end of the preheater 19, and a dimer flowmeter 21 is provided on the pipeline II6.

[0063] In this embodiment, reference Figure 7 A feed pump 22 is installed in pipeline I5. Hexafluoropropylene is delivered to preheater 19 for preheating via feed pump 22. The preheated material is then delivered to tubular fixed-bed reactor 2, where it reacts under the action of the catalyst. A hexafluoropropylene flowmeter 20 monitors the flow rate of the material in pipeline I5, while a dimer flowmeter 21 monitors the flow rate of the material in pipeline II6, facilitating feed rate control.

[0064] Example 11

[0065] In order to facilitate the public to understand the present solution, this embodiment takes a preferred embodiment as an example to further illustrate the present solution. The production system of perfluoro-4-methyl-2-pentene is designed with a tubular fixed bed reactor 2 and a tubular fixed bed reactor 3, and also includes a raw material tank 1 for storing hexafluoropropylene and a product liquid storage tank 4. Figure 8 .

[0066] In this embodiment, the raw material tank 1 is connected to the feed port I2.1.1 of the shell and tube fixed bed reactor 2 through the pipeline I5, the discharge port I2.1.2 of the shell and tube fixed bed reactor 2 is connected to the feed port II3.1.1 of the tubular fixed bed reactor 3 through the pipeline II6, and the discharge port II3.1.2 of the tubular fixed bed reactor 3 is connected to the product liquid storage tank 4 through the pipeline III7. The shell and tube fixed bed reactor 2 and the tubular fixed bed reactor 3 are both provided with a plurality of reaction tubes 8, and the reaction tubes 8 are equipped with a catalyst fixing mechanism 9. The catalyst fixing mechanism 9 includes a main fixing frame 10 in a double helical shape, and a plurality of brackets 11 for fixing the catalyst are connected between the two main fixing frames 10. The main fixing frames 10 are provided with a plurality of guide branches 12.

[0067] In this embodiment, the structure of the reaction tube 8 with the catalyst fixing mechanism 9 is as follows: Figure 2 The distal ends of the guide branches 12 face outwards; the guide branches 12 are evenly distributed. Adjacent guide branches 12 are staggered and welded to the main fixing frame 10, or connected to the main fixing frame 10 via a threaded structure.

[0068] In this embodiment, the bracket 11 is an oblique strip structure; the distance between adjacent guide strips 12 is 4 mm.

[0069] In this embodiment, the inner diameter of the reaction tube 8 is set to 30 mm, and the guide bars 12 are in contact with the inner wall of the reaction tube 8 .

[0070] In this embodiment, the shell-and-tube fixed-bed reactor 2 further comprises a shell 2.1 having a feed port I 2.1.1 at the top and a discharge port I 2.1.2 at the bottom. The upper and lower ends of the reaction tubes 8 are fixed within the shell 2.1 via an upper tube sheet 2.2 and a lower tube sheet 2.3, respectively. A chamber 2.4 for communicating with the medium is formed between the shell 2.1, the reaction tubes 8, the upper tube sheet 2.2, and the lower tube sheet 2.3. An inlet 2.1.3 communicating with the chamber 2.4 is provided at the bottom of the shell 2.1; and an outlet 2.1.4 communicating with the chamber 2.4 is provided at the top of the shell 2.1.

[0071] In this embodiment, a pressure sensor I 13 and a temperature sensor I 14 are provided on the housing 2.1 near the feed port I 2.1.1; a pressure sensor II 15, a temperature sensor II 16 and a liquid level sensor 17 are provided on the housing 2.1 near the discharge port I 2.1.2.

[0072] In this embodiment, the tubular fixed bed reactor 2 includes a tubular body 3.1, in which multiple reaction tubes 8 are connected in series through pipelines. The first reaction tube 8 is connected to the feed port II3.1.1 of the tubular body 3.1, and the tail of the last reaction tube 8 is connected to the discharge port II3.1.2 of the tubular body 3.1.

[0073] In this embodiment, a plurality of temperature sensors III 18 are provided on the tubular body 3.1; the temperature sensors III 18 are distributed in the first section, the middle section and the tail section of the tubular body 3.1.

[0074] In this embodiment, a preheater 19 is provided on the pipeline I5, and a hexafluoropropylene flowmeter 20 is provided on the pipeline I5 at the front end of the preheater 19; a dimer flowmeter 21 is provided on the pipeline II6.

