1-cyclopropyl-3-(2-methylthio-4-trifluoromethylphenyl) propyl-1, 3-diketone production system
By designing a production system with esterification and condensation units, the problems of highly corrosive reagents and high-temperature reactions in traditional synthesis methods were solved, enabling the low-cost and high-yield production of 1-cyclopropyl-3-(2-(methylthio)-4-(trifluoromethyl)phenyl)propyl-1,3-dione, which is suitable for the industrial application of isoxazolidinone.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- INNER MONGOLIA LANKE BIOTECHNOLOGY CO LTD
- Filing Date
- 2025-05-15
- Publication Date
- 2026-05-05
AI Technical Summary
In the traditional synthesis of 1-cyclopropyl-3-(2-methylthio-4-trifluoromethylphenyl)propyl-1,3-dione, the esterification reaction uses highly corrosive reagents, and the condensation reaction requires high temperature and is prone to inducing side reactions, resulting in high requirements for the corrosion resistance of equipment and limiting the sustainability of its industrial application.
A production system comprising an esterification unit and a condensation unit was designed. The system uses raw materials such as concentrated sulfuric acid and methanol to carry out an esterification reaction under mild conditions, followed by a condensation reaction with cyclopropyl methyl ketone under mild conditions. This reduces the generation of waste, lowers production costs, and increases yield.
This study achieved efficient production of 1-cyclopropyl-3-(2-(methylthio)-4-(trifluoromethyl)phenyl)propyl-1,3-dione under mild reaction conditions, reducing waste generation, lowering production costs, and providing high-quality reaction feedstock, thus laying the foundation for the industrial production of isoxazolidinone.
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Figure CN224194737U_ABST
Abstract
Description
Technical fields:
[0001] This utility model relates to the field of isoxazolidin production technology, specifically to a production system for 1-cyclopropyl-3-(2-methylthio-4-trifluoromethylphenyl)propyl-1,3-dione. Background technology:
[0002] Isoxazolidinone, a broad-spectrum herbicide, exhibits excellent bioactivity against both grasses and broadleaf weeds. It also demonstrates advantages such as safety, low residue, good environmental and ecological compatibility, and high safety profile for corn and sugar beets. 1-Cyclopropyl-3-(2-methylthio-4-trifluoromethylphenyl)propyl-1,3-dione is a key intermediate in the synthesis of isoxazolidinone and can be used in the production of insecticides, herbicides, and other pesticides. The traditional synthesis of 1-cyclopropyl-3-(2-methylthio-4-trifluoromethylphenyl)propyl-1,3-dione uses 2-methylthio-4-trifluoromethylbenzoic acid as a starting material and requires two core reactions: esterification and Claisen condensation. The traditional esterification reaction involves reacting 2-methylthio-4-trifluoromethylbenzoic acid with methanol under acidic conditions such as thionyl chloride or PCl5 catalysis to generate methyl 2-methylthio-4-trifluoromethylbenzoate; subsequently, the intermediate cyclopropyl methyl ketone undergoes Claisen condensation under strongly alkaline conditions in a KOH / ethanol system to generate the target diketone compound, which is finally purified by acidification.
[0003] However, this route has significant drawbacks: (1) the esterification step relies on highly corrosive reagents such as PCl5 or thionyl chloride, the reaction is violent and produces a large amount of acidic gas, and the post-processing is prone to producing acidic waste; (2) the condensation reaction conditions are harsh and require high temperature reaction, which can easily induce side reactions, such as methylthio oxidation or trifluoromethyl dehalogenation, and strict temperature control is required to avoid product degradation; in addition, this method has high requirements for the corrosion resistance of equipment, which limits the sustainability of its industrial application. Utility Model Content:
[0004] The purpose of this invention is to provide a production system for 1-cyclopropyl-3-(2-methylthio-4-trifluoromethylphenyl)propyl-1,3-dione.
