Butyl benzyl phthalate production device

Abstract

The utility model relates to a butyl benzyl phthalate production device which comprises a reaction kettle, the reaction kettle comprises a kettle body and a jacket arranged on the outer side of the kettle body, a spiral coil pipe is arranged on the inner side of the jacket, a stirring device is arranged on the kettle body, and the stirring device comprises a stirring shaft, stirring blades and a stirring motor which are arranged on the kettle body. A benzyl chloride storage tank and a triethylamine storage tank are arranged above the kettle body, the benzyl chloride storage tank is communicated with the kettle body through a raw material conveying device, and the kettle body is communicated with the triethylamine storage tank through a raw material conveying device; the raw material conveying device comprises a raw material conveying pipe as well as a liquid flow sensor, a first adjusting valve, a quantitative tank and a second adjusting valve which are sequentially arranged on the raw material conveying pipe in the direction from the position close to the kettle body to the position away from the kettle body; a temperature sensor and a pH sensor are arranged in the kettle body. The feeding speed of the benzyl chloride and the triethylamine can be controlled, and the temperature of the reaction kettle in the adding process of the benzyl chloride and the triethylamine can be fed back. The utility model has the advantages of convenient use and wide market prospect.

Description

Technical Field

[0001] The utility model relates to production equipment for butyl benzyl phthalate, in particular to a production device for butyl benzyl phthalate. Background Art

[0002] Plasticizers have an inter-molecular chain isolation effect on the base material in the adhesive layer, can shield its active groups, weaken the interaction between molecules, thereby reducing its glass transition temperature and melting temperature, and improving the brittleness of the adhesive layer. Plasticizer molecules contain polar and non-polar parts. When playing a plasticizing role, the polar part interacts with the plasticized material to form a uniform and stable system, and the non-polar part acts as a chain spacer. According to the mode of action, plasticizers are divided into external plasticizers and internal plasticizers. External plasticizers are dispersed in the adhesive layer in the form of separated molecules. Butyl benzyl phthalate is an excellent external plasticizer, which is mainly used in the processing and molding of plastic products to improve the plasticity and fluidity of the resin. It can also dissolve organic pigments, so that the products have excellent transparency and smooth surface. The product is a transparent oily liquid with a slight aromatic smell, strong solvent ability, excellent foaming performance and oil extraction resistance, good anti-pollution, low volatility, low water extraction and anti-migration, and fast plasticization speed.

[0003] The production principle of butyl benzyl phthalate is that phthalic anhydride and butanol generate monobutyl phthalate through esterification reaction, and then neutralize with alkali solution, and the obtained sodium monobutyl phthalate and benzyl chloride are condensed under the catalysis of triethylamine to generate butyl benzyl phthalate. The specific process is: phthalic anhydride and butanol are esterified at 100℃ to 105℃ to generate monobutyl phthalate, and then neutralized with alkali at 65℃ to 75℃ to generate sodium salt of monobutyl phthalate, and then condensed with benzyl chloride under the catalysis of triethylamine at 110℃ to 112℃ to generate crude butyl benzyl phthalate. After washing and layering, the crude butyl benzyl phthalate is subjected to steam vacuum distillation to remove low-boiling substances and salts to obtain the finished butyl benzyl phthalate.

[0004] Among them, the reaction of sodium butyl phthalate and benzyl chloride under the catalysis of triethylamine is also called condensation reaction, which is specifically: after the reactor is heated to above 85°C, 1.2KmoL of benzyl chloride and 10moL of triethylamine are added to the reactor at the same time and evenly. When the temperature of the reactor reaches 100°C, the reaction system begins to reflux, and the reaction temperature is controlled at 110°C to 112°C, and the pH is controlled between 8.5 and 9.0. After four hours of reaction, the condensation reaction can be stopped and the jacket gas can be turned off. Since the activity of benzyl chloride is higher than that of general alcohols, the condensation reaction is a strong exothermic reaction. If the speed of adding benzyl chloride and triethylamine is too fast, it will cause the reactor to be flushed, so benzyl chloride and triethylamine need to be added evenly, and then the temperature of the reactor is controlled. There is room for improvement in this part of the prior art, so that the staff can be given enough prompts to control the feeding speed of benzyl chloride and triethylamine, thereby reducing the dangerous situation of reactor flushing. Summary of the invention