[0075] The perfluoro-4-methyl-2-pentene production system of this embodiment utilizes a specially designed shell-and-tube fixed-bed reactor 2 and a tubular fixed-bed reactor 3. The reaction tubes 8 of these reactors are equipped with a specially designed catalyst retaining mechanism 9, which stably and evenly distributes the fluorine-containing catalyst and increases the contact area between the catalyst and the reactants. Furthermore, the distal ends of the flow guide branches 12 face outward, facilitating timely transfer of the product liquid and improving the synthesis efficiency of the perfluoro-4-methyl-2-pentene intermediate. This reactor also significantly reduces the amount of catalyst entering the back-end process, reducing the processing complexity in these back-end processes (such as the distillation process), improving product purity, and lowering production costs.

Claims

1. A production system for perfluoro-4-methyl-2-pentene, characterized in that: The invention comprises a raw material tank (1) for storing hexafluoropropylene, at least one tubular fixed bed reactor (2), at least one tubular fixed bed reactor (3) and a product liquid storage tank (4), wherein the raw material tank (1) is connected to the feed port of the first-stage tubular fixed bed reactor (2) via a pipeline I (5), the discharge port of the last-stage tubular fixed bed reactor (2) is connected to the feed port of the first-stage tubular fixed bed reactor (3) via a pipeline II (6), and the discharge port of the last-stage tubular fixed bed reactor (3) is connected to the product liquid storage tank (4) via a pipeline III (7). The tubular fixed bed reactor (2) and the tubular fixed bed reactor (3) are both provided with a plurality of reaction tubes (8), each of which is provided with a catalyst fixing mechanism (9), the catalyst fixing mechanism (9) comprising a main fixing frame (10) in a double helical shape, a plurality of brackets (11) for fixing the catalyst being connected between the two main fixing frames (10), and a plurality of guide bars (12) being provided on the main fixing frame (10).

2. A perfluoro-4-methyl-2-pentene production system according to claim 1, characterized in that: The distal ends of the guide branches (12) face outward; the guide branches (12) are evenly distributed.

3. The production system of perfluoro-4-methyl-2-pentene according to claim 1, characterized in that: Adjacent guide branches (12) are arranged in a staggered manner, and the guide branches (12) are welded to the main fixing frame (10), or the guide branches (12) are connected to the main fixing frame (10) via a threaded structure.

4. The production system of perfluoro-4-methyl-2-pentene according to claim 1, characterized in that: The support (11) is a mesh or oblique strip structure; adjacent diversion strips (12) are 2 to 8 mm apart.

5. The production system of perfluoro-4-methyl-2-pentene according to claim 1, characterized in that: The inner diameter of the reaction tube (8) is set to 30-50 mm, and the guide branch (12) is in contact with the inner wall of the reaction tube (8).

6. The production system of perfluoro-4-methyl-2-pentene according to claim 1, characterized in that: The shell-and-tube fixed-bed reactor (2) further comprises a shell (2.1), the top of the shell (2.1) being provided with a feed port I (2.1.1); the bottom being provided with a discharge port I (2.1.2); the upper and lower ends of the reaction tubes (8) being fixed in the shell (2.1) via an upper tube plate (2.2) and a lower tube plate (2.3), respectively; a chamber (2.4) for passing a medium is formed between the shell (2.1), the reaction tubes (8), the upper tube plate (2.2), and the lower tube plate (2.3); an inlet (2.1.3) communicating with the chamber (2.4) is provided at the bottom of the shell (2.1); and an outlet (2.1.4) communicating with the chamber (2.4) is provided at the top of the shell (2.1).

7. A perfluoro-4-methyl-2-pentene production system according to claim 6, characterized in that: A pressure sensor I (13) and a temperature sensor I (14) are provided on the housing (2.1) near the feed port I (2.1.1); a pressure sensor II (15), a temperature sensor II (16) and a liquid level sensor (17) are provided on the housing (2.1) near the discharge port I (2.1.2).

8. The production system of perfluoro-4-methyl-2-pentene according to claim 1, characterized in that: The tubular fixed bed reactor (2) comprises a tubular body (3.1), wherein a plurality of reaction tubes (8) are connected in series via a pipeline in the tubular body (3.1), wherein the first reaction tube (8) is connected to a feed port II (3.1.1) of the tubular body (3.1), and the tail end of the last reaction tube (8) is connected to a discharge port II (3.1.2) of the tubular body (3.1).

9. A perfluoro-4-methyl-2-pentene production system according to claim 8, characterized in that: A plurality of temperature sensors III (18) are provided on the tubular body (3.1); the temperature sensors III (18) are distributed at the first section, the middle section and the tail section of the tubular body (3.1).

10. The production system of perfluoro-4-methyl-2-pentene according to claim 1, characterized in that: The pipeline I (5) is provided with a preheater (19), and the pipeline I (5) at the front end of the preheater (19) is provided with a hexafluoropropylene flowmeter (20); the pipeline II (6) is provided with a dimer flowmeter (21).

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