2-nitro-3-methylbenzoyl chloride methylamine reaction production apparatus

Abstract

The utility model provides a kind of 2-nitro-3-methyl benzoyl chloride methylamine reaction's production device, belong to fine chemical technology field, including reaction unit, reaction unit is equipped with amination kettle, amination kettle is used to make reaction raw materials occur reaction in amination kettle to generate reaction product;Liquid separation unit, the feed inlet of liquid separation unit is communicated with the discharge port of amination kettle, to carry out layering to reaction product, obtain liquid separation product;Alkaline washing unit, the feed inlet of alkaline washing unit is communicated with the discharge port of liquid separation unit, to carry out alkaline washing to liquid separation product, obtain alkali washing product;Desolventizing unit, the feed inlet of desolventizing unit is communicated with the discharge port of alkaline washing unit, to carry out desolventizing to alkali washing product, obtain desolventizing product.The production device utilizes 2-nitro-3-methyl benzoyl chloride and methylamine reaction to generate 2-nitro-N,3-dimethyl benzamide, reaction condition is mild, reaction time is short, raw material utilization is high, process operation is simple, product yield and production efficiency are high.

Description

Technical Field

[0001] This utility model relates to the field of fine chemical technology, and in particular to a production apparatus for the methylamine reaction of 2-nitro-3-methylbenzoyl chloride. Background Technology

[0002] 2-Nitro-N,3-Dimethylbenzamide, with the molecular formula C9H 12 N₂O, with a molecular weight of 164.2044 and CAS number 870997-57-2, is an intermediate for 2-nitro-N,3-dimethylbenzamide, a key raw material for the highly effective, low-toxicity insecticide chlorantraniliprole, K-amine (2-amino-3-methyl-5-chlorobenzoic acid). The existing synthetic method involves adding methyl 2-nitro-3-methylbenzoate to a methanol solution containing a certain amount of monomethylamine, then refluxing the reaction mixture to generate 2-nitro-N,3-dimethylbenzamide. The disadvantages of this synthesis method are as follows: 1) Long reaction time, typically exceeding 5 hours, resulting in low production efficiency; 2) Low single-pass conversion rate, as methyl 2-nitro-3-methylbenzoate is difficult to react completely, with a yield of only about 80%; 3) Low utilization rate of monomethylamine, with monomethylamine escaping during reflux, requiring absorption treatment, and the obtained product must be purified to meet usage requirements; 4) Post-treatment generates large amounts of wastewater and inorganic salts, significantly impacting clean production. Therefore, there is a need to provide a production apparatus for 2-nitro-N,3-dimethylbenzamide with mild reaction conditions, short reaction time, simple process operation, and high product yield to expand production capacity and increase economic benefits. Utility Model Content

[0003] This invention provides a production apparatus for the methyl amination reaction of 2-nitro-3-methylbenzoyl chloride, which features mild reaction conditions, short reaction time, simple process operation, and high product yield, in order to solve the problems of low raw material utilization, low product yield, and low production efficiency of existing production apparatuses.

[0004] Specifically, this utility model provides a production apparatus for the methylamine reaction of 2-nitro-3-methylbenzoyl chloride, comprising:

[0005] The reaction unit is equipped with an amination vessel, which is used to react the reactants to generate the reaction product, which is 2-nitro-N,3-dimethylbenzamide.

[0006] The liquid separation unit has its inlet connected to the outlet of the amination vessel to separate the reaction products into liquid products.

[0007] The alkaline washing unit has its inlet connected to the outlet of the separation unit to perform alkaline washing on the separation product to obtain the alkaline washed product.

[0008] The desolvation unit has its inlet connected to the outlet of the alkaline washing unit to desolvate the alkaline washing product and obtain a desolvated product, which is crude 2-nitro-N,3-dimethylbenzamide.