[0005] In view of the deficiencies in the prior art, the utility model provides a production device for butyl benzyl phthalate, which can control the feed rate of benzyl chloride and triethylamine and can also feed back the temperature of a reactor during the process of adding benzyl chloride and triethylamine, so as to overcome the defects in the prior art.

[0006] The technical scheme adopted by the utility model is: a production device of butyl benzyl phthalate, comprising a reaction kettle, the reaction kettle comprising a kettle body and a jacket arranged outside the kettle body, a spiral coil arranged inside the jacket, a stirring device arranged on the kettle body, the stirring device comprising a stirring shaft arranged on the kettle body, stirring blades arranged on the stirring shaft and a stirring motor connected to the stirring shaft, a benzyl chloride storage tank and a triethylamine storage tank arranged above the kettle body, the benzyl chloride storage tank and the kettle body as well as the kettle body and the triethylamine storage tank are respectively connected through a raw material conveying device, the raw material conveying device comprises a raw material conveying pipe and a liquid flow sensor, a first regulating valve, a quantitative tank and a second regulating valve arranged in sequence along the direction from close to the kettle body to far away from the kettle body on the raw material conveying pipe, and a temperature sensor and a pH sensor are arranged on the kettle body.

[0007] Preferably, the quantitative tank is provided with an observation window, the observation window is provided with a scale layer, and the top of the triethylamine storage tank and the top of the corresponding quantitative tank, as well as the top of the benzyl chloride storage tank and the top of the corresponding quantitative tank are respectively connected through a pressure balance pipe.

[0008] Preferably, the kettle body is provided with an inlet end of a first drain pipe, the outlet end of the first drain pipe is connected with a second drain pipe and a third drain pipe, the first drain pipe is sequentially provided with a third regulating valve and a liquid separator mirror along the direction from close to the kettle body to away from the kettle body, the second drain pipe and the third drain pipe are respectively provided with a first stop valve, and the kettle body is provided with a first liquid level sensor.

[0009] Preferably, the gas phase outlet end of the kettle is provided with the inlet end of the first gas phase delivery pipe, the inlet end of the first gas phase delivery pipe is connected to the raw material inlet end of the distillation tower, the reflux end of the kettle and the bottom of the distillation tower are connected through the reflux liquid delivery pipe, the top of the distillation tower is connected to the inlet end of the heat source channel of the first heat exchanger, and the outlet end of the heat source channel of the first heat exchanger is connected to the raw material inlet end of the cyclone separator.

[0010] Preferably, a second gas-phase delivery pipe is arranged between the first heat exchanger and the distillation tower, a second stop valve is arranged on the second gas-phase delivery pipe, a third stop valve and a first pressure sensor are arranged in sequence on the first gas-phase delivery pipe along the direction from close to the distillation tower to away from the distillation tower, a fourth stop valve is arranged on the reflux liquid delivery pipe, the first gas-phase delivery pipe between the third stop valve and the first pressure sensor is connected to the inlet end of the third gas-phase delivery pipe, the outlet end of the third gas-phase delivery pipe is connected to the heat source channel of the first heat exchanger, and the third gas-phase delivery pipe is arranged with a vacuum pump and a fifth stop valve in sequence along the direction from close to the first heat exchanger to away from the first heat exchanger.

[0011] Preferably, it also includes a steam delivery main pipe, an aeration pipe is arranged on the kettle body, aeration holes are arranged on the bottom of the aeration pipe, the top of the aeration pipe and the steam delivery main pipe, as well as the steam delivery main pipe and the inner cavity of the jacket outside the spiral coil are respectively connected through steam delivery branch pipes, and the steam delivery branch pipes are sequentially provided with gas flow sensors and a fourth regulating valve along the direction away from the steam delivery main pipe to close to the steam delivery main pipe.