[0005] This utility model is implemented by the following technical solution: a 1-cyclopropyl-3-(2-methylthio-4-trifluoromethylphenyl)propyl-1,3-dione production system, which includes an esterification unit and a condensation unit. The esterification unit includes a concentrated sulfuric acid high-level tank, a first process water high-level tank, a methanol high-level tank, a first toluene high-level tank, an esterification reactor, an esterification distillation reactor, a first packaging system, and a stratified liquid receiving tank. The outlets of the concentrated sulfuric acid high-level tank, the first process water high-level tank, the methanol high-level tank, and the first toluene high-level tank are all connected to the inlet of the esterification reactor. A 2-methylthio-4-trifluoromethylbenzoic acid feeding port is provided on the side of the esterification reactor. The discharge port of the esterification reactor is connected to the inlet of the esterification distillation reactor, and the outlet of the esterification distillation reactor is connected to the inlet of the first packaging system. The outlet of the esterification reactor is connected to the inlet of the stratified liquid receiving tank through a pipeline.
[0006] The condensation unit includes a cyclopropyl ketone high-level tank, a second process water high-level tank, a concentrated hydrochloric acid high-level tank, a second toluene high-level tank, a condensation reactor, a condensation distillation reactor, and a second packaging system. The outlets of the cyclopropyl ketone high-level tank, the second process water high-level tank, the concentrated hydrochloric acid high-level tank, and the second toluene high-level tank are all connected to the inlet of the condensation reactor. The side of the condensation reactor is provided with a methyl 2-methylthio-4-trifluoromethylbenzoate feeding port. The outlet of the condensation reactor is connected to the inlet of the condensation distillation reactor, and the discharge port of the condensation distillation reactor is connected to the second packaging system.
[0007] Furthermore, the esterification unit also includes an esterification condenser and an esterification receiving tank. The exhaust port of the esterification reactor is connected to the inlet of the esterification condenser, and the outlet of the esterification condenser is connected to the esterification receiving tank. The exhaust port of the esterification receiving tank is connected to the inlet of a vacuum condenser. The outlet of the vacuum condenser is divided into two paths: one path is connected to the inlet of the vacuum condenser, and the other path is connected to the inlet of the tail gas condenser. The outlet of the vacuum condenser is connected to the inlet of the vacuum condenser receiving tank, and the outlet of the tail gas condenser is connected to the inlet of the tail gas condenser receiving tank.
[0008] Furthermore, the esterification unit also includes an esterification distillation condenser and an esterification distillation receiving tank. The exhaust port of the esterification distillation vessel is connected to the inlet of the esterification distillation condenser, and the outlet of the esterification distillation condenser is connected to the inlet of the esterification distillation receiving tank. The outlet of the esterification distillation receiving tank is divided into two paths: one path is connected to the inlet of a vacuum condenser, and the other path is connected to the inlet of a tail gas condenser. The outlet of the vacuum condenser is connected to the inlet of the vacuum condenser receiving tank, and the outlet of the tail gas condenser is connected to the inlet of the tail gas condenser receiving tank.
[0009] Furthermore, the condensation unit also includes a condensation condenser and a condensation recovery tank. The exhaust port of the condensation reactor is connected to the inlet of the condensation condenser, and the outlet of the condensation condenser is connected to the inlet of the condensation recovery tank. The outlet of the condensation recovery tank is divided into two paths: one path is connected to the inlet of a vacuum condenser, and the other path is connected to the inlet of a tail gas condenser. The outlet of the vacuum condenser is connected to the inlet of a vacuum condensation receiving tank, and the outlet of the tail gas condenser is connected to the inlet of a tail gas condensation receiving tank.
[0010] Furthermore, the condensation unit also includes a condensation distillation condenser and a condensation distillation recovery tank. The exhaust port of the condensation distillation vessel is connected to the inlet of the condensation distillation condenser, and the outlet of the condensation distillation condenser is connected to the inlet of the condensation distillation recovery tank. The outlet of the condensation distillation recovery tank is divided into two paths: one path is connected to the inlet of a vacuum condenser, and the other path is connected to the inlet of a tail gas condenser. The outlet of the vacuum condenser is connected to the inlet of a vacuum condensation receiving tank, and the outlet of the tail gas condenser is connected to the inlet of a tail gas condensation receiving tank.
[0011] Furthermore, the condensation unit also includes a sodium chloride concentration vessel and a centrifuge. The discharge port of the condensation reaction vessel is connected to the inlet of the sodium chloride concentration vessel, the outlet of the sodium chloride concentration vessel is connected to the inlet of the centrifuge, and the liquid phase outlet of the centrifuge is connected to the inlet of the sodium chloride concentration vessel.
