Method and device for synthesizing 3-chloro-4-oxo-1-pentanol from alpha-acetyl-alpha-chloro-gamma-butyrolactone

Abstract

The invention discloses a method and device for synthesizing 3-chloro-4-oxo-1-pentanol from alpha-acetyl-alpha-chloro-gamma-butyrolactone, and relates to the technical field of organic synthesis.The device comprises an operation table, and a reaction assembly, a receiving assembly, an auxiliary heating assembly and a cooling assembly are all fixedly connected to the top of the operation table; the receiving assembly is fixedly connected to one end, close to the discharge port of the reaction assembly, of the operation table; the auxiliary heating assembly and the cooling assembly are fixedly connected to one end, close to the feed port, of the reaction assembly. According to the scheme, the alpha-acetyl-alpha-chloro-gamma-butyrolactone is used as the raw material, the solid acid is used as the catalyst for hydrolysis to produce the 3-chloro-4-oxo-1-pentanol, the production proportion is high, the added value of the product is greatly improved, the fixed bed is adopted for continuous production, the solid acid catalyst can be continuously used, and the production cost is low. The production capacity of the 3-chloro-4-oxo-1-pentanol is greatly improved, the production cost of the 3-chloro-4-oxo-1-pentanol is reduced, meanwhile, inorganic acid is not used, generation of waste water and waste salt is reduced, and economic benefits and environmental benefits are achieved.

Description

Technical Field

[0001] This invention relates to the field of organic synthesis technology, specifically a method and apparatus for synthesizing 3-chloro-4-oxo-1-pentanol from α-acetyl-α-chloro-γ-butyrolactone. Background Technology

[0002] 3-Chloro-4-oxo-1-pentanol is an important fine chemical intermediate, mainly used in the synthesis of vitamin B1, prothioconazole, and chlormethiazole hydrochloride. Methods for producing 3-chloro-4-oxo-1-pentanol include chlorination of 3-chloro-4-oxo-1-pentane and chlorination of 3-chloro-4-oxo-1-butane, but these methods have some drawbacks, such as harsh reaction conditions, low yield, and environmental pollution. Currently, the main method used is the hydrolysis of α-acetyl-α-chloro-γ-butyrolactone to prepare 3-chloro-4-oxo-1-pentanol.

[0003] The α-acetyl-α-chloro-γ-butyrolactone hydrolysis method uses α-acetyl-α-chloro-γ-butyrolactone as raw material to generate 3-chloro-4-oxo-1-pentanol and carbon dioxide under the action of a catalyst. The α-acetyl-α-chloro-γ-butyrolactone hydrolysis method has a short process, few equipment, low investment, and less waste, and is characterized by high efficiency and safety. However, the hydrolysis of α-acetyl-α-chloro-γ-butyrolactone currently mainly uses inorganic acids such as hydrochloric acid or sulfuric acid as catalysts, which causes significant environmental pollution, severe equipment corrosion, and difficulty in catalyst recovery. At the same time, it generates a large amount of wastewater and waste salt. These wastes not only require additional treatment costs, but also cause serious environmental pollution, which does not meet the requirements of current green chemistry and sustainable development. This leads to increased investment in environmental protection by enterprises, further squeezing profit margins.

[0004] Therefore, those skilled in the art provide a method and apparatus for synthesizing 3-chloro-4-oxo-1-pentanol from α-acetyl-α-chloro-γ-butyrolactone to solve the problems mentioned in the background art. Summary of the Invention

[0005] The purpose of this invention is to provide a method and apparatus for synthesizing 3-chloro-4-oxo-1-pentanol from α-acetyl-α-chloro-γ-butyrolactone, so as to solve the problems mentioned in the background art.

[0006] To address the above problems, the present invention provides the following technical solution: A method for synthesizing 3-chloro-4-oxo-1-pentanol from α-acetyl-α-chloro-γ-butyrolactone, the method comprising the following steps: S1. First, fill the solid acid catalyst into the reaction assembly on the operating table, and connect the feed end of the feed pipe on the fixed bed reactor to the feed end of the storage tank. Connect the oil inlet and water inlet of the reaction assembly to the auxiliary heating assembly and the cooling assembly, respectively. S2. Turn on the cooling component and introduce a certain amount of water into the reaction component. Start the first heater, the second heater and the auxiliary heating component. The first heater heats the heat transfer oil input into the auxiliary heating component. The heat transfer oil circulates in the reaction component and heats the reaction component evenly. At the same time, α-acetyl-α-chloro-γ-butyrolactone is continuously input into the reaction component. Under the action of the catalyst in the reaction component, the hydrolysis reaction takes place. S3. α-Acetyl-α-chloro-γ-butyrolactone is continuously fed into the reaction assembly through the feed pipe for reaction, and the liquid produced by the hydrolysis reaction is collected in the receiving tube. The method for synthesizing chloro-oxy-pentanol from α-acetyl-α-chloro-γ-butyrolactone provided by this invention is implemented using the following components, specifically: The system includes an operating platform. The reaction assembly, receiving assembly, auxiliary heating assembly, and cooling assembly are all fixedly connected to the top of the operating platform. The receiving assembly is fixedly connected to one end of the operating platform near the discharge port of the reaction assembly. The auxiliary heating assembly and cooling assembly are fixedly connected to one end of the reaction assembly near the feed port. The auxiliary heating assembly is also fixedly connected to a control assembly for adjusting the input flow rate of the conveying pipe and the cooling assembly. The top of the reaction assembly is also fixedly connected to a dispensing assembly for uniformly dispersing α-acetyl-α-chloro-γ-butyrolactone within the reaction assembly. The output end of the dispensing assembly extends through and into the reaction assembly. A pressure relief assembly for reducing pressure within the reaction assembly is also fixedly connected to the dispensing assembly.

[0007] Preferably, the reaction assembly includes a fixed-bed reactor, and a reaction cylinder is fixedly connected inside the fixed-bed reactor. A heating chamber is formed between the fixed-bed reactor and the reaction cylinder. The first heater and the second heater are fixedly connected to the outer wall of the fixed-bed reactor near the top and bottom, respectively. A first thermometer for monitoring the temperature inside the reaction cylinder is also fixedly connected to one end of the fixed-bed reactor near the top. Multiple sets of support grids are fixedly connected to the inner wall of the reaction cylinder. Solid acid catalyst is filled between two adjacent sets of support grids. A feed pipe is fixedly connected to one end of the fixed bed reactor near the top. The end of the feed pipe near the fixed bed reactor passes through the fixed bed reactor and the reaction cylinder in sequence and extends into the reaction cylinder. The extended end of the feed pipe is connected to the material distribution component. The end of the conveying pipe near the fixed bed reactor is connected to the feed pipe.