[0009] Furthermore, the inlet of the amination reactor is connected to the outlet of a feed storage tank, which includes a dichloroethane storage tank, a monomethylamine liquid storage tank, a liquid alkali tank, and a high-level tank. The high-level tank stores 2-nitro-3-methylbenzoyl chloride. The outlets of the dichloroethane storage tank, the monomethylamine liquid storage tank, the liquid alkali tank, and the high-level tank are all connected to the inlet of the amination reactor. A metering pump is installed between the liquid alkali tank and the high-level tank and the amination reactor.

[0010] Furthermore, the outlet of the amination reactor is connected to the inlet of the water separator of the liquid separation unit, and the outlet of the water separator is connected to the alkaline washing unit; the upper part of the water separator is provided with a water outlet, which is connected in sequence to the stratified water collection vessel and the filter tank; the filter cake outlet of the filter tank is connected to the reuse port of the water separator.

[0011] Furthermore, the alkaline washing unit is equipped with at least two alkaline washing vessels. The outlet of the water separation vessel is connected in sequence to the inlet of the primary alkaline washing vessel and the secondary alkaline washing vessel. The inlets of the primary and secondary alkaline washing vessels are also connected to the outlet of the alkaline water tank. The outlet of the secondary alkaline washing vessel is connected to the desolvation unit. The upper part of the primary and secondary alkaline washing vessels is equipped with a liquid outlet, which is connected to the stratified water collection vessel.

[0012] Furthermore, the solvent removal unit is equipped with a solvent removal kettle, the inlet of which is connected to the outlet of the secondary alkaline washing kettle; the solvent outlet of the solvent removal kettle is connected to the inlet of the pickling kettle, and the outlet of the pickling kettle is connected to the inlet of the dichloroethane storage tank; the solvent removal unit is also equipped with a water tank and a hydrochloric acid tank, and the outlets of the water tank and the hydrochloric acid tank are connected to the inlets of the solvent removal kettle and the pickling kettle respectively through pipelines.

[0013] Furthermore, the production unit also includes a purification unit, the inlet of which is connected to the outlet of the desolventizing unit, so as to wash and dry the desolventized product to obtain a purified product, which is a high-quality 2-nitro-N,3-dimethylbenzamide.

[0014] Furthermore, the purification unit is equipped with a two-in-one reactor. The inlet of the two-in-one reactor is connected to the outlet of the desolvation unit, the outlet of the two-in-one reactor is connected to the inlet of the dryer, and the outlet of the dryer is connected to the refined product storage tank.

[0015] Furthermore, the feed inlet of the two-in-one reactor is also connected to the outlet of the water tank; the top of the two-in-one reactor is equipped with an air inlet, which is connected to a nitrogen pipeline; the filtrate outlet of the two-in-one reactor is connected to a sewage tank.

[0016] Furthermore, the filtrate outlet of the filter tank is connected to the sewage tank.

[0017] The production apparatus for the methyl amination reaction of 2-nitro-3-methylbenzoyl chloride provided by this utility model utilizes the reaction of 2-nitro-3-methylbenzoyl chloride with monomethylamine to generate 2-nitro-N,3-dimethylbenzamide. The reaction is carried out in the amination vessel of the reaction unit, and the use of a metering pump can avoid side reactions and product condensation caused by local overheating in the amination vessel. It also facilitates precise control of the reaction rate, avoids temperature runaway, shortens the reaction time, improves selectivity and raw material conversion rate, and has mild reaction conditions, resulting in high product yield and improved production efficiency. The reaction yield of 2-nitro-N,3-dimethylbenzamide is greater than 98%, and its liquid chromatography content in the reaction product is greater than 98%.

[0018] The production unit operates continuously with each unit in a non-hazardous manner. It can be automated to further precisely control reaction and production conditions. The process is simple to operate, and the safety and cleanliness of subsequent production are guaranteed, which is conducive to large-scale industrial production.