[0012] Furthermore, an intermediate esterification tank is provided between the esterification condenser and the esterification receiving tank. The outlet of the esterification condenser is connected to the inlet of the intermediate esterification tank, and the bottom outlet of the intermediate esterification tank is connected to the inlet of the esterification receiving tank. The lower side outlet of the intermediate esterification tank is connected to the reflux port of the esterification reactor, and the upper side outlet of the intermediate esterification tank is connected to the inlet of the receiving tank of the esterification reactor.
[0013] Furthermore, a condensation intermediate tank is provided between the condensation condenser and the condensation recovery tank. The outlet of the condensation condenser is connected to the inlet of the condensation intermediate tank, and the bottom outlet of the condensation intermediate tank is connected to the inlet of the condensation recovery tank. The lower side outlet of the condensation intermediate tank is connected to the reflux port of the condensation reactor, and the upper side outlet of the condensation intermediate tank is connected to the inlet of the condensation recovery tank.
[0014] Advantages of this invention: The production system has a simple connection structure and is easy to implement. 2-Methylthio-4-trifluoromethylbenzoic acid and other raw materials are first esterified to obtain methyl 2-methylthio-4-trifluoromethylbenzoate, which is then reacted with cyclopropyl ketone and other raw materials to obtain 1-cyclopropyl-3-(2-(methylthio)-4-(trifluoromethyl)phenyl)propyl-1,3-dione, reducing the generation of waste and lowering production costs. Furthermore, the reaction temperature is not high, the reaction conditions are mild, the yield is high, and the production cost is low. It can reduce the impurity content in the product 1-cyclopropyl-3-(2-(methylthio)-4-(trifluoromethyl)phenyl)propyl-1,3-dione, providing high-quality reaction raw materials for the subsequent industrial production of isoxazolidin, and is suitable for large-scale industrial production. Attached image description:
[0015] Figure 1 This is a schematic diagram of the overall structure of this embodiment.
[0016] Figure 2 This is a schematic diagram of the esterification unit structure.
[0017] Figure 3 This is a schematic diagram of the condensation unit structure.
[0018] Esterification Unit 1, Concentrated Sulfuric Acid High-Level Tank 11, First Process Water High-Level Tank 12, Methanol High-Level Tank 13, First Toluene High-Level Tank 14, Esterification Reactor 15, Esterification Distillation Reactor 16, First Packaging System 17, Separated Liquid Receiving Tank 18, 2-Methylthio-4-trifluoromethylbenzoic Acid Feeding Port 19, Esterification Condenser 110, Esterification Receiving Tank 111, Esterification Intermediate Tank 112, Esterification Distillation Condenser 113, Esterification Distillation Receiving Tank 114, Condensation Unit 2, Cyclopropyl Methyl Ketone High-Level Tank 21, Second Process Water 22. High-level tank, 23. High-level tank for concentrated hydrochloric acid, 24. High-level tank for second toluene, 25. Condensation reactor, 26. Condensation distillation reactor, 27. Second packaging system, 28. Feed port for methyl 2-methylthio-4-trifluoromethylbenzoate, 29. Condensation condenser, 210. Condensation recovery tank, 211. Condensation intermediate tank, 212. Condensation distillation condenser, 213. Condensation distillation recovery tank, 214. Sodium chloride concentration reactor, 215. Centrifuge, 3. Vacuum condenser, 4. Tail gas condenser, 5. Vacuum condensation receiving tank, 6. Tail gas condensation receiving tank. Detailed implementation method:
[0019] In the description of this utility model, it should be noted that the terms "center," "upper," "lower," "left," "right," "vertical," "horizontal," "inner," and "outer," etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of describing this utility model and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this utility model. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and should not be construed as indicating or implying relative importance.
[0020] like Figures 1 to 3 As shown, a production system for 1-cyclopropyl-3-(2-methylthio-4-trifluoromethylphenyl)propyl-1,3-dione includes an esterification unit 1 and a condensation unit 2.