[0008] Preferably, a discharge pipe is also fixedly connected to the fixed bed reactor, and the discharge pipe is located directly below the second heater. One end of the discharge pipe near the fixed bed reactor passes through the fixed bed reactor and the reaction cylinder in sequence and is connected to the reaction cylinder. The other end of the discharge pipe is connected to the receiving component. The receiving assembly includes a receiving cylinder, the inlet end of which is connected to an output pipe, the other end of which is connected to a discharge pipe on a fixed bed reactor, and the outlet end of the receiving cylinder is fixedly connected to a discharge pipe.

[0009] Preferably, the auxiliary heating component includes an oil storage tank and a spiral tube. The oil storage tank is fixedly connected to the end of the operating table away from the receiving component and is located between the fixed bed reactor and the cooling component. The spiral tube is fixedly connected to the heating chamber between the fixed bed reactor and the reaction cylinder. The discharge end of the oil storage tank is connected to an oil delivery pipe, and the other end of the oil delivery pipe passes through the fixed bed reactor and is connected to the spiral tube. The auxiliary heating assembly also includes a preheating box and an oil outlet pipe. The preheating box is fixedly connected to the top of the oil storage tank. One end of the oil outlet pipe near the fixed bed reactor is connected to the discharge end of the spiral tube. The other end of the oil outlet pipe passes through the preheating box and is connected to the oil storage tank. A second thermometer is also fixedly connected to the oil outlet pipe located in the preheating box. The preheating box is also provided with a through hole for the feed pipe to pass through.

[0010] Preferably, the cooling component includes a water tank, a water pump is fixedly connected to the outlet end of the water tank, and a water supply pipe is fixedly connected to the output end of the water pump. The other end of the water supply pipe is fixedly connected to a water inlet, which is fixedly connected to the fixed bed reactor. The end of the water tank near the fixed bed reactor is connected to the heating chamber between the fixed bed reactor and the reaction cylinder. The water tank is also fixedly connected to a water outlet pipe, and the other end of the water outlet pipe is connected to the heating chamber.

[0011] Preferably, the control assembly includes a control box, which is fixedly connected to the oil storage tank. The material conveying pipe and the water conveying pipe are both installed through the control box. A drive motor is fixedly connected inside the control box, and a transmission gear is fixedly connected to the output end of the drive motor. The transmission gear is rotatably connected to the control box. Both ends of the transmission gear are provided with transmission racks, and both sets of transmission racks mesh with the transmission gear. Control plates are fixedly connected to the ends of the two sets of transmission racks that are far apart from each other. The two sets of control plates are respectively installed through adjacent material conveying pipes or water conveying pipes, and sealing gaskets are provided on both sides of the two sets of control plates.

[0012] Preferably, the control plate near the water supply pipe has a first connecting port with the same inner diameter as the water supply pipe, and the control plate near the material supply pipe has a second connecting port with the same inner diameter as the material supply pipe and a third connecting port smaller than the inner diameter of the material supply pipe. A plug rod is fixedly connected to the side wall of the control plate near the water supply pipe. A trigger seat adapted to the plug rod is provided in the inner wall of the control box. The signal output end of the trigger seat is connected to the water pump in the water tank through a wire.

[0013] Preferably, the material distribution assembly includes a servo motor fixedly connected to the fixed bed reactor, the output end of the servo motor is fixedly connected to a transmission rod, and the other end of the transmission rod passes through the fixed bed reactor and extends into the reaction cylinder; The material distribution assembly also includes a connecting box fixedly connected to the inner wall of the reaction cylinder. The feed end of the connecting box is connected to the feed pipe. The bottom of the connecting box is also connected to a material distribution plate. The top of the material distribution plate passes through the connecting box and is fixed to the transmission rod through a connecting shaft. The bottom of the material distribution plate is also provided with multiple material distribution ports.

[0014] Preferably, the material distribution assembly further includes a drive gear fixedly connected to the transmission rod, a synchronous gear is provided on one side of the drive gear, and the drive gear meshes with the synchronous gear, and the pressure relief assembly is rotatably connected to the synchronous gear; The pressure relief assembly includes a pressure relief box, the top of which is fixed to the inner wall of the top of the fixed bed reactor via a connecting shaft. A pressure relief block, which is fixed to a synchronous gear, is rotatably connected inside the pressure relief box. A connecting hole, which communicates with the inside of the reaction cylinder, is opened on the arc surface of the pressure relief box. A connecting groove, which communicates with the connecting hole, is opened inside the pressure relief block. A pressure relief pipe is also fixedly connected to the arc surface of the pressure relief box, and the pressure relief pipe is connected to the connecting hole via the connecting groove. The other end of the pressure relief pipe passes through the top of the fixed bed reactor and extends to the outside of the fixed bed reactor. A pressure relief head is fixedly connected to the extended end of the pressure relief pipe.

[0015] The effects of the above solution are as follows: 1. The method provided by this invention uses α-acetyl-α-chloro-γ-butyrolactone as raw material and a solid acid as catalyst to hydrolyze α-acetyl-α-chloro-γ-butyrolactone to produce 3-chloro-4-oxo-1-pentanol, and the proportion of 3-chloro-4-oxo-1-pentanol produced is higher, which increases the added value of the final product. Under the premise of maintaining a high conversion rate of α-acetyl-α-chloro-γ-butyrolactone and selectivity of 3-chloro-4-oxo-1-pentanol, a fixed bed is used for continuous production, and the solid acid catalyst can be used continuously, which greatly improves the production capacity of 3-chloro-4-oxo-1-pentanol and reduces the production cost of 3-chloro-4-oxo-1-pentanol. At the same time, since inorganic acids are not used, the generation of wastewater and waste salt is reduced, which has significant economic and environmental benefits.

[0016] 2. When using this invention, during the synthesis process, the temperature inside the reaction chamber is monitored in real time by a first thermometer. When the temperature is too high, the drive motor in the control box is started, which drives the transmission gear to rotate, connecting the water supply pipe. The water pump then delivers water from the water tank to the heating chamber to cool the spiral tube and the reaction chamber, thereby reducing the internal temperature of the reaction chamber. At the same time, the control plate adjusts the connection port of the feed pipe to reduce the feed rate, reduce the generation of reaction heat, and further promote cooling. This precise control ensures that the reaction is carried out under suitable conditions, improving product quality and yield.