[0019] The production unit utilizes a liquid separation unit and an alkaline washing unit to remove impurities, byproducts, and water from the reaction products, which helps to improve the purity of the target product. The solvent removal unit recovers the solvent for further reuse, and the purification unit further refines the crude target product. Wastewater is collected for subsequent purification and reuse, which can significantly reduce the amount of production water used and achieve zero emissions, making the production process green, environmentally friendly, and economical. Attached Figure Description

[0020] To more clearly illustrate the technical solutions in the embodiments of this utility model or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0021] Figure 1 A schematic diagram of the production apparatus for the methylamination reaction of 2-nitro-3-methylbenzoyl chloride provided in one embodiment of the present invention;

[0022] Figure 2 A schematic diagram of the production apparatus for the methylamination reaction of 2-nitro-3-methylbenzoyl chloride provided in another embodiment of the present invention;

[0023] Figure 3 A schematic diagram of the production apparatus for the methylamine reaction of 2-nitro-3-methylbenzoyl chloride provided in another embodiment of this utility model.

[0024] Explanation of reference numerals in the attached figures:

[0025] 101-Amination reactor, 102-Dichloroethane storage tank, 103-Methylamine liquid storage tank, 104-Liquid alkali tank, 105-High-level tank, 106-Quantitative pump, 201-Water separator, 202-Separated water collection reactor, 203-Filter tank, 301-Primary alkali washing reactor, 302-Secondary alkali washing reactor, 303-Alkali water tank, 401-Desolventizing reactor, 402-Acid washing reactor, 403-Water tank, 404-Hydrochloric acid tank, 501-Two-in-one reaction vessel, 502-Dryer, 503-Refined product storage tank, 504-Sewage pool. Detailed Implementation

[0026] To make the objectives, technical solutions, and advantages of the embodiments of this utility model clearer, the technical solutions in the embodiments of this utility model are described clearly and completely below. Obviously, the described embodiments are only some embodiments of this utility model, not all embodiments. Based on the embodiments of this utility model, all other embodiments obtained by those skilled in the art without creative effort are also within the protection scope of this utility model.

[0027] Specifically, such as Figure 1 As shown, this utility model provides a production apparatus for the methylamine reaction of 2-nitro-3-methylbenzoyl chloride, comprising:

[0028] The reaction unit is equipped with an amination vessel 101, which is used to react the reactants to generate the reaction product, which is 2-nitro-N,3-dimethylbenzamide.

[0029] The liquid separation unit has its inlet connected to the outlet of the amination vessel 101 to separate the reaction products into layers and obtain the liquid separation product.

[0030] The alkaline washing unit has its inlet connected to the outlet of the separation unit to perform alkaline washing on the separation product to obtain the alkaline washed product.

[0031] The desolvation unit has its inlet connected to the outlet of the alkaline washing unit to desolvate the alkaline washing product and obtain a desolvated product, which is crude 2-nitro-N,3-dimethylbenzamide.

[0032] The production apparatus of this invention utilizes the reaction of 2-nitro-3-methylbenzoyl chloride with monomethylamine to generate 2-nitro-N,3-dimethylbenzamide, unlike the reaction using methyl 2-nitro-3-methylbenzoate as a raw material. The reaction unit enables rapid mixing and reaction of 2-nitro-3-methylbenzoyl chloride and monomethylamine without the need for reflux reaction, thus shortening the reaction time, increasing the raw material conversion rate, improving production efficiency, and providing mild reaction conditions, simple process operation, high product yield, and ensuring the safety and cleanliness of subsequent production. It is a non-hazardous process with minimal production safety risks, which is conducive to large-scale and industrialized production.