[0012] Preferably, the liquid phase inlet end of the cyclone separator is connected to a first recovery tank, and the first recovery tank and the cyclone separator are connected through a liquefaction recovery pipe. The number of first recovery tanks is several, and the number of liquefaction recovery pipes corresponds to the number of first recovery tanks. A sixth stop valve is correspondingly arranged on each liquefaction recovery pipe, and the spiral coil is connected to the inlet end of the heat source channel of the second heat exchanger, and the outlet end of the heat source channel of the second heat exchanger is connected to the second recovery tank. The second recovery tank and the first recovery tank are respectively provided with a second liquid level sensor, a ventilation valve and a fourth liquid discharge pipe, and the fourth liquid discharge pipe is provided with a seventh stop valve.

[0013] The utility model has the following beneficial effects: firstly, a benzyl chloride storage tank and a triethylamine storage tank are arranged above the kettle body of the utility model, the benzyl chloride storage tank and the kettle body, and the kettle body and the triethylamine storage tank are respectively connected through a raw material conveying device, the raw material conveying device comprises a raw material conveying pipe and a liquid flow sensor, a first regulating valve, a quantitative tank and a second regulating valve which are arranged in sequence along the raw material conveying pipe in a direction from close to the kettle body to far away from the kettle body, so that the feeding speed of the benzyl chloride and the triethylamine can be controlled conveniently, and the kettle body is provided with a temperature sensor and a pH sensor to realize the feedback of the temperature of the medium in the kettle body and the pH of the medium in the kettle body during the adding process of the benzyl chloride and the triethylamine, and the feeding speed of the benzyl chloride and the triethylamine is further adjusted according to the temperature of the medium in the kettle body and the pH of the medium in the kettle body, so as to reduce the phenomenon of the reaction kettle being rushed due to the adding speed of the benzyl chloride and the triethylamine being too fast.

[0014] Secondly, the first gas phase conveying pipe of the utility model is sequentially provided with a third stop valve and a first pressure sensor along the direction from close to the distillation tower to far away from the distillation tower. The installation of the first pressure sensor facilitates the feedback of the pressure parameters of the medium conveyed through the first gas phase conveying pipe.

[0015] Finally, the steam delivery branch pipe of the utility model is provided with a gas flow sensor, a second pressure sensor and a fourth regulating valve in sequence along the direction away from the steam delivery main pipe to close to the steam delivery main pipe; installing the gas flow sensor is convenient for feedback of the flow parameters of the gas medium transported through the steam delivery branch pipe, and installing the second pressure sensor is convenient for feedback of the pressure parameters of the gas medium transported through the steam delivery branch pipe.

[0016] The utility model has the advantages of simple structure, convenient operation, ingenious design, greatly improved work efficiency, good social and economic benefits, and is a product that is easy to promote and use. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] Figure 1 It is a structural schematic diagram of the utility model.

[0018] Figure 2 for Figure 1 A partial enlarged schematic diagram of detail A.

[0019] Figure 3 for Figure 1 A partial enlarged schematic diagram of detail B. DETAILED DESCRIPTION