[0017] 3. In use, during continuous feeding, the servo motor starts and drives the transmission rod to rotate, which in turn drives the distribution plate to rotate, allowing α-acetyl-α-chloro-γ-butyrolactone to fall evenly into the reaction cylinder and react with the catalyst. Simultaneously, the transmission rod drives the drive gear to rotate, which in turn drives the synchronous gear to rotate, thereby causing the pressure relief block in the pressure relief box to rotate. When the two ends of the connecting groove on the pressure relief block are connected to the connecting hole and the pressure relief pipe respectively, the gas in the reaction cylinder can be discharged, reducing the pressure inside the reaction cylinder. Even feeding ensures that the reaction proceeds fully, and reasonable pressure relief avoids the safety hazards caused by excessive pressure inside the reaction cylinder, ensuring the safe and stable operation of the reaction. Attached Figure Description

[0018] Figure 1 This is a flowchart of the process of the present invention; Figure 2 This is a first-view schematic diagram of the present invention; Figure 3 This is a schematic diagram from a second perspective of the present invention; Figure 4 In this invention Figure 3 Enlarged schematic diagram of the structure at point A above; Figure 5 This is a schematic diagram of the structure of the fixed-bed reactor in this invention; Figure 6 This is a schematic diagram of the structure inside the preheating box in this invention; Figure 7 This is a schematic diagram of the internal structure of the control box in this invention; Figure 8 This is a cross-section inside the fixed-bed reactor of the present invention. Figure 1 ; Figure 9 This is a cross-section inside the fixed-bed reactor of the present invention. Figure 2 ; Figure 10 This is a schematic diagram of the pressure relief assembly in this invention; Figure 11 This is a partial structural diagram of the control component in this invention.

[0019] In the diagram: 1. Control panel; 2. Reaction assembly; 21. Fixed-bed reactor; 22. First heater; 23. Second heater; 24. Discharge pipe; 25. First thermometer; 26. Reaction cylinder; 27. Support grid; 28. Feed pipe; 29. ​​Conveying pipe; 3. Receiving assembly; 31. Receiving cylinder; 32. Output pipe; 33. Discharge pipe; 4. Auxiliary heating assembly; 41. Oil storage tank; 42. Oil conveying pipe; 43. Spiral tube; 44. Preheating box; 45. Oil outlet pipe; 46. Second thermometer; 5. Cooling assembly; 51. Water tank; 52. Water conveying pipe; 5 3. Water inlet; 6. Control assembly; 61. Control box; 62. Transmission gear; 63. Transmission rack; 64. Control plate; 65. First connecting port; 66. Second connecting port; 67. Third connecting port; 68. Trigger seat; 69. Insert rod; 7. Material distribution assembly; 71. Servo motor; 72. Transmission rod; 73. Drive gear; 74. Material distribution plate; 75. Material distribution port; 76. Connecting box; 77. Synchronous gear; 8. Pressure relief assembly; 81. Pressure relief box; 82. Pressure relief block; 83. Connecting hole; 84. Connecting groove; 85. Pressure relief pipe; 86. Pressure relief head. Detailed Implementation

[0020] The technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings.

[0021] Example 1, please refer to Figure 1-11 This invention provides a method for synthesizing 3-chloro-4-oxo-1-pentanol from α-acetyl-α-chloro-γ-butyrolactone, the method comprising the following steps: First, a solid acid catalyst is packed between multiple sets of support grids 27, and a certain amount of water is added into the fixed bed reactor 21. Then, α-acetyl-α-chloro-γ-butyrolactone is continuously added into the reaction cylinder 26 through the feed pipe 28 and the conveying pipe 29 to carry out the reaction. The added α-acetyl-α-chloro-γ-butyrolactone reacts with the catalyst. The hydrolysis reaction liquid is transported to the receiving cylinder 31 through the output pipe 32 to receive the obtained reaction liquid. During the reaction, the first heater 22 and the second heater 23 on the fixed bed reactor 21 are started first, and the oil supply pipe 42 is opened. The heat transfer oil in the oil storage tank 41 flows into the spiral tube 43 through the oil supply pipe 42 and flows in a spiral pattern along the spiral tube 43. When the heat transfer oil flows into the spiral tube 43, it absorbs the heat from the first heater 22 and the second heater 23, causing the temperature in the heating chamber to rise until it reaches the predetermined temperature. The heat transfer oil circulates continuously in the spiral tube 43, so that the temperature in the heating chamber remains stable. The heat transfer oil flowing out through the oil outlet pipe 45 flows back to the oil storage tank 41 after passing through the preheating box 44 for cooling. When the heat transfer oil passes through the preheating box 44, the residual heat of the heat transfer oil raises the temperature inside the preheating box 44, which in turn raises the temperature of α-acetyl-α-chloro-γ-butyrolactone in the feed pipe 29 passing through the preheating box 44, thus achieving the preheating effect. During the continuous feeding process, the servo motor 71 starts simultaneously. When the servo motor 71 starts, it drives the transmission rod 72 to rotate. The transmission rod 72 drives the distribution plate 74 to rotate, so that α-acetyl-α-chloro-γ-butyrolactone falls evenly into the reaction cylinder 26 and reacts with the catalyst in the reaction cylinder 26. When the transmission rod 72 rotates, it also drives the drive gear 73 to rotate. When the drive gear 73 rotates one revolution, it drives the synchronous gear 77 to rotate one-quarter revolution. The synchronous gear 77 also drives the pressure relief block 82 in the pressure relief box 81 to rotate. When the two ends of the connecting groove 84 on the pressure relief block 82 rotate to connect with the connecting hole 83 and the pressure relief pipe 85 respectively, the gas in the reaction cylinder 26 can be discharged through the connecting hole 83 and the pressure relief pipe 85, thereby reducing the pressure in the reaction cylinder 26. During the continuous reaction, when the first thermometer 25 detects that the temperature inside the reaction cylinder 26 is too high, the drive motor in the control box 61 starts. The drive motor drives the transmission gear 62 to rotate, causing the two sets of transmission racks 63 to drive the two sets of control plates 64 to move in a direction away from each other. The first connecting port 65 on one of the control plates 64 moves to connect with the water supply pipe 52. At the same time, the water pump starts and transports the water in the water tank 51 to the heating chamber between the fixed bed reactor 21 and the reaction cylinder 26 through the water supply pipe 52. The water flows in the heating chamber to cool the spiral tube 43 and the reaction cylinder 26, thereby reducing the temperature inside the reaction cylinder 26. The second connecting port 66 on another control plate 64 is moved to separate from the feed pipe 29, and the third connecting port 67 is moved to connect with the feed pipe 29. Since the diameter of the third connecting port 67 is smaller than the inner diameter of the feed pipe 29, the feed rate of the feed pipe 29 is reduced, the heat generated in the reaction cylinder 26 is reduced, and the temperature in the reaction cylinder 26 is further reduced. When the temperature inside the reaction cylinder 26 drops to the predetermined temperature, the servo motor starts again, causing the trigger seat 68 to separate from the insertion rod 69, shutting off the water pump. At the same time, the two sets of control boards 64 are reset, shutting off the water supply pipe 52, and the material supply pipe 29 resumes normal feeding rate, continuing the continuous feeding operation.