[0033] like Figure 1 As shown, further, the inlet of the amination reactor 101 is connected to the outlet of a feed storage tank, which includes a dichloroethane storage tank 102, a monomethylamine liquid storage tank 103, a liquid alkali tank 104, and a high-level tank 105. The high-level tank 105 stores 2-nitro-3-methylbenzoyl chloride. The outlets of the dichloroethane storage tank 102, the monomethylamine liquid storage tank 103, the liquid alkali tank 104, and the high-level tank 105 are all connected to the inlet of the amination reactor 101. A metering pump 106 is respectively installed between the liquid alkali tank 104 and the high-level tank 105 and the amination reactor 101.

[0034] Dichloroethane is first added as a solvent to the amination reactor 101, followed by monomethylamine, one of the reaction raw materials. Finally, 2-nitro-3-methylbenzoyl chloride and liquid alkali are added dropwise to the amination reactor 101 through a metering pump 106. The dropping temperature and the reaction temperature in the amination reactor 101 are controlled to be ≤30℃. The reaction conditions are mild, which improves the safety of the entire process. The reaction time can be controlled within 2-3 hours, shortening the reaction cycle, significantly improving production efficiency, and effectively reducing production time and costs.

[0035] The use of a metering pump 106 for feeding the liquid alkali tank 104 and the high-level tank 105 avoids side reactions and product polycondensation caused by localized overheating in the amination reactor 101, and also prevents temperature runaway. It also facilitates precise control of the reaction rate, improving reaction selectivity and conversion rate. Furthermore, commonly used heat exchange components and stirring components can be installed in the amination reactor 101. The heat exchange components facilitate timely transfer of reaction heat and control of the reaction temperature, while the stirring components disperse and mix the reactants, ensuring a rapid and complete reaction.

[0036] like Figure 2 As shown, further, the outlet of the amination vessel 101 is connected to the inlet of the water separator 201 of the liquid separation unit, and the outlet of the water separator 201 is connected to the alkaline washing unit; the upper part of the water separator 201 is provided with a water outlet, which is connected in sequence to the stratified water collection vessel 202 and the filter tank 203; the filter cake outlet of the filter tank 203 is connected to the reuse port of the water separator 201.

[0037] The separation unit mainly removes water from the material discharged from the amination vessel 101. The lower organic phase, i.e. the separation product, is further purified. The upper aqueous phase is collected in the stratified water collection vessel 202 and separated into layers again. It is then filtered in the filter tank 203. The resulting filter cake contains reaction products and is sent back to the water separation vessel 201 for recycling. This process removes non-target products while increasing the yield of the target product.

[0038] like Figure 2 As shown, the alkaline washing unit is further provided with at least two alkaline washing vessels. The outlet of the water separation vessel 201 is connected in sequence to the inlet of the primary alkaline washing vessel 301 and the secondary alkaline washing vessel 302. The inlets of the primary alkaline washing vessel 301 and the secondary alkaline washing vessel 302 are also connected to the outlet of the alkaline water tank 303. The outlet of the secondary alkaline washing vessel 302 is connected to the desolvation unit. The upper part of the primary alkaline washing vessel 301 and the secondary alkaline washing vessel 302 is provided with a liquid outlet, which is connected to the stratified water collection vessel 202.

[0039] The separated product is washed in an alkaline washing tank with 5% alkaline water from alkaline water tank 303 to remove impurities and by-products, and also to reduce the concentration and viscosity of the separated product, facilitating subsequent processing. After heating, the separated product is thoroughly stirred and then allowed to stand to separate into layers. The lower alkaline-washed product is sent to the desolvation unit, while the upper aqueous phase is similarly sent to the separation water collection tank 202 for processing. Separation and alkaline washing help improve the purity of the target product.

[0040] like Figure 2 As shown, the solvent removal unit further includes a solvent removal vessel 401, the inlet of which is connected to the outlet of the secondary alkaline washing vessel 302; the solvent outlet of the solvent removal vessel 401 is connected to the inlet of the pickling vessel 402, and the outlet of the pickling vessel 402 is connected to the inlet of the dichloroethane storage tank 102; the solvent removal unit also includes a water tank 403 and a hydrochloric acid tank 404, the outlets of which are connected to the inlets of the solvent removal vessel 401 and the pickling vessel 402 respectively via pipelines.

