Continuous process for the synthesis of triamides and uses thereof
By using a continuous flow microreaction synthesis method and a microchannel reactor to control the hydrogenation and amidation reactions of ketoximes, the problems of inhomogeneity and exothermic runaway in traditional batch reactors have been solved, enabling efficient, low-cost and large-scale production of triamide compounds.
Patent Information
- Application Number
- CN202610706956.6
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2026-05-21
- Publication Date
- 2026-07-21
AI Technical Summary
The existing traditional batch reactor method for producing nucleating agents for triformamide derivatives suffers from problems such as uneven mixing, uneven temperature distribution, easy runaway of exothermic reactions, and significant scale-up effects, leading to increased side reactions, unstable product quality, and limiting its efficient production.
A continuous flow microreaction synthesis method was adopted to synthesize triamide compounds by means of efficient synergistic effect of ketoxime catalytic hydrogenation and continuous amidation using a microchannel reactor. The reaction temperature and residence time were controlled to achieve the stability and controllability of the reaction.
It enables continuous and controllable synthesis of triamide compounds, improves production efficiency, reduces costs, and is suitable for large-scale production and green synthesis of high-performance nucleating agents.
Smart Images
Figure CN122427093A_ABST
Abstract
Description
Technical Field
[0001] This invention relates to the field of organic synthesis, and in particular to a continuous synthesis method for triamide compounds and its application. Background Technology
[0002] Adding nucleating agents to polymers to improve their properties is a widely used method due to its simplicity, efficiency, low cost, and adaptability. Triformamide derivative nucleating agents combine excellent nucleation effects with mechanical strengthening properties, and their dispersion characteristics are particularly outstanding. They can be uniformly dispersed in polymer melts without the addition of dispersants. However, their complex production process results in significantly higher costs than other types of nucleating agents.
[0003] Existing traditional batch reactor production suffers from problems such as uneven mixing, uneven temperature distribution, easy runaway exothermic reactions, and significant scale-up effects, which may lead to increased side reactions and unstable product quality, thus limiting the efficient production of triformamide derivative nucleating agents.
[0004] In view of this, the present invention is hereby proposed. Summary of the Invention
[0005] One of the objectives of this invention is to provide a continuous synthesis method for triamide compounds, which not only has a stable exothermic reaction and precise controllable residence time, but also has safe and reliable operation, good scale-up performance, and can produce triamide compounds at low cost, high efficiency and large scale.
[0006] The second objective of this invention is to provide an application of a continuous synthesis method for triamide compounds, which is beneficial for achieving low-cost, high-efficiency, and large-scale production of triamide nucleating agents.
[0007] In order to achieve the above-mentioned objectives of the present invention, the following technical solution is adopted: In a first aspect, a method for the continuous synthesis of triamide compounds includes the following steps: (a) A ketoxime and a solvent are passed into a microchannel reactor to undergo a hydrogenation reaction, yielding an amine intermediate; (b) The amine intermediate, acyl chloride and acid-binding agent are passed into a microchannel reactor to undergo an amidation reaction to obtain the triamide compound.
[0008] Furthermore, in step (a), the temperature of the hydrogenation reaction is 30℃-60℃, and the time is 1h-10h.
[0009] Further, in step (a), the catalyst for the hydrogenation reaction includes at least one of Pd / C, Pd / Al2O3, Pd / CaCO3, Pt / C, PtO2, Pt / Al2O3, Ru / C, Ru / Al2O3, Rh / C, Rh / Al2O3, RhCl(PPh3)3, Ni, Ni / Al2O3, Cu, Co, and Co / Al2O3; Preferably, the molar ratio of the ketoxime to the catalyst compound is 150:0.5-5; Preferably, the mass concentration of the catalyst compound is 5%-20%.
[0010] Furthermore, the hydrogen gas introduction rate for the hydrogenation reaction is 1 ml / min to 500 ml / min.
[0011] Furthermore, in step (b), the amidation reaction is carried out at a temperature of 60°C-100°C for a time of 60s-600s.
[0012] Furthermore, the molar ratio of the acyl chloride to the ketoxime is 3-10:1; Preferably, the molar ratio of the acyl chloride to the acid binder is 1:1-10.
[0013] Furthermore, the pressure of the microchannel reactor is 0.01 MPa-10 MPa.
[0014] Furthermore, the microchannel reactor includes at least one of a wall-mounted microchannel reactor, a packed bed microchannel reactor, and a quasi-homogeneous microchannel reactor.