[0020] like Figures 1 to 3As shown, a production device for butyl benzyl phthalate comprises a reactor 1, wherein the reactor 1 comprises a reactor body and a jacket arranged outside the reactor body, a spiral coil 2 is arranged inside the jacket, and the spiral coil 2 is fitted with the reactor body, a stirring device is arranged on the reactor body, and the stirring device comprises a stirring shaft 3 arranged on the reactor body, a stirring blade 4 arranged on the stirring shaft 3, and a stirring motor 5 connected to the stirring shaft 3 by transmission, a benzyl chloride storage tank 6 and a triethylamine storage tank 7 are arranged above the reactor body, the benzyl chloride storage tank 6 and the reactor body, and the reactor body and the triethylamine storage tank 7 are respectively connected through a raw material conveying device, the raw material conveying device comprises a raw material conveying pipe 8 and a liquid flow sensor 9, a first regulating valve 10, a quantitative tank 11, and a second regulating valve 12 arranged in sequence along the direction from close to the reactor body to away from the reactor body, and a temperature sensor 13 and a pH sensor 14 are arranged on the reactor body. The quantitative tank 11 is provided with an observation window 15, which is a sheet structure made of a transparent material. A scale layer 16 is provided on the observation window 15. The top of the triethylamine storage tank 7 and the top of the corresponding quantitative tank 11, as well as the top of the benzyl chloride storage tank 6 and the top of the corresponding quantitative tank 11 are respectively connected through a pressure balance pipe 17.

[0021] The kettle body is provided with an inlet end of a first drain pipe 18, and the outlet end of the first drain pipe 18 is connected to a second drain pipe 19 and a third drain pipe 20. The first drain pipe 18 is provided with a third regulating valve 21 and a liquid separator mirror 22 in sequence along the direction from close to the kettle body to away from the kettle body. The second drain pipe 19 and the third drain pipe 20 are respectively provided with a first stop valve 23, and the kettle body is provided with a first liquid level sensor 24.

[0022] The inlet end of the first gas-phase delivery pipe 25 is provided on the gas phase outlet end of the kettle, and the inlet end of the first gas-phase delivery pipe 25 is connected to the raw material inlet end of the distillation tower 26, the reflux end of the kettle and the bottom of the distillation tower 26 are connected through the reflux liquid delivery pipe 27, the inlet end of the heat source channel of the first heat exchanger 28, and the outlet end of the heat source channel of the first heat exchanger 28 are connected to the raw material inlet end of the cyclone separator 29. The inlet end of the first gas-phase delivery pipe 25 is provided on the gas phase outlet end of the kettle, and the inlet end of the first gas-phase delivery pipe 25 is connected to the raw material inlet end of the distillation tower 26, the reflux end of the kettle and the bottom of the distillation tower 26 are connected through the reflux liquid delivery pipe 27, the top of the distillation tower 26 is connected to the inlet end of the heat source channel of the first heat exchanger 28, and the outlet end of the heat source channel of the first heat exchanger 28 is connected to the raw material inlet end of the cyclone separator 29.

[0023] A second gas phase delivery pipe 30 is arranged between the first heat exchanger 28 and the distillation tower 26, and a second stop valve 31 is arranged on the second gas phase delivery pipe 30. A third stop valve 32 and a first pressure sensor 33 are arranged in sequence on the first gas phase delivery pipe 25 along the direction from close to the distillation tower 26 to far away from the distillation tower 26, and a fourth stop valve 34 is arranged on the reflux liquid delivery pipe 27. The first gas phase delivery pipe 25 between the third stop valve 32 and the first pressure sensor 33 is connected to the inlet end of the third gas phase delivery pipe 35, and the outlet end of the third gas phase delivery pipe 35 is connected to the heat source channel of the first heat exchanger 28. The third gas phase delivery pipe 35 is sequentially provided with a vacuum pump 36 and a fifth stop valve 37 along the direction from close to the first heat exchanger 28 to far away from the first heat exchanger 28.