[0021] Esterification unit 1 includes a concentrated sulfuric acid high-level tank 11, a first process water high-level tank 12, a methanol high-level tank 13, a first toluene high-level tank 14, an esterification reactor 15, an esterification distillation reactor 16, a first packaging system 17, and a stratified liquid receiving tank 18. The outlets of the concentrated sulfuric acid high-level tank 11, the first process water high-level tank 12, the methanol high-level tank 13, and the first toluene high-level tank 14 are all connected to the inlet of the esterification reactor 15. A 2-methylthio-4-trifluoromethylbenzoic acid feeding port 19 is provided on the side of the esterification reactor 15. The discharge port of the esterification reactor 15 is connected to the inlet of the esterification distillation reactor 16, and the outlet of the esterification distillation reactor 16 is connected to the first packaging system 17. The feed inlet of system 17 is connected; the discharge outlet of esterification reactor 15 is connected to the inlet of stratified liquid receiving tank 18 via a pipeline; the exhaust port of esterification reactor 15 is connected to the inlet of esterification condenser 110, and the outlet of esterification condenser 110 is connected to esterification receiving tank 111; the exhaust port of esterification receiving tank 111 is connected to the inlet of vacuum condenser 3, the outlet of vacuum condenser 3 is divided into two paths, one path is connected to the inlet of vacuum condenser 3, and the other path is connected to the inlet of tail gas condenser 4; the outlet of vacuum condenser 3 is connected to the inlet of vacuum condensation receiving tank 5, and the outlet of tail gas condenser 4 is connected to the inlet of tail gas condensation receiving tank 6. An intermediate esterification tank 112 is provided between the esterification condenser 110 and the esterification receiving tank 111. The outlet of the esterification condenser 110 is connected to the inlet of the intermediate esterification tank 112, and the bottom outlet of the intermediate esterification tank 112 is connected to the inlet of the esterification receiving tank 111. The lower side outlet of the intermediate esterification tank 112 is connected to the reflux port of the esterification reactor 15, and the upper side outlet of the intermediate esterification tank 112 is connected to the inlet of the receiving tank of the esterification reactor 15. The exhaust port of the esterification distillation kettle 16 is connected to the inlet of the esterification distillation condenser 113, and the outlet of the esterification distillation condenser 113 is connected to the inlet of the esterification distillation receiving tank 114. The outlet of the esterification distillation receiving tank 114 is divided into two paths: one path is connected to the inlet of the vacuum condenser 3, and the other path is connected to the inlet of the tail gas condenser 4. The outlet of the vacuum condenser 3 is connected to the inlet of the vacuum condensation receiving tank 5, and the outlet of the tail gas condenser 4 is connected to the inlet of the tail gas condensation receiving tank 6.
[0022] Esterification reaction:
[0023] 1000 kg of 2-methylthio-4-trifluoromethylbenzoic acid was added to the esterification reactor 15 through the 2-methylthio-4-trifluoromethylbenzoic acid feed port 19, and 1700 L of toluene was added to the esterification reactor 15 through the first toluene high-level tank 14. Afterwards, the mixture was heated and refluxed to remove water. The steam produced in the esterification reactor 15 was condensed by the esterification condenser 110 and then entered the esterification intermediate tank 112. The collected condensate was returned to the esterification reactor 15. After the water removal was completed, the esterification reactor 15 was cooled to approximately 40°C. Then, 500 kg of concentrated sulfuric acid and 1500 L of methanol were added dropwise to the esterification reactor 15 through the concentrated sulfuric acid high-level tank 11 and the methanol high-level tank 13, respectively. The reflux reaction continued. After the reaction was deemed satisfactory, the mixture was allowed to settle and separate into layers. The lower layer of sulfuric acid was discharged into the layered liquid receiving tank 18, while several layers remained in the esterification reactor 15. Next, process water is added to the esterification reactor 15 through the first process water high-level tank 12 to wash the several layers. After washing, the layers are separated again. The water at the bottom is discharged into the layered liquid receiving tank 18, and the organic layer at the top is sent to the esterification distillation reactor for vacuum distillation to remove toluene. The resulting methyl 2-methylthio-4-trifluoromethylbenzoate is sent to the first packaging system 17 for packaging and use.