[0015] Furthermore, the triamide compounds include 1,3,5-tris(methylcarbonylamino)benzene, 1,3,5-tris(ethylcarbonylamino)benzene, 1,3,5-tris(propylcarbonylamino)benzene, 1,3,5-tris(isopropylcarbonylamino)benzene, 1,3,5-tris(n-butylcarbonylamino)benzene, 1,3,5-tris(2-methylpropylcarbonylamino)benzene, 1,3,5-tris(3-methylpropylcarbonylamino)benzene, and 1,3,5-tris(2,2-dimethylpropionamide). Benzene, 1,3,5-tris(n-pentylcarbonylamino)benzene, 1,3,5-tris(isopentylcarbonylamino)benzene, 1,3,5-tris(neopentylcarbonylamino)benzene, 1,3,5-tris(sec-pentylcarbonylamino)benzene, 1,3,5-tris(tert-pentylcarbonylamino)benzene, 1,3,5-tris(n-hexylcarbonylamino)benzene, 1,3,5-tris(2-methylpentylcarbonylamino)benzene, 1,3,5-tris(3-methylpentylcarbonylamino)benzene, 1,3,5-tris(4-methyl 1,3,5-Tris(3-methyl-2-ethylpropylcarbonylamino)benzene, 1,3,5-Tris(2,2-dimethylbutylcarbonylamino)benzene, 1,3,5-Tris(2,3-dimethylbutylcarbonylamino)benzene, 1,3,5-Tris(2,4-dimethylbutylcarbonylamino)benzene, 1,3,5-Tris(3,3-dimethylbutylcarbonylamino)benzene, 1,3,5-Tris(3-ethylbutylcarbonylamino)benzene, 1,3,5-Tris(2,2, At least one of 3-trimethylpropylcarbonylamino)benzene, 1,3,5-tris(2,3,3-trimethylpropylcarbonylamino)benzene, 1,3,5-tris(2,3,4-trimethylpropylcarbonylamino)benzene, 1,3,5-tris(2-ethyl-2-methylpropylcarbonylamino)benzene, 1,3,5-tris(2-isopropylpropylcarbonylamino)benzene, 1,3,5-tris(2-sec-butylethylcarbonylamino)benzene, and 1,3,5-tris(3-isopropylpropylcarbonylamino)benzene.
[0016] Secondly, the application of any of the methods described above in the production of nucleating agents.
[0017] Compared with the prior art, the present invention has at least the following beneficial effects: The continuous synthesis method for triamide compounds provided by this invention is a continuous flow microreaction synthesis method. Employing a multi-module continuous microreaction approach, it achieves continuous and controllable synthesis of triamide compounds through the highly efficient synergy of ketoxime-catalyzed hydrogenation and continuous amidation. This method not only features stable exothermic reactions and precisely controllable residence times, but also safe and reliable operation and excellent scale-up performance. Compared with traditional methods, this invention offers higher production efficiency and significantly reduced production costs, enabling low-cost, high-efficiency, and large-scale production of triamide nucleating agents. This is beneficial for the green synthesis and industrial application of high-performance nucleating agents. Attached Figure Description
[0018] To more clearly illustrate the specific embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the specific embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.
[0019] Figure 1 This is a schematic flowchart of a continuous synthesis method for triamide compounds provided in one embodiment of the present invention. Detailed Implementation
[0020] The technical solution of the present invention will be clearly and completely described below with reference to the embodiments. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.
[0021] According to a first aspect of the present invention, a continuous synthesis method for triamide compounds is provided, comprising the following steps: (a) A ketoxime and a solvent are passed into a microchannel reactor to undergo a hydrogenation reaction, yielding an amine intermediate; (b) An amine intermediate, an acyl chloride, and an acid-binding agent are passed into a microchannel reactor to undergo an amidation reaction to obtain the triamide compound.
[0022] Microchannel reactors have significant advantages such as high mass and heat transfer efficiency, precise and controllable reaction parameters, good safety, and easy scale-up. With the help of channel structures with characteristic dimensions in the micrometer to millimeter range, these reactors can achieve rapid mixing, efficient heat exchange, and highly ordered flow of materials, thereby significantly improving reaction rate and selectivity.
[0023] This invention is a continuous flow microreaction synthesis method that uses a multi-module continuous microreaction approach. Through the efficient synergy of ketoxime catalytic hydrogenation and continuous amidation, it achieves the continuous and controllable synthesis of triamide compounds. The reaction is not only exothermic and stable with precise controllable residence time and safe and reliable operation, but also has good scale-up performance.