[0024] Since the generated butyl benzyl phthalate product needs to be subjected to a post-treatment process, that is, high-pressure steam needs to be introduced into the jacket at the same time as the generated butyl benzyl phthalate product. The light components in the generated butyl benzyl phthalate product are vaporized after being heated and discharged together with the discharged high-pressure steam, and the inorganic salt components in the generated butyl benzyl phthalate product are dissolved in the liquefied high-pressure steam to form a water phase, which is fully stirred and allowed to stand to separate into an organic phase and an inorganic phase to achieve the technical purpose of removing impurities. Therefore, the product also includes a steam delivery main pipe 38, and the kettle body An aeration pipe 39 is arranged on the top, and aeration holes 40 are arranged on the bottom of the aeration pipe 39. The number of aeration holes 40 is adopted, and the plurality of aeration holes 40 are evenly distributed at the bottom of the aeration pipe 39. The top end of the aeration pipe 39 and the steam delivery main pipe 38 as well as the steam delivery main pipe 38 and the inner cavity of the jacket outside the spiral coil 2 are connected through a steam delivery branch pipe 41 respectively. The steam delivery branch pipe 41 is sequentially provided with a gas flow sensor 42, a second pressure sensor 53 and a fourth regulating valve 43 along the direction away from the steam delivery main pipe 38 to close to the steam delivery main pipe 38. The liquid phase inlet end of the cyclone separator 29 is connected to the first recovery tank 44, and the first recovery tank 44 and the cyclone separator 29 are connected through a liquefaction recovery pipe 45. The number of first recovery tanks 44 is several, and the number of liquefaction recovery pipes 45 corresponds to the number of first recovery tanks 44. A sixth stop valve 46 is correspondingly provided on each liquefaction recovery pipe 45. The spiral coil 2 is connected to the inlet end of the heat source channel of the second heat exchanger 47, and the outlet end of the heat source channel of the second heat exchanger 47 is connected to the second recovery tank 48. The benzyl chloride storage tank 6, the triethylamine storage tank 7, the second recovery tank 48 and the first recovery tank 44 are respectively provided with a second liquid level sensor 49 and a ventilation valve 50. The second recovery tank 48 and the first recovery tank 44 are respectively provided with a fourth liquid discharge pipe 51, and the fourth liquid discharge pipe 51 is provided with a seventh stop valve 52.

[0025] The usage of this product is as follows: Figures 1 to 3 As shown, the following steps are included:

[0026] S1. This step is an esterification reaction, which includes firstly adding 1KmoL of phthalic anhydride and 1.05KmoL of n-butanol into the kettle body of the reactor 1, controlling the high-pressure steam to be introduced into the jacket of the reactor 1 through the corresponding steam delivery branch pipe 41, maintaining the pressure of the high-pressure steam at 0.2Mpa, and starting to slowly increase the temperature. When the phthalic anhydride is completely dissolved, the high-pressure steam is stopped from being continuously delivered to the jacket of the reactor 1. After the dissolution is completed, the temperature parameter fed back by the temperature sensor 13 installed on the kettle body of the reactor 1 does not exceed 140°C; then the reaction temperature is controlled at 100°C to 105°C for 1 hour.

[0027] Since the boiling point of n-butanol is 117.7°C and the boiling point of phthalic anhydride is 284.5°C, the boiling point of phthalic anhydride is higher than that of n-butanol; in step S1, the gas discharged from the top of the distillation tower 26 contains a large amount of n-butanol, and therefore the gas discharged from the top of the distillation tower 26 is transported to the heat source channel of the first heat exchanger 28 for heat exchange with the medium continuously transported to the cold source channel of the first heat exchanger 28, and then transported to one of the first recovery tanks 44 for recovery.

[0028] S2, this step is an esterification reaction, 1KmoL of caustic soda solution is gradually added to the kettle body of the reactor 1 that has completed step S1, and circulating water is introduced into the spiral coil 2 during the process of adding caustic soda solution. During the process of adding caustic soda solution, the temperature parameter fed back by the temperature sensor 13 installed on the kettle body of the reactor 1 is between 65°C and 70°C; when the caustic soda solution is added, the kettle body of the reactor 1 is gradually saturated with soda ash solution, and the data fed back by the pH sensor 14 installed on the kettle body of the reactor 1 is between 8.5 and 9.0; when the saturated soda ash solution is added, After that, the circulating water into the spiral coil 2 is stopped, and high-pressure steam is introduced into the jacket of the reactor 1. The pressure of the high-pressure steam is maintained at 0.2Mpa, and the reactor body of the reactor 1 begins to gradually heat up; finally, the benzyl chloride storage tank 6 and the triethylamine storage tank 7 are both delivered to the corresponding quantitative tank 11 to deliver the liquid medium to a preset liquid level height. In the process of the quantitative tank 11 receiving the liquid medium, since the liquid medium enters the quantitative tank 11, the air originally in the quantitative tank 11 is delivered to the corresponding benzyl chloride storage tank 6 or the triethylamine storage tank 7, thereby maintaining the pressure balance of the quantitative tank 11 in the process of receiving the liquid medium.