[0041] The alkaline washing product is desolvated at atmospheric pressure in desolvation kettle 401. Water and hydrochloric acid can be added to desolvation kettle 401 to adjust the pH to 6-7. The desolvated dichloroethane solvent is sent to acid washing kettle 402. After being adjusted to neutral with hydrochloric acid and water in solvent acid washing kettle 402, it is sent back to dichloroethane storage tank 102 for reuse, or it can be directly reused in the next batch of synthesis, significantly reducing the amount of new solvent used in the next batch of production, which is beneficial to reducing costs. It should be noted that since the recovered dichloroethane contains unreacted monomethylamine, when reusing or recycling, the discharge rate from the monomethylamine storage tank should be reduced according to the monomethylamine content in the mother liquor.

[0042] like Figure 3As shown, the production apparatus further includes a purification unit, the inlet of which is connected to the outlet of the desolventizing unit, so as to wash and dry the desolventized product to obtain a purified product, which is a high-quality 2-nitro-N,3-dimethylbenzamide.

[0043] like Figure 3 As shown, the purification unit is further equipped with a two-in-one reactor 501. The inlet of the two-in-one reactor 501 is connected to the outlet of the desolvation unit, the outlet of the two-in-one reactor 501 is connected to the inlet of the dryer 502, and the outlet of the dryer 502 is connected to the refined product storage tank 503.

[0044] like Figure 3 As shown, the feed inlet of the two-in-one reactor 501 is also connected to the outlet of the water tank 403; the top of the two-in-one reactor 501 is provided with an air inlet, which is connected to a nitrogen pipeline; the filtrate outlet of the two-in-one reactor 501 is connected to the sewage tank 504.

[0045] The crude 2-nitro-N,3-dimethylbenzamide, a product of solvent removal, is subjected to final washing, stirring, and crystallization in a two-in-one reactor 501. After nitrogen pressure filtration, the filtrate is treated in wastewater tank 504, and the filter cake is dried in dryer 502 to obtain the purified 2-nitro-N,3-dimethylbenzamide, which is temporarily stored in refined product storage tank 503 for subsequent reactions or sale. Dryer 502 can be a disc dryer.

[0046] like Figure 3 As shown, the filtrate outlet of filter tank 203 is further connected to wastewater tank 504. The water filtered out of filter tank 203 is also sent to wastewater tank 504 for sewage treatment. This wastewater can be reused in the production process after purification, which greatly reduces the amount of production water used, thereby achieving zero discharge in production.

[0047] The present invention will be further described in detail below with reference to specific embodiments.

[0048] In the production apparatus for the methyl amination reaction of 2-nitro-3-methylbenzoyl chloride, during operation, dichloroethane and a methylamine aqueous solution are fed into the amination reactor 101 through a dichloroethane storage tank 102 and a methylamine liquid storage tank 103 to lower the temperature of the material in the amination reactor 101 to below 10°C. Then, 3-methyl-2-nitrobenzoyl chloride and liquid alkali from the liquid alkali tank 104 and the high-level tank 105 are pumped into the amination reactor 101 through a metering pump 106, and the dropping temperature is controlled to be ≤30°C. After the dropping is completed, the temperature is maintained for 1 hour, and then maintained at 25-30°C for another hour. Samples are taken for analysis. After passing the test, the material containing the reaction product in the amination reactor 101 is transferred to the water separator 201.