[0024] Compared with traditional methods, the method of this invention has higher production efficiency and significantly reduced production costs, enabling low-cost, high-efficiency, and large-scale production of triamide nucleating agents, which is beneficial to the green synthesis and industrial application of high-performance nucleating agents.
[0025] The continuous synthesis method of the triamide compounds of this invention is described in [reference needed]. Figure 1The method includes a ketoxime hydrogenation reaction step and an amidation reaction step. Specifically, the catalyst is first fixed in a microchannel reactor, and the temperature of the microchannel reactor is controlled. Then, the reaction solvent and the reactant ketoxime are added through the inlet, and hydrogen gas (H2) is introduced. The residence time is controlled to allow the ketoxime to undergo a hydrogenation reaction, generating an intermediate product, namely an amine intermediate. The obtained amine intermediate is then mixed with the reactant acyl chloride and acid-binding agent in the microchannel reactor to undergo an amidation reaction. The temperature and residence time of the microchannel reactor are controlled to obtain the final product, namely a triamide compound. The method of this invention achieves continuous synthesis throughout the entire process and has outstanding advantages such as stable exothermic reaction, precise control of material residence time, high operational safety, and ease of scale-up.
[0026] In a preferred embodiment, in step (a), the temperature of the hydrogenation reaction can be 30°C-60°C, with typical but non-limiting temperatures such as 30°C, 40°C, 50°C, and 60°C, and the time of the hydrogenation reaction can be 1h-10h, with typical but non-limiting times such as 1h, 2h, 3h, 4h, 5h, 6h, 7h, 8h, 9h, and 10h, which is more conducive to the full progress of the hydrogenation reaction, thereby obtaining a higher product yield.
[0027] The channels of the microchannel reactor can be preheated, that is, the channels of the microchannel reactor are heated to the required temperature and kept at that temperature, with a temperature range of 30℃-60℃.
[0028] In a preferred embodiment, in step (a), the catalyst for the hydrogenation reaction includes, but is not limited to, at least one of Pd / C, Pd / Al2O3, Pd / CaCO3, Pt / C, PtO2, Pt / Al2O3, Ru / C, Ru / Al2O3, Rh / C, Rh / Al2O3, RhCl(PPh3)3, Ni, Ni / Al2O3, Cu, Co, and Co / Al2O3.
[0029] In this invention, the molar ratio of the raw material ketoxime to the catalyst compound input per unit time in the microchannel reactor can be 150:(0.5-5), and the mass concentration of the catalyst compound can be 5%-20%.
[0030] In a preferred embodiment, the hydrogen flow rate for the hydrogenation reaction can be 1 ml / min to 500 ml / min, with typical but non-limiting flow rates such as 1 ml / min, 10 ml / min, 100 ml / min, 200 ml / min, 300 ml / min, 400 ml / min, and 500 ml / min.
[0031] In a preferred embodiment, in step (b), the amidation reaction temperature can be 60°C-100°C, with typical but non-limiting temperatures such as 60°C, 70°C, 80°C, 90°C, and 100°C, and the mixing reaction time can be 60s-600s, with typical but non-limiting times such as 60s, 80s, 100s, 200s, 300s, 400s, 500s, and 600s, which is more conducive to promoting the reaction to proceed fully, thereby significantly improving the yield of the final product.
[0032] The channels of the microchannel reactor are heated to the required temperature and held at that temperature, which can be 40℃-100℃.
[0033] In this invention, the molar ratio of acyl chloride to ketoxime can be 3-10:1, and the molar ratio of acyl chloride to acid binder can be 1:1-10.
[0034] In a preferred embodiment, the pressure of the microchannel reactor can be 0.01 MPa-10 MPa, with typical but non-limiting pressures such as 0.01 MPa, 0.1 MPa, 1 MPa, 2 MPa, 3 MPa, 4 MPa, 5 MPa, 6 MPa, 7 MPa, 8 MPa, 9 MPa, and 10 MPa.
[0035] In a preferred embodiment, the microchannel reactor includes, but is not limited to, at least one of a wall-mounted microchannel reactor, a packed bed microchannel reactor, and a quasi-homogeneous microchannel reactor.
[0036] In this invention, the structure of the triamide compounds is shown in the following formula: ; R1, R2, and R3 can be the same or different C1-C12 substituted alkyl, cycloalkyl, or aromatic groups.
[