[0024] During the esterification process, the liquid discharged from the intermediate esterification tank 112 is sampled and analyzed periodically. When the toluene concentration in the liquid exceeds the standard, it is discharged into the esterification receiving tank 111 and subsequently sent to the toluene recovery system. The gas discharged from the esterification distillation kettle 16 is condensed by the esterification condenser 110, and the condensed liquid is collected in the esterification distillation receiving tank 114 and subsequently sent to the toluene recovery system.
[0025] The condensation unit 2 includes a cyclopropyl ketone high-level tank 21, a second process water high-level tank 22, a concentrated hydrochloric acid high-level tank 23, a second toluene high-level tank 24, a condensation reactor 25, a condensation distillation kettle 26, and a second packaging system 27. The outlets of the cyclopropyl ketone high-level tank 21, the second process water high-level tank 22, the concentrated hydrochloric acid high-level tank 23, and the second toluene high-level tank 24 are all connected to the inlet of the condensation reactor 25. A methyl 2-methylthio-4-trifluoromethylbenzoate feeding port 28 is provided on the side of the condensation reactor 25. The outlet of the condensation reactor 25 is connected to the inlet of the condensation distillation kettle 26, and the discharge port of the condensation distillation kettle 26 is connected to the second packaging system 27. The exhaust port of the condensation reactor 25 is connected to the inlet of the condensation condenser 29, and the outlet of the condensation condenser 29 is connected to the inlet of the condensation recovery tank 210. The outlet of the condensation recovery tank 210 is divided into two paths: one path is connected to the inlet of the vacuum condenser 3, and the other path is connected to the inlet of the tail gas condenser 4. The outlet of the vacuum condenser 3 is connected to the inlet of the vacuum condensation receiving tank 5, and the outlet of the tail gas condenser 4 is connected to the inlet of the tail gas condensation receiving tank 6. A condensation intermediate tank 211 is provided between the condensation condenser 29 and the condensation recovery tank 210. The outlet of the condensation condenser 29 is connected to the inlet of the condensation intermediate tank 211, and the bottom outlet of the condensation intermediate tank 211 is connected to the inlet of the condensation recovery tank 210. The lower side outlet of the condensation intermediate tank 211 is connected to the reflux port of the condensation reactor 25, and the upper side outlet of the condensation intermediate tank 211 is connected to the inlet of the condensation recovery tank 210. The exhaust port of the condensation distillation kettle 26 is connected to the inlet of the condensation distillation condenser 212, and the outlet of the condensation distillation condenser 212 is connected to the inlet of the condensation distillation recovery tank 213. The outlet of the condensation distillation recovery tank 213 is divided into two paths: one path is connected to the inlet of the vacuum condenser 3, and the other path is connected to the inlet of the tail gas condenser 4. The outlet of the vacuum condenser 3 is connected to the inlet of the vacuum condensation receiving tank 5, and the outlet of the tail gas condenser 4 is connected to the inlet of the tail gas condensation receiving tank 6. The discharge port of the condensation reaction kettle 25 is connected to the inlet of the sodium chloride concentration kettle 214, the outlet of the sodium chloride concentration kettle 214 is connected to the inlet of the centrifuge 215, and the liquid phase outlet of the centrifuge 215 is connected to the inlet of the sodium chloride concentration kettle 214.
[0026] Condensation reaction:
[0027] 2200L of toluene was added to the second toluene high-level tank 24 and the condensation reactor 25. 525kg of sodium methoxide and 1100kg of methyl 2-methylthio-4-trifluoromethylbenzoate prepared in esterification unit 1 were added to the condensation reactor 25 through the methyl 2-methylthio-4-trifluoromethylbenzoate feed port 28. After heating to 50℃, 340kg of cyclopropyl methyl ketone was added dropwise to the condensation reactor 25 through the cyclopropyl methyl ketone high-level tank 21, completing the addition within one hour. After the addition was complete, the temperature was maintained at 55-60℃ for 1.5 hours to carry out the condensation reaction. During the reaction, the steam produced in the condensation reactor 25 was condensed by the condensation condenser 29 and entered the condensation intermediate tank 211. The collected condensate was returned to the condensation reactor 25.