[0029] In step S2, the product sodium salt of monobutyl phthalate is a weak acid and strong base salt. After the reaction is completed, the material is controlled to be weakly alkaline, which is conducive to maintaining the stability of the product. In this step, the gas discharged from the top of the distillation tower 26 contains a large amount of n-butanol, and the first recovery tank 44 described in step S1 continues to receive the material that is liquefied after heat exchange in the first heat exchanger 28.

[0030] S3, this step is a condensation reaction. After the temperature parameter fed back by the temperature sensor 13 installed on the kettle body of the reactor 1 is above 85°C, the raw material conveying device corresponding to the benzyl chloride storage tank 6 and the raw material conveying device corresponding to the triethylamine storage tank 7 are both opened to convey the medium into the reactor 1, and the flow rate of the medium conveyed by the raw material conveying device to the kettle body of the reactor 1 is fed back by the corresponding liquid flow sensor 9, and the flow rate of the medium conveyed by the raw material conveying device to the kettle body of the reactor 1 is adjusted by the corresponding first regulating valve 10; when the temperature sensor 13 installed on the kettle body of the reactor 1 feeds back After the temperature parameter fed back is above 100°C, the distillation tower 26 transports the reflux liquid to the kettle body of the reactor 1 through the reflux liquid transport pipe 27, and the amount of high-pressure steam transported to the jacket of the reactor 1 is reasonably adjusted to maintain the temperature parameter fed back by the temperature sensor 13 installed on the kettle body of the reactor 1 at 110°C to 112°C during the addition of benzyl chloride and triethylamine to the reactor 1, and the data fed back by the pH sensor 14 installed on the kettle body of the reactor 1 is between 8.5 and 9.0. The condensation reaction can be stopped after 4 hours of reaction, and the jacket of the reactor 1 stops receiving the high-pressure steam.

[0031] Step S3 is a condensation reaction. During this step, if the temperature parameter fed back by the temperature sensor 13 installed on the kettle body of the reactor 1 is higher than the preset temperature, the supply of benzyl chloride and triethylamine into the kettle body of the reactor 1 should be stopped to maintain the temperature parameter fed back by the temperature sensor 13 installed on the kettle body of the reactor 1 at 110°C to 112°C. In addition, since the maximum reaction temperature of this step is below 112°C, the gas discharged from the top of the distillation tower 26 contains a large amount of n-butanol, and the first recovery tank 44 described in step S1 and step S2 still continues to receive the liquefied material after heat exchange by the first heat exchanger 28.

[0032] S4, this step is a water washing step. After the completion of step S3, the synthesis of crude butyl benzyl phthalate has been completed in the kettle body of the reactor 1. In this step, the light components and inorganic salt components of the crude butyl benzyl phthalate need to be removed, specifically as follows: First, the jacket of the reactor 1 receives high-pressure steam, and the pressure of the high-pressure steam is 0.3 to 0.4Mpa; then, when the temperature parameter fed back by the temperature sensor 13 installed in the kettle body of the reactor 1 is at 100°C, the aeration pipe 39 receives the high-pressure steam and delivers the high-pressure steam to the medium in the kettle body of the reactor 1 through the aeration hole 40. At the same time, the distillation tower 26 delivers reflux liquid to the kettle body of the reactor 1 through the reflux liquid delivery pipe 27, and the delivery amount of the high-pressure steam is controlled to maintain the temperature parameter fed back by the temperature sensor 13 installed in the kettle body of the reactor 1 not greater than 140°C, and the reaction time is maintained not less than 5 hours. When the reaction is completed, the aqueous phase layer in the reactor body of the reactor 1 is discharged outward through the first discharge pipe 18 and the second discharge pipe 19 in turn. When the liquid separation mirror 22 is fed back to the boundary surface between the organic phase and the aqueous phase, the discharge of the aqueous phase layer in the reactor body of the reactor 1 is stopped.