[0049] The material is heated to 60-65℃ in the water separation vessel 201, dissolved, stirred for 0.5 hours, and then allowed to stand for 0.5 hours to separate into layers. The lower organic phase, i.e., the separation product, is sent to the primary alkaline washing vessel 301, while the upper aqueous phase is sent to the separation water collection vessel 202. 5% alkaline solution from the alkaline solution tank 303 is added to the separation product in the primary alkaline washing vessel 301, heated to 60-65℃, dissolved, stirred for 0.5 hours, and allowed to stand for 0.5 hours to separate into layers. The lower organic phase is sent to the secondary alkaline washing vessel 302, while the upper aqueous phase is sent to the separation water collection vessel 202. 5% alkaline solution is added to the secondary alkaline washing vessel 302, heated to 60-65℃, dissolved, stirred for 0.5 hours, and allowed to stand for 0.5 hours to separate into layers. The lower organic phase, i.e., the alkaline washing product, is sent to the desolventizing vessel 401, while the upper aqueous phase is sent to the separation water collection vessel 202. The water phase collected in the stratified water collection vessel 202 is cooled to 10-20℃ and placed in the filter tank 203 for filtration. The filtrate is sent to the sewage tank 504. The filter cake is rinsed with water once and then sent back to the water separator 201 for reuse.

[0050] After the alkaline washing product enters the desolventizing reactor 401, it is heated to 85°C under normal pressure to remove some dichloroethane. Water is then added through water tank 403, and hydrochloric acid is added through hydrochloric acid tank 404 to adjust the pH of the material in the desolventizing reactor 401 to 6-7. Desolventizing continues until all dichloroethane is removed (temperature ≤95°C). The temperature is then lowered to 15-20°C, and the desolventized product is pressurized into the combined reactor 501. The dichloroethane removed from the desolventizing reactor 401 enters the acid washing reactor 402. 50% water is added through water tank 403, and hydrochloric acid is added dropwise through hydrochloric acid tank 404 to adjust the pH of the material to neutral. Then, 50% water is added for a second water wash. The resulting dichloroethane is clear and transparent and is returned to the dichloroethane storage tank 102 for reuse.

[0051] After the desolventized product enters the two-in-one reactor 501, water is added to the two-in-one reactor 501 through the water tank 403, and the mixture is stirred for 10 minutes. Then, nitrogen is turned on through the nitrogen pipeline (pressure ≤0.2MPa) to press the material in the two-in-one reactor 501 until it is dry. The filtrate is sent to the sewage tank 504, and the filter cake is sent to the disc dryer 502 for drying at a temperature ≤90℃. The moisture content of the 2-nitro-N,3-dimethylbenzamide concentrate obtained after drying is ≤0.2%, and it is sent to the concentrate storage tank 503.

[0052] It should be noted that the detailed structure of some devices in this utility model is not described in detail, but belongs to the prior art known to those skilled in the art, and therefore will not be described again here. In addition, the parts of this device not described are the same as or can be implemented using existing technology.

[0053] It should be noted that those skilled in the art, under the guidance of this utility model, can also make some modifications to the design of the above system. For example, overflow / nitrogen pipelines are also installed on the equipment within the system; pumps, pressure sensors, flow meters, or temperature sensors are installed on the conveying pipelines within the system in different units or devices, and various valves, such as pressure relief valves, pressure regulating valves, safety valves, and pneumatic valves, are also installed to regulate and stabilize the pressure of the entire system, and the opening degree of the valves can also be adjusted to regulate the flow rate of materials in the pipeline.

[0054] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of this utility model, and not 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; and these 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

1. A production apparatus for the methylamine reaction of 2-nitro-3-methylbenzoyl chloride, characterized in that, include: The reaction unit is equipped with an amination vessel, which is used to react the reactants to generate a reaction product, the reaction product being 2-nitro-N,3-dimethylbenzamide. The liquid separation unit has its inlet connected to the outlet of the amination reactor to separate the reaction products into liquid products. An alkaline washing unit is provided, wherein the inlet of the alkaline washing unit is connected to the outlet of the liquid separation unit to perform alkaline washing on the liquid separation product to obtain an alkaline washed product. The solvent removal unit has its inlet connected to the outlet of the alkaline washing unit to remove solvent from the alkaline washing product and obtain a solvent-removed product, which is crude 2-nitro-N,3-dimethylbenzamide.