[0022] Example 2, please refer to Figure 2-11 The present invention also provides an apparatus for synthesizing 3-chloro-4-oxo-1-pentanol from α-acetyl-α-chloro-γ-butyrolactone, comprising an operating table 1, on which a reaction assembly 2, a receiving assembly 3, an auxiliary heating assembly 4, and a cooling assembly 5 are fixedly connected. The receiving assembly 3 is fixedly connected to one end of the operating table 1 near the outlet of the reaction assembly 2. The auxiliary heating assembly 4 and the cooling assembly 5 are fixedly connected to one end of the reaction assembly 2 near the inlet. The auxiliary heating assembly 4 is also fixedly connected to a regulating assembly 6 for adjusting the flow rate of the feed pipe 29 and the cooling assembly 5. The top of the reaction assembly 2 is also fixedly connected to a distributing assembly 7 for uniformly dispersing α-acetyl-α-chloro-γ-butyrolactone within the reaction assembly 2. The output end of the distributing assembly 7 extends through and into the reaction assembly 2. The distributing assembly 7 is also fixedly connected to a pressure relief assembly 8 for depressurizing the reaction assembly 2. Specifically, in use, the fixed acid catalyst is first added to reaction component 2, a certain amount of water is introduced, and the temperature is raised to 40-95℃. Water and α-acetyl-α-chloro-γ-butyrolactone are continuously introduced at a volume hourly space velocity of 0.6-1 h⁻¹. ­-1 Meanwhile, the hydrolysis reaction solution is collected in receiving component 3; During the addition of α-acetyl-α-chloro-γ-butyrolactone, the distribution component 7 can make α-acetyl-α-chloro-γ-butyrolactone evenly distributed in the reaction component 2, so that α-acetyl-α-chloro-γ-butyrolactone can be in complete contact with the catalyst in the reaction component 2. In this stage, the molar ratio of α-acetyl-α-chloro-γ-butyrolactone to water in the mixture was 1:1.6-3.2; By using a fixed-bed device to load solid acid catalysts, continuous production can be achieved, reducing production costs and making it more environmentally friendly. Meanwhile, the solid acid catalyst is an acidic cation exchange resin or catalyst resin, and its active groups are sulfonic acid groups or styrene groups. When water is added to the reaction component 2, the water volume is 1 times that of the resin.

[0023] In this embodiment, the reaction assembly 2 includes a fixed-bed reactor 21, and a reaction cylinder 26 is fixedly connected inside the fixed-bed reactor 21. A heating chamber is formed between the fixed-bed reactor 21 and the reaction cylinder 26. A first heater 22 and a second heater 23 are respectively fixedly connected to the outer walls of the fixed-bed reactor 21 near the top and bottom. A first thermometer 25 for monitoring the temperature inside the reaction cylinder 26 is also fixedly connected to one end of the fixed-bed reactor 21 near the top. Multiple sets of support grids 27 are also fixedly connected to the inner wall of the reaction cylinder 26. Solid acid catalyst is filled between adjacent sets of support grids 27. A feed pipe 28 is also fixedly connected to one end of the fixed-bed reactor 21 near the top. The feed pipe 28 passes through the fixed-bed reactor 21 sequentially. The reactor 21 and the reaction cylinder 26 extend into the reaction cylinder 26, and the extended end of the feed pipe 28 is connected to the distribution component 7. The end of the conveying pipe 29 near the fixed bed reactor 21 is connected to the feed pipe 28. The fixed bed reactor 21 is also fixedly connected to the discharge pipe 24, and the discharge pipe 24 is located directly below the second heater 23. The end of the discharge pipe 24 near the fixed bed reactor 21 passes through the fixed bed reactor 21 and the reaction cylinder 26 in sequence and is connected to the reaction cylinder 26. The other end of the discharge pipe 24 is connected to the receiving component 3. The receiving component 3 includes a receiving cylinder 31. The feed end of the receiving cylinder 31 is connected to the output pipe 32. The other end of the output pipe 32 is connected to the discharge pipe 24 on the fixed bed reactor 21. The discharge end of the receiving cylinder 31 is fixedly connected to the discharge pipe 33. Specifically, in use, the solid acid catalyst is first filled between multiple sets of support grids 27. After filling, a certain amount of water is introduced into the reaction cylinder 26. Then, α-acetyl-α-chloro-γ-butyrolactone is continuously added into the reaction cylinder 26 through the feed pipe 28 and the conveying pipe 29 to carry out the reaction. The added α-acetyl-α-chloro-γ-butyrolactone reacts with the catalyst and flows downward along the multiple support grids 27. The hydrolysis reaction liquid is transported to the receiving cylinder 31 through the output pipe 32. The obtained reaction liquid is then sampled and analyzed. During this process, α-acetyl-α-chloro-γ-butyrolactone enters the resin. Under the action of acidic groups in the solid acid, the ester bond in α-acetyl-α-chloro-γ-butyrolactone accepts a proton and combines with water. After proton transfer, the ester bond breaks and the ring opens. After removing the carboxyl group, 3-chloro-4-oxo-1-pentanol is obtained. At the same time, the removed carboxyl group becomes carbon dioxide and a proton, and then reacts with α-acetyl-α-chloro-γ-butyrolactone again. This invention uses a solid acid catalyst to catalyze the hydrolysis of α-acetyl-α-chloro-γ-butyrolactone to produce 3-chloro-4-oxo-1-pentanol. Compared with liquid inorganic acids, using solid acid as a catalyst requires less water, the post-treatment is simpler, and the wastewater and waste salt generated are greatly reduced. Furthermore, the solid acid catalyst can be reused, resulting in significant economic and environmental benefits.