[0033] In step S4, since a large amount of water vapor is directly introduced into the reactor body of the reactor 1, the medium transported outward from the top of the distillation tower 26 is composed of n-butanol carried by water vapor. Compared with the gas discharged from the top of the distillation tower 26 in steps S1, S2 and S3, the content of n-butanol in the gas is greatly reduced. Therefore, another first recovery tank 44 should be replaced to receive the material liquefied after heat exchange in the first heat exchanger 28.

[0034] S5. The staff detects the butyl benzyl phthalate that has completed step S4 in the reactor body of the reactor 1 to see whether it meets the corresponding index requirements. If it does not meet the corresponding index requirements, step S4 is performed again; if it meets the corresponding index requirements, the corresponding butyl benzyl phthalate is transported to the next process through the first liquid discharge pipe 18 and the third liquid discharge pipe 20 in sequence.

[0035] Through the embodiment, the above kettle body of the product is provided with a benzyl chloride storage tank 6 and a triethylamine storage tank 7, the benzyl chloride storage tank 6 and the kettle body, and the kettle body and the triethylamine storage tank 7 are respectively connected through a raw material conveying device, the raw material conveying device comprises a raw material conveying pipe 8 and a liquid flow sensor 9, a first regulating valve 10, a quantitative tank 11 and a second regulating valve 12 arranged in sequence along the direction from close to the kettle body to far away from the kettle body, so as to realize the convenient control of the feeding speed of benzyl chloride and triethylamine, and the kettle body is provided with a temperature sensor 13 and a pH sensor 14 to realize the feedback of the temperature of the medium in the kettle body and the pH of the medium in the kettle body during the addition of benzyl chloride and triethylamine, and the feeding speed of benzyl chloride and triethylamine is further adjusted according to the temperature of the medium in the kettle body and the pH of the medium in the kettle body, thereby reducing the phenomenon of material rushing in the reaction kettle due to the addition of benzyl chloride and triethylamine too fast.

[0036] The embodiments described above are only preferred embodiments of the present invention and are not intended to limit the scope of implementation of the present invention. Therefore, any equivalent changes or modifications made based on the structures, features and principles described in the patent scope of the present invention should be included in the patent application scope of the present invention.

Claims

1. A production device for butyl benzyl phthalate, comprising a reaction kettle (1), wherein the reaction kettle (1) comprises a kettle body and a jacket arranged outside the kettle body, characterized in that: A spiral coil (2) is arranged inside the jacket, and a stirring device is arranged on the kettle body. The stirring device comprises a stirring shaft (3) arranged on the kettle body, a stirring blade (4) arranged on the stirring shaft (3), and a stirring motor (5) connected to the stirring shaft (3). A benzyl chloride storage tank (6) and a triethylamine storage tank (7) are arranged above the kettle body. The benzyl chloride storage tank (6) and the kettle body, and the kettle body and the triethylamine storage tank (7) are respectively connected through a raw material conveying device. The raw material conveying device comprises a raw material conveying pipe (8) and a liquid flow sensor (9), a first regulating valve (10), a quantitative tank (11), and a second regulating valve (12) arranged in sequence along the raw material conveying pipe (8) from close to the kettle body to away from the kettle body. A temperature sensor (13) and a pH sensor (14) are arranged on the kettle body.