[0028] After the reaction is qualified, 500L of water is added to the condensation reactor 25 through the second process water high-level tank 22, and hydrochloric acid is added dropwise to the condensation reactor 25 through the concentrated hydrochloric acid high-level tank 23 to adjust the pH of the reactor to 2-3. After standing, the water layer is discharged into the sodium chloride concentration reactor 214. The remaining organic layer in the condensation reactor is then washed with water, 5% potassium carbonate alkali, and water in sequence. The separated water layers are all discharged into the sodium chloride concentration reactor 214. After the water layer is concentrated in the sodium chloride concentration reactor 214, the sodium chloride byproduct is separated by a centrifuge. Finally, the organic layer in the condensation reactor 25 is sent to the condensation distillation reactor 26 to remove toluene by vacuum distillation. The obtained 1-cyclopropyl-3-(2-(methylthio)-4-(trifluoromethyl)phenyl)propyl-1,3-dione is packaged by the second packaging system 27 to obtain the product.
[0029] During the condensation process, the liquid discharged from the intermediate condensation tank 211 is sampled and analyzed periodically. When the toluene concentration in the liquid exceeds the standard, it is discharged into the condensation recovery tank 210 and subsequently sent to the toluene recovery system. The gas discharged from the condensation distillation kettle 26 is condensed by the condensation distillation condenser 212, and the condensed liquid is collected in the condensation distillation recovery tank 213 and subsequently sent to the toluene recovery system.
[0030] During the above reaction process, the gases discharged from the esterification receiving tank 111, esterification distillation receiving tank 114, condensation recovery tank 210, and condensation distillation recovery tank 213 during vacuuming are all condensed by a vacuum condenser and then sent to the vacuum condensation collection tank 5. The tail gas discharged during the reaction process is condensed by the tail gas condenser 4 and then sent to the tail gas condensation receiving tank 6. Finally, the gases discharged from the vacuum condensation collection tank 5 and the tail gas condensation receiving tank 6 are sent to the tail gas treatment system, while the liquid is also sent to the toluene recovery system.
[0031] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of this utility model, and are not intended to limit it. Although the utility model has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some or all of the technical features therein. Such modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of this utility model.
Claims
A production system for 1,1-cyclopropyl-3-(2-methylthio-4-trifluoromethylphenyl)propyl-1,3-dione, characterized in that, It includes esterification units and condensation units. The esterification unit includes a concentrated sulfuric acid high-level tank, a first process water high-level tank, a methanol high-level tank, a first toluene high-level tank, an esterification reactor, an esterification distillation reactor, a first packaging system, and a stratified liquid receiving tank. The outlets of the concentrated sulfuric acid high-level tank, the first process water high-level tank, the methanol high-level tank, and the first toluene high-level tank are all connected to the inlet of the esterification reactor. The side of the esterification reactor is provided with a 2-methylthio-4-trifluoromethylbenzoic acid feeding port. The discharge port of the esterification reactor is connected to the inlet of the esterification distillation reactor, and the outlet of the esterification distillation reactor is connected to the inlet of the first packaging system. The outlet of the esterification reactor is connected to the inlet of the stratified liquid receiving tank through a pipeline. The condensation unit includes a cyclopropyl ketone high-level tank, a second process water high-level tank, a concentrated hydrochloric acid high-level tank, a second toluene high-level tank, a condensation reactor, a condensation distillation reactor, and a second packaging system. The outlets of the cyclopropyl ketone high-level tank, the second process water high-level tank, the concentrated hydrochloric acid high-level tank, and the second toluene high-level tank are all connected to the inlet of the condensation reactor. The side of the condensation reactor is provided with a methyl 2-methylthio-4-trifluoromethylbenzoate feeding port. The outlet of the condensation reactor is connected to the inlet of the condensation distillation reactor, and the discharge port of the condensation distillation reactor is connected to the second packaging system.
2. The 1-cyclopropyl-3-(2-methylthio-4-trifluoromethylphenyl)propyl-1,3-dione production system according to claim 1, characterized in that, The esterification unit further includes an esterification condenser and an esterification receiving tank. The exhaust port of the esterification reactor is connected to the inlet of the esterification condenser, and the outlet of the esterification condenser is connected to the esterification receiving tank. The exhaust port of the esterification receiving tank is connected to the inlet of a vacuum condenser. The outlet of the vacuum condenser is divided into two paths: one path is connected to the inlet of the vacuum condenser, and the other path is connected to the inlet of the tail gas condenser. The outlet of the vacuum condenser is connected to the inlet of the vacuum condenser receiving tank, and the outlet of the tail gas condenser is connected to the inlet of the tail gas condenser receiving tank.