[0024] In this embodiment, the auxiliary heating component 4 includes an oil storage cylinder 41 and a spiral tube 43. The oil storage cylinder 41 is fixedly connected to the end of the operating table 1 away from the receiving component 3, and the oil storage cylinder 41 is located between the fixed bed reactor 21 and the cooling component 5. The spiral tube 43 is fixedly connected to the heating chamber between the fixed bed reactor 21 and the reaction cylinder 26. The discharge end of the oil storage cylinder 41 is connected to an oil delivery pipe 42. The other end of the oil delivery pipe 42 passes through the fixed bed reactor 21 and is connected to the spiral tube 43. The auxiliary heating component 4 also includes a preheating box 44 and an oil outlet pipe 45. The preheating box 44 is fixedly connected to the top of the oil storage cylinder 41. The end of the oil outlet pipe 45 near the fixed bed reactor 21 is connected to the discharge end of the spiral tube 43. The other end of the oil outlet pipe 45 passes through the preheating box 44 and is connected to the oil storage cylinder 41. A second thermometer 46 is also fixedly connected to the oil outlet pipe 45 located in the preheating box 44. The preheating box 44 is also provided with a through hole for the material delivery pipe 29 to pass through. Specifically, during the reaction, the first heater 22 and the second heater 23 on the fixed bed reactor 21 are first started, and the oil supply pipe 42 is opened. The heat transfer oil in the oil storage tank 41 flows into the spiral tube 43 through the oil supply pipe 42 and flows in a spiral pattern along the spiral tube 43. When the heat transfer oil flows into the spiral tube 43, it absorbs the heat from the first heater 22 and the second heater 23, causing the temperature in the heating chamber to rise until it reaches the predetermined temperature. The heat transfer oil circulates continuously in the spiral tube 43, so that the temperature in the heating chamber remains stable. The heat transfer oil flowing out through the oil outlet pipe 45 flows back to the oil storage tank 41 after passing through the preheating box 44 for cooling. When the heat transfer oil passes through the preheating box 44, the residual heat of the heat transfer oil raises the temperature inside the preheating box 44, which in turn raises the temperature of α-acetyl-α-chloro-γ-butyrolactone in the feed pipe 29 passing through the preheating box 44, thus achieving the preheating effect.

[0025] In this embodiment, the cooling component 5 includes a water tank 51. A water pump is fixedly connected to the outlet end of the water tank 51, and a water pipe 52 is fixedly connected to the output end of the water pump. The other end of the water pipe 52 is fixedly connected to a water inlet 53, which is fixedly connected to the fixed bed reactor 21. The end of the water tank 51 near the fixed bed reactor 21 is connected to the heating chamber between the fixed bed reactor 21 and the reaction cylinder 26. A water outlet pipe is also fixedly connected to the water tank 51, and the other end of the water outlet pipe is connected to the heating chamber. The control component 6 includes a control box 61, which is fixedly connected to the oil storage tank 41. The feed pipe 29 and the water pipe 52 are both installed through the control box 61. A drive motor is fixedly connected inside the control box 61, and a transmission gear 62 is fixedly connected to the output end of the drive motor. The transmission gear 62 is rotatably connected to the control box 61. Both ends of the device are provided with transmission racks 63, and both sets of transmission racks 63 mesh with transmission gears 62. The ends of the two sets of transmission racks 63 that are far apart from each other are respectively fixedly connected to control plates 64. The two sets of control plates 64 are respectively installed through adjacent conveying pipes 29 or water conveying pipes 52, and both sides of the two sets of control plates 64 are provided with sealing gaskets. The control plate 64 near the water conveying pipe 52 has a first connecting port 65 with the same inner diameter as the water conveying pipe 52. The control plate 64 near the conveying pipe 29 has a second connecting port 66 with the same inner diameter as the conveying pipe 29 and a third connecting port 67 with a smaller inner diameter than the conveying pipe 29. A plug rod 69 is also fixedly connected to the side wall of the control plate 64 near the water conveying pipe 52. A trigger seat 68 adapted to the plug rod 69 is provided in the inner wall of the control box 61. The signal output end of the trigger seat 68 is connected to the water pump in the water tank 51 through a wire. Specifically, during the continuous reaction, when the first thermometer 25 detects that the temperature inside the reaction cylinder 26 is too high, the drive motor in the control box 61 starts. The drive motor drives the transmission gear 62 to rotate, and the transmission gear 62 drives two sets of transmission racks 63 to move away from each other. The two sets of transmission racks 63 respectively drive two sets of control plates 64 to move away from each other. The first connecting port 65 on one of the control plates 64 moves to connect with the water supply pipe 52. At the same time, the plug 69 on the control plate 64 is inserted into the trigger seat 68, which triggers the trigger seat 68 and sends a signal to the water pump in the water tank 51 through the wire, so that the water pump starts. The water pump transports the water in the water tank 51 to the heating chamber between the fixed bed reactor 21 and the reaction cylinder 26 through the water supply pipe 52. The water flows in the heating chamber to cool the spiral tube 43 and the reaction cylinder 26, thereby reducing the temperature inside the reaction cylinder 26. The second connecting port 66 on another control plate 64 is moved to separate from the feed pipe 29, and the third connecting port 67 is moved to connect with the feed pipe 29. Since the diameter of the third connecting port 67 is smaller than the inner diameter of the feed pipe 29, the amount of α-acetyl-α-chloro-γ-butyrolactone input into the feed pipe 29 is reduced, the feed rate is reduced, the heat of reaction is reduced, and the temperature inside the reaction cylinder 26 is further reduced. When the temperature inside the reaction cylinder 26 drops to the predetermined temperature, the servo motor starts again, causing the trigger seat 68 to separate from the insertion rod 69, shutting off the water pump. At the same time, the two sets of control boards 64 are reset, shutting off the water supply pipe 52, and the material supply pipe 29 resumes normal feeding rate, continuing the continuous feeding operation.

[0026] In this embodiment, the material distribution assembly 7 includes a servo motor 71 fixedly connected to the fixed bed reactor 21. The output end of the servo motor 71 is fixedly connected to a transmission rod 72. The other end of the transmission rod 72 passes through the fixed bed reactor 21 and extends into the reaction cylinder 26. The material distribution assembly 7 also includes a connecting box 76 fixedly connected to the inner wall of the reaction cylinder 26. The feed end of the connecting box 76 is connected to the feed pipe 28. The bottom of the connecting box 76 is also connected to a material distribution plate 74. The top of the material distribution plate 74 passes through the connecting box 76 and is fixed to the transmission rod 72 through a connecting shaft. The bottom of the material distribution plate 74 is also provided with multiple material distribution ports 75. The material distribution assembly 7 also includes a drive gear 73 fixedly connected to the transmission rod 72. A synchronous gear 77 is provided on one side of the drive gear 73. The drive gear 73 meshes with the synchronous gear 77. The pressure relief assembly 8 is rotatably connected to the synchronous gear 77. Specifically, during use, when α-acetyl-α-chloro-γ-butyrolactone is fed into the reaction cylinder 26 through the feed pipe 28, the feed pipe 28 first feeds it into the connecting box 76, and the connecting box 76 then feeds it into the distribution plate 74, and it falls into the reaction cylinder 26 through the distribution port 75. During this process, the servo motor 71 starts simultaneously. When the servo motor 71 starts, it drives the transmission rod 72 to rotate. The transmission rod 72 drives the distribution plate 74 to rotate, so that α-acetyl-α-chloro-γ-butyrolactone falls evenly into the reaction cylinder 26 and reacts with the catalyst in the reaction cylinder 26.