2. The production device of butyl benzyl phthalate according to claim 1, characterized in that: The quantitative tank (11) is provided with an observation window (15), and a scale layer (16) is provided on the observation window (15). The top of the triethylamine storage tank (7) and the top of the corresponding quantitative tank (11) as well as the top of the benzyl chloride storage tank (6) and the top of the corresponding quantitative tank (11) are respectively connected via a pressure balance pipe (17).

3. The production device of butyl benzyl phthalate according to claim 1, characterized in that: The kettle body is provided with an inlet end of a first liquid discharge pipe (18), and the outlet end of the first liquid discharge pipe (18) is connected with a second liquid discharge pipe (19) and a third liquid discharge pipe (20). The first liquid discharge pipe (18) is provided with a third regulating valve (21) and a liquid separation sight glass (22) in sequence from close to the kettle body to far away from the kettle body. The second liquid discharge pipe (19) and the third liquid discharge pipe (20) are respectively provided with a first stop valve (23). The kettle body is provided with a first liquid level sensor (24).

4. The production device of butyl benzyl phthalate according to claim 1, characterized in that: The gas phase outlet end of the kettle body is provided with the inlet end of a first gas phase delivery pipe (25), the inlet end of the first gas phase delivery pipe (25) is connected to the raw material inlet end of a distillation tower (26), the reflux end of the kettle body and the bottom of the distillation tower (26) are connected via a reflux liquid delivery pipe (27), the top of the distillation tower (26) and the inlet end of a heat source channel of a first heat exchanger (28) are connected, and the outlet end of the heat source channel of the first heat exchanger (28) is connected to the raw material inlet end of a cyclone separator (29).

5. The production device of butyl benzyl phthalate according to claim 4, characterized in that: A second gas phase delivery pipe (30) is provided between the first heat exchanger (28) and the distillation tower (26), a second stop valve (31) is provided on the second gas phase delivery pipe (30), a third stop valve (32) and a first pressure sensor (33) are provided in sequence on the first gas phase delivery pipe (25) in a direction from close to the distillation tower (26) to far away from the distillation tower (26), a fourth stop valve (34) is provided on the reflux liquid delivery pipe (27), the first gas phase delivery pipe (25) between the third stop valve (32) and the first pressure sensor (33) is connected to the inlet end of the third gas phase delivery pipe (35), the outlet end of the third gas phase delivery pipe (35) is connected to the heat source channel of the first heat exchanger (28), and a vacuum pump (36) and a fifth stop valve (37) are provided in sequence on the third gas phase delivery pipe (35) in a direction from close to the first heat exchanger (28) to far away from the first heat exchanger (28).

6. The production device of butyl benzyl phthalate according to claim 5, characterized in that: The kettle body is provided with an aeration pipe (39), the bottom of the aeration pipe (39) is provided with an aeration hole (40), the top of the aeration pipe (39) and the steam transport main pipe (38) as well as the steam transport main pipe (38) and the inner cavity of the jacket outside the spiral coil (2) are connected through a steam transport branch pipe (41), and the steam transport branch pipe (41) is provided with a gas flow sensor (42) and a fourth regulating valve (43) in sequence along the direction away from the steam transport main pipe (38) to close to the steam transport main pipe (38).

7. The production device of butyl benzyl phthalate according to claim 5, characterized in that: The liquid phase inlet end of the cyclone separator (29) is connected to a first recovery tank (44). The first recovery tank (44) and the cyclone separator (29) are connected via a liquefied recovery pipe (45). The number of first recovery tanks (44) is multiple, and the number of liquefied recovery pipes (45) corresponds to the number of first recovery tanks (44). A sixth stop valve (46) is correspondingly provided on each liquefied recovery pipe (45). The spiral coil (2) is connected to an inlet end of a heat source channel of a second heat exchanger (47). The outlet end of the heat source channel of the second heat exchanger (47) is connected to a second recovery tank (48). The second recovery tank (48) and the first recovery tank (44) are respectively provided with a second liquid level sensor (49), a ventilation valve (50) and a fourth liquid discharge pipe (51). The fourth liquid discharge pipe (51) is provided with a seventh stop valve (52).

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