2. The production apparatus for the methylamination reaction of 2-nitro-3-methylbenzoyl chloride according to claim 1, characterized in that, The inlet of the amination reactor is connected to the outlet of a feed storage tank, which includes a dichloroethane storage tank, a monomethylamine liquid storage tank, a liquid alkali tank, and a high-level tank. The high-level tank stores 2-nitro-3-methylbenzoyl chloride. The outlets of the dichloroethane storage tank, the monomethylamine liquid storage tank, the liquid alkali tank, and the high-level tank are all connected to the inlet of the amination reactor. A metering pump is installed between the liquid alkali tank and the high-level tank and the amination reactor.

3. The production apparatus for the methylamination reaction of 2-nitro-3-methylbenzoyl chloride according to claim 1, characterized in that, The outlet of the amination reactor is connected to the inlet of the water separator of the liquid separation unit, and the outlet of the water separator is connected to the alkaline washing unit; the upper part of the water separator is provided with a water outlet, which is connected in sequence to the stratified water collection vessel and the filter tank; the filter cake outlet of the filter tank is connected to the reuse port of the water separator.

4. The production apparatus for the methylamination reaction of 2-nitro-3-methylbenzoyl chloride according to claim 3, characterized in that, The alkaline washing unit is equipped with at least two alkaline washing tanks. The outlet of the water separation tank is connected in sequence to the inlet of the primary alkaline washing tank and the secondary alkaline washing tank. The inlets of the primary alkaline washing tank and the secondary alkaline washing tank are also connected to the outlet of the alkaline water tank. The outlet of the secondary alkaline washing tank is connected to the desolvation unit. The upper part of the primary alkaline washing tank and the secondary alkaline washing tank is provided with a liquid outlet, which is connected to the stratified water collection tank.

5. The production apparatus for the methylamination reaction of 2-nitro-3-methylbenzoyl chloride according to claim 4, characterized in that, The solvent removal unit is equipped with a solvent removal vessel, the inlet of which is connected to the outlet of the secondary alkaline washing vessel; the solvent outlet of the solvent removal vessel is connected to the inlet of the acid washing vessel, and the outlet of the acid washing vessel is connected to the inlet of the dichloroethane storage tank; the solvent removal unit is also equipped with a water tank and a hydrochloric acid tank, and the outlets of the water tank and the hydrochloric acid tank are respectively connected to the inlets of the solvent removal vessel and the acid washing vessel through pipelines.

6. The production apparatus for the methylamination reaction of 2-nitro-3-methylbenzoyl chloride according to claim 3, characterized in that, The production apparatus further includes a purification unit, the inlet of which is connected to the outlet of the desolventizing unit, to wash and dry the desolventized product to obtain a purified product, which is a high-purity 2-nitro-N,3-dimethylbenzamide.

7. The production apparatus for the methylamination reaction of 2-nitro-3-methylbenzoyl chloride according to claim 6, characterized in that, The purification unit is equipped with a two-in-one reactor. The inlet of the two-in-one reactor is connected to the outlet of the desolvation unit. The outlet of the two-in-one reactor is connected to the inlet of the dryer. The outlet of the dryer is connected to the refined product storage tank.

8. The production apparatus for the methylamination reaction of 2-nitro-3-methylbenzoyl chloride according to claim 7, characterized in that, The feed inlet of the two-in-one reactor is also connected to the outlet of the water tank; the top of the two-in-one reactor is provided with an air inlet, which is connected to a nitrogen pipeline; the filtrate outlet of the two-in-one reactor is connected to a sewage tank.

9. The production apparatus for the methylamine reaction of 2-nitro-3-methylbenzoyl chloride according to claim 8, characterized in that, The filtrate outlet of the filter tank is connected to the sewage tank.

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