[0027] In this embodiment, the pressure relief assembly 8 includes a pressure relief box 81. The top of the pressure relief box 81 is fixed to the inner wall of the top of the fixed bed reactor 21 via a connecting shaft. A pressure relief block 82, which is fixed to the synchronous gear 77, is rotatably connected in the pressure relief box 81. A connecting hole 83, which communicates with the inside of the reaction cylinder 26, is opened on the arc surface of the pressure relief box 81. A connecting groove 84, which communicates with the connecting hole 83, is opened inside the pressure relief block 82. A pressure relief pipe 85 is also fixedly connected to the arc surface of the pressure relief box 81. The pressure relief pipe 85 is connected to the connecting hole 83 via the connecting groove 84. The other end of the pressure relief pipe 85 passes through the top of the fixed bed reactor 21 and extends to the outside of the fixed bed reactor 21. A pressure relief head 86 is fixedly connected to the extended end of the pressure relief pipe 85. Specifically, when the transmission rod 72 rotates, the transmission rod 72 simultaneously drives the drive gear 73 to rotate. When the drive gear 73 rotates one revolution, it drives the synchronous gear 77 to rotate one-quarter revolution, thereby activating the pressure relief assembly 8. When the synchronous gear 77 rotates, it simultaneously drives the pressure relief block 82 in the pressure relief box 81 to rotate. When the two ends of the connecting groove 84 on the pressure relief block 82 rotate to connect with the connecting hole 83 and the pressure relief pipe 85 respectively, the gas in the reaction cylinder 26 can be discharged through the connecting hole 83 and the pressure relief pipe 85, thereby reducing the pressure in the reaction cylinder 26. When the two ends of the connecting groove 84 are rotated to disengage from the connecting hole 83 or the pressure relief pipe 85, they cannot be connected. By intermittently venting, the impact of sudden pressure changes on the reaction system can be avoided, the process stability can be maintained, and the pressure inside the reaction cylinder 26 can always be kept stable.

[0028] Example 3 α-Acetyl-α-chloro-γ-butyrolactone and water were pumped into fixed-bed reactor 21 at a molar ratio of 1:32. The reaction temperature was 85℃, the reaction pressure was atmospheric pressure, the volume hourly space velocity (VHSV) of α-acetyl-α-chloro-γ-butyrolactone was 0.8 h⁻¹, the catalyst was LS-10 ion exchange resin, the conversion rate of α-acetyl-α-chloro-γ-butyrolactone was 99.9%, and the selectivity of 3-chloro-4-oxo-1-pentanol was 97.8%.

[0029] Example 4 α-Acetyl-α-chloro-γ-butyrolactone and water were pumped into fixed-bed reactor 21 at a molar ratio of 1:32. The reaction temperature was 85℃, the reaction pressure was atmospheric pressure, the volume hourly space velocity (VHSV) of α-acetyl-α-chloro-γ-butyrolactone was 0.8 h⁻¹, and 15% wetted catalyst resin was used as the catalyst. The conversion rate of α-acetyl-α-chloro-γ-butyrolactone was 99.9%, and the selectivity of 3-chloro-4-oxo-1-pentanol was 97.9%.

[0030] Example 5 α-Acetyl-α-chloro-γ-butyrolactone and water were pumped into fixed-bed reactor 21 at a molar ratio of 1:32. The reaction temperature was 85℃, the reaction pressure was atmospheric pressure, the volume hourly space velocity (VHSV) of α-acetyl-α-chloro-γ-butyrolactone was 0.8 h⁻¹, and 282-1 catalyst resin was used as the catalyst. The conversion rate of α-acetyl-α-chloro-γ-butyrolactone was 99.9%, and the selectivity of 3-chloro-4-oxo-1-pentanol was 98.6%.

[0031] Example 6 α-Acetyl-α-chloro-γ-butyrolactone and water were pumped into fixed-bed reactor 21 at a molar ratio of 1:32. The reaction temperature was 85℃, the reaction pressure was atmospheric pressure, the volume hourly space velocity (VHSV) of α-acetyl-α-chloro-γ-butyrolactone was 1.0 h⁻¹, and 282-1 catalyst resin was used as the catalyst. The conversion rate of α-acetyl-α-chloro-γ-butyrolactone was 98.7%, and the selectivity of 3-chloro-4-oxo-1-pentanol was 97.6%.

[0032] Example 7 α-Acetyl-α-chloro-γ-butyrolactone and water were pumped into fixed-bed reactor 21 at a molar ratio of 1:32. The reaction temperature was 85℃, the reaction pressure was atmospheric pressure, the volume hourly space velocity (VHSV) of α-acetyl-α-chloro-γ-butyrolactone was 0.6 h⁻¹, 282-1 catalyst resin was used as the catalyst, the conversion rate of α-acetyl-α-chloro-γ-butyrolactone was 100%, and the selectivity of 3-chloro-4-oxo-1-pentanol was 98.8%.

[0033] Example 8 α-Acetyl-α-chloro-γ-butyrolactone and water were pumped into fixed-bed reactor 21 at a molar ratio of 1:32. The reaction temperature was 75℃, the reaction pressure was atmospheric pressure, the volume hourly space velocity (VHSV) of α-acetyl-α-chloro-γ-butyrolactone was 0.8 h⁻¹, and 282-1 catalyst resin was used as the catalyst. The conversion rate of α-acetyl-α-chloro-γ-butyrolactone was 97.7%, and the selectivity of 3-chloro-4-oxo-1-pentanol was 98.8%.

[0034] Example 9 α-Acetyl-α-chloro-γ-butyrolactone and water were pumped into fixed-bed reactor 21 at a molar ratio of 1:32. The reaction temperature was 95℃, the reaction pressure was atmospheric pressure, the volume hourly space velocity (VHSV) of α-acetyl-α-chloro-γ-butyrolactone was 0.8 h⁻¹, 282-1 catalyst resin was used as the catalyst, the conversion rate of α-acetyl-α-chloro-γ-butyrolactone was 100%, and the selectivity of 3-chloro-4-oxo-1-pentanol was 97.8%.

[0035] Example 10 α-Acetyl-α-chloro-γ-butyrolactone and water were pumped into fixed-bed reactor 21 at a molar ratio of 1:16. The reaction temperature was 85℃, the reaction pressure was atmospheric pressure, the volume hourly space velocity (VHSV) of α-acetyl-α-chloro-γ-butyrolactone was 0.8 h⁻¹, 282-1 catalyst resin was used as the catalyst, the conversion rate of α-acetyl-α-chloro-γ-butyrolactone was 100%, and the selectivity of 3-chloro-4-oxo-1-pentanol was 98.8%.