3. The 1-cyclopropyl-3-(2-methylthio-4-trifluoromethylphenyl)propyl-1,3-dione production system according to claim 1, characterized in that, The esterification unit further includes an esterification distillation condenser and an esterification distillation receiving tank. The exhaust port of the esterification distillation kettle is connected to the inlet of the esterification distillation condenser, and the outlet of the esterification distillation condenser is connected to the inlet of the esterification distillation receiving tank. The outlet of the esterification distillation receiving tank is divided into two paths: one path is connected to the inlet of a vacuum condenser, and the other path is connected to the inlet of a tail gas condenser. The outlet of the vacuum condenser is connected to the inlet of the vacuum condenser receiving tank, and the outlet of the tail gas condenser is connected to the inlet of the tail gas condenser receiving tank.
4. The 1-cyclopropyl-3-(2-methylthio-4-trifluoromethylphenyl)propyl-1,3-dione production system according to claim 1, characterized in that, The condensation unit further includes a condensation condenser and a condensation recovery tank. The exhaust port of the condensation reactor is connected to the inlet of the condensation condenser, and the outlet of the condensation condenser is connected to the inlet of the condensation recovery tank. The outlet of the condensation recovery tank is divided into two paths: one path is connected to the inlet of a vacuum condenser, and the other path is connected to the inlet of a tail gas condenser. The outlet of the vacuum condenser is connected to the inlet of a vacuum condensation receiving tank, and the outlet of the tail gas condenser is connected to the inlet of a tail gas condensation receiving tank.
5. The 1-cyclopropyl-3-(2-methylthio-4-trifluoromethylphenyl)propyl-1,3-dione production system according to claim 1, characterized in that, The condensation unit further includes a condensation distillation condenser and a condensation distillation recovery tank. The exhaust port of the condensation distillation kettle is connected to the inlet of the condensation distillation condenser, and the outlet of the condensation distillation condenser is connected to the inlet of the condensation distillation recovery tank. The outlet of the condensation distillation recovery tank is divided into two paths: one path is connected to the inlet of a vacuum condenser, and the other path is connected to the inlet of a tail gas condenser. The outlet of the vacuum condenser is connected to the inlet of a vacuum condensation receiving tank, and the outlet of the tail gas condenser is connected to the inlet of a tail gas condensation receiving tank.
6. The 1-cyclopropyl-3-(2-methylthio-4-trifluoromethylphenyl)propyl-1,3-dione production system according to claim 1, characterized in that, The condensation unit also includes a sodium chloride concentration vessel and a centrifuge. The discharge port of the condensation reaction vessel is connected to the inlet of the sodium chloride concentration vessel, the outlet of the sodium chloride concentration vessel is connected to the inlet of the centrifuge, and the liquid phase outlet of the centrifuge is connected to the inlet of the sodium chloride concentration vessel.
7. The 1-cyclopropyl-3-(2-methylthio-4-trifluoromethylphenyl)propyl-1,3-dione production system according to claim 2, characterized in that, An intermediate esterification tank is provided between the esterification condenser and the esterification receiving tank. The outlet of the esterification condenser is connected to the inlet of the intermediate esterification tank, and the bottom outlet of the intermediate esterification tank is connected to the inlet of the esterification receiving tank. The lower side outlet of the intermediate esterification tank is connected to the reflux port of the esterification reactor, and the upper side outlet of the intermediate esterification tank is connected to the inlet of the receiving tank of the esterification reactor.
8. The 1-cyclopropyl-3-(2-methylthio-4-trifluoromethylphenyl)propyl-1,3-dione production system according to claim 4, characterized in that, A condensation intermediate tank is provided between the condensation condenser and the condensation recovery tank. The outlet of the condensation condenser is connected to the inlet of the condensation intermediate tank, and the bottom outlet of the condensation intermediate tank is connected to the inlet of the condensation recovery tank. The lower side outlet of the condensation intermediate tank is connected to the reflux port of the condensation reactor, and the upper side outlet of the condensation intermediate tank is connected to the inlet of the condensation recovery tank.