[0036] Example 11 α-Acetyl-α-chloro-γ-butyrolactone and water were pumped into fixed-bed reactor 21 at a molar ratio of 1:32. The reaction temperature was 95℃, the reaction pressure was atmospheric pressure, the volume hourly space velocity (VHSV) of α-acetyl-α-chloro-γ-butyrolactone was 0.8 h⁻¹, 282-1 catalyst resin was used as the catalyst, the conversion rate of α-acetyl-α-chloro-γ-butyrolactone was 100%, and the selectivity of 3-chloro-4-oxo-1-pentanol was 97.8%.

[0037] Example 12 In specific implementation, the purity of α-acetyl-α-chloro-γ-butyrolactone is ≥95%, and the solid acid catalyst is a commercially available acidic ion exchange resin, catalyst resin, etc. In the examples, the concentration of each component in the reaction mixture is analyzed by gas chromatography using a Thermo TRACE 1300 gas chromatograph, an SPB-1 capillary column, and a flame ionization detector. Component concentration is quantified using the internal standard method. First, the peak area of ​​each component is measured, and the component concentration is obtained through a standard working curve. Indicators such as the conversion rate of α-acetyl-α-chloro-γ-butyrolactone and the selectivity of 3-chloro-4-oxo-1-pentanol are calculated. The specific calculation methods in the above examples are as follows: α-Acetyl-α-chloro-γ-butyrolactone conversion rate % = ((mass of added α-acetyl-α-chloro-γ-butyrolactone - mass of α-acetyl-α-chloro-γ-butyrolactone in reaction solution) / mass of added α-acetyl-α-chloro-γ-butyrolactone) 100%; 3-Chloro-4-oxo-1-pentanol selectivity % = (mass of 3-chloro-4-oxo-1-pentanol in reaction solution / 136.58) / (mass of reacted α-acetyl-α-chloro-γ-butyrolactone / 162.01) 100%.

[0038] It should be noted that all the devices in this application are common devices on the market, and can be selected according to the needs of specific use. The circuit connection relationship of each device is a simple series and parallel connection circuit. There is no innovation in the circuit connection part. Those skilled in the art can easily implement it. It belongs to the prior art and will not be described in detail.

[0039] While the present invention has been disclosed above, it is not limited thereto. Any person skilled in the art can make various modifications and alterations without departing from the spirit and scope of the invention; therefore, the scope of protection of the present invention should be determined by the scope defined in the claims.

Claims

1. A process for the synthesis of 3-chloro-4-oxo-l-pentanol from α-acetyl-α-chloro-γ-butyrolactone, characterized in that: It comprises the following steps: S1, the preparation before synthesis: firstly, the solid acid catalyst is filled into the reaction assembly (2) on the operation table (1), and the inlet end of the material conveying pipe (29) on the fixed bed reactor (21) is connected with the feeding end of the storage tank, and the oil inlet end and the water inlet end of the reaction assembly (2) are connected with the auxiliary heating assembly (4) and the cooling assembly (5) respectively; S2, reaction: open the cooling assembly (5) to introduce a certain amount of water into the reaction assembly (2), start the first heater (22), the second heater (23) and the auxiliary heating assembly (4), heat the heat conducting oil input by the auxiliary heating assembly (4) through the first heater (22), and the heat conducting oil is circulated in the reaction assembly (2) to uniformly heat the reaction assembly (2), and α-acetyl-α-chloro-γ-butyrolactone is continuously input into the reaction assembly (2) to carry out hydrolysis reaction under the action of the catalyst in the reaction assembly (2); S3, continuous synthesis: continuously conveying α-acetyl-α-chloro-γ-butyrolactone into the reaction assembly (2) for reaction, and the liquid produced by hydrolysis reaction is collected in the receiving cylinder (31).

2. The apparatus used in the process for the synthesis of 3-chloro-4-oxo-l-pentanol from α-acetyl-α-chloro-γ-butyrolactone according to claim 1, characterized by the fact that: The reaction assembly (2), the receiving assembly (3), the auxiliary heating assembly (4) and the cooling assembly (5) are fixedly connected to the top of the operation table (1), the receiving assembly (3) is fixedly connected to one end of the operation table (1) close to the discharge port of the reaction assembly (2), the auxiliary heating assembly (4) and the cooling assembly (5) are fixedly connected to one end of the reaction assembly (2) close to the inlet, and the auxiliary heating assembly (4) is further fixedly connected with the control assembly (6) for adjusting the input flow of the material conveying pipe (29) and the cooling assembly (5); The top of the reaction assembly (2) is further fixedly connected with the material distribution assembly (7) for uniformly distributing α-acetyl-α-chloro-γ-butyrolactone in the reaction assembly (2), the output end of the material distribution assembly (7) penetrates and extends into the reaction assembly (2), and the material distribution assembly (7) is further fixedly connected with the pressure relief assembly (8) for reducing the pressure in the reaction assembly (2).

3. A device for the synthesis of 3-chloro-4-oxo-l-pentanol from α-acetyl-α-chloro-γ-butyrolactone according to claim 2, characterized in that: The reaction assembly (2) comprises a fixed bed reactor (21), the fixed bed reactor (21) is further fixedly connected with a reaction cylinder (26), a heating cavity is formed between the fixed bed reactor (21) and the reaction cylinder (26), the first heater (22) and the second heater (23) are fixedly connected to the outer walls of the fixed bed reactor (21) close to the top and the bottom respectively, and the fixed bed reactor (21) is further fixedly connected with a first thermometer (25) for monitoring the temperature in the reaction cylinder (26) at one end close to the top. A plurality of groups of support grids (27) are fixedly connected in the inner wall of the reaction cylinder (26), and solid acid catalysts are filled between adjacent two groups of support grids (27); one end of the fixed bed reactor (21) near the top is also fixedly connected with a feeding pipe (28), one end of the feeding pipe (28) near the fixed bed reactor (21) penetrates the fixed bed reactor (21) and the reaction cylinder (26) in sequence and extends into the reaction cylinder (26), and the extending end of the feeding pipe (28) is in communication with the distribution assembly (7); one end of the feeding pipe (28) near the fixed bed reactor (21) is in communication with the feeding pipe (28).

4. A device for the synthesis of 3-chloro-4-oxo-l-pentanol from α-acetyl-α-chloro-γ-butyrolactone according to claim 3, characterized in that: A discharge pipe (24) is also fixedly connected to the fixed bed reactor (21), and the discharge pipe (24) is located directly below the second heater (23); one end of the discharge pipe (24) near the fixed bed reactor (21) penetrates the fixed bed reactor (21) and the reaction cylinder (26) in sequence and is in communication with the reaction cylinder (26); the other end of the discharge pipe (24) is in communication with the receiving assembly (3). The receiving assembly (3) comprises a receiving cylinder (31), the feeding end of the receiving cylinder (31) is in communication with an output pipe (32), the other end of the output pipe (32) is in communication with the discharge pipe (24) on the fixed bed reactor (21), and the discharging end of the receiving cylinder (31) is fixedly connected with a discharge pipe (33).

5. A device for the synthesis of 3-chloro-4-oxo-l-pentanol from α-acetyl-α-chloro-γ-butyrolactone according to claim 4, characterized in that: The auxiliary heating assembly (4) comprises an oil storage cylinder (41) and a spiral pipe (43), the oil storage cylinder (41) is fixedly connected to one end of the operating table (1) away from the receiving assembly (3), and the oil storage cylinder (41) is located between the fixed bed reactor (21) and the cooling assembly (5); the spiral pipe (43) is fixedly connected in the heating cavity between the fixed bed reactor (21) and the reaction cylinder (26); the discharging end of the oil storage cylinder (41) is in communication with an oil conveying pipe (42), and the other end of the oil conveying pipe (42) penetrates the fixed bed reactor (21) and is in communication with the spiral pipe (43); The auxiliary heating assembly (4) further comprises a preheating box (44) and an oil outlet pipe (45), the preheating box (44) is fixedly connected to the top of the oil storage cylinder (41), one end of the oil outlet pipe (45) near the fixed bed reactor (21) is in communication with the discharging end of the spiral pipe (43), the other end of the oil outlet pipe (45) penetrates into the preheating box (44) and is in communication with the oil storage cylinder (41), a second thermometer (46) is also fixedly connected to the oil outlet pipe (45) in the preheating box (44), and a through hole is formed in the preheating box (44) for the feeding pipe (29) to pass through.

6. A device for the synthesis of 3-chloro-4-oxo-l-pentanol from α-acetyl-α-chloro-γ-butyrolactone according to claim 5, characterized in that: The cooling assembly (5) comprises a water tank (51), the discharge end of the water tank (51) is fixedly connected with a water pump, and the output end of the water pump is fixedly connected with a water delivery pipe (52); the other end of the water delivery pipe (52) is fixedly connected with a water inlet (53), the water inlet (53) is fixedly connected to the fixed bed reactor (21), and the end of the water tank (51) close to the fixed bed reactor (21) is in communication with the heating cavity between the fixed bed reactor (21) and the reaction cylinder (26). The water tank (51) is also fixedly connected with a water outlet pipe, and the other end of the water outlet pipe is in communication with the heating cavity.

7. A device for the synthesis of 3-chloro-4-oxo-l-pentanol from α-acetyl-α-chloro-γ-butyrolactone according to claim 6, characterized in that: The control assembly (6) comprises a control box (61), the control box (61) is fixedly connected to the oil storage cylinder (41), the material delivery pipe (29) and the water delivery pipe (52) are both arranged in the control box (61), a drive motor is fixedly connected in the control box (61), the output end of the drive motor is fixedly connected with a transmission gear (62), the transmission gear (62) is rotatably connected in the control box (61), both ends of the transmission gear (62) are provided with transmission racks (63), both groups of transmission racks (63) are engaged with the transmission gear (62), and the two groups of transmission racks (63) are fixedly connected with control plates (64) at the ends away from each other, the two groups of control plates (64) are arranged in the adjacent material delivery pipe (29) or water delivery pipe (52) in a penetrating mode, and both sides of the two groups of control plates (64) are provided with sealing pads.

8. A device for the synthesis of 3-chloro-4-oxo-l-pentanol from α-acetyl-α-chloro-γ-butyrolactone according to claim 7, characterized in that: The control plate (64) close to the water delivery pipe (52) is provided with a first communication port (65) with the same inner diameter as the water delivery pipe (52), the control plate (64) close to the material delivery pipe (29) is provided with a second communication port (66) with the same inner diameter as the material delivery pipe (29) and a third communication port (67) smaller than the inner diameter of the material delivery pipe (29); The control plate (64) close to the water delivery pipe (52) is also fixedly connected with a plug rod (69), a trigger seat (68) matched with the plug rod (69) is arranged in the inner wall of the control box (61), and the signal output end of the trigger seat (68) is connected with the water pump in the water tank (51) through a wire.

9. A device for synthesizing 3-chloro-4-oxo-l-pentanol from α-acetyl-α-chloro-γ-butyrolactone according to claim 3, characterized in that: The material distribution assembly (7) comprises a servo motor (71) fixedly connected to the fixed bed reactor (21), the output end of the servo motor (71) is fixedly connected with a transmission rod (72), and the other end of the transmission rod (72) penetrates through the fixed bed reactor (21) and extends into the reaction cylinder (26). The material distribution assembly (7) further comprises a communication box (76) fixedly connected to the inner wall of the reaction cylinder (26), the feed inlet of the communication box (76) is in communication with the feed pipe (28), the bottom of the communication box (76) is further communicated with a material distribution plate (74), the top of the material distribution plate (74) penetrates through the communication box (76) and is fixedly connected with the transmission rod (72) through a connecting shaft, and the bottom of the material distribution plate (74) is provided with a plurality of material distribution ports (75).

10. A device for the synthesis of 3-chloro-4-oxo-l-pentanol from α-acetyl-α-chloro-γ-butyrolactone according to claim 9, characterized in that: The distributing assembly (7) further comprises a driving gear (73) fixedly connected to the transmission rod (72), one side of the driving gear (73) is provided with a synchronous gear (77), and the driving gear (73) is engaged with the synchronous gear (77); the pressure relief assembly (8) is rotationally connected to the synchronous gear (77); The pressure relief assembly (8) comprises a pressure relief box (81), the top of the pressure relief box (81) is fixed to the inner wall of the top of the fixed bed reactor (21) through a connecting shaft, a pressure relief block (82) fixed to the synchronous gear (77) is rotationally connected in the pressure relief box (81), a communication hole (83) in communication with the inside of the reaction cylinder (26) is formed in the arc surface of the pressure relief box (81), a communication groove (84) in communication with the communication hole (83) is formed in the inside of the pressure relief block (82), a pressure relief pipe (85) is further fixedly connected to the arc surface of the pressure relief box (81), the pressure relief pipe (85) is in communication with the communication hole (83) through the communication groove (84), the other end of the pressure relief pipe (85) penetrates through the top of the fixed bed reactor (21) and extends to the outside of the fixed bed reactor (21), and a pressure relief head (86) is fixedly connected to the extending end of the pressure relief pipe (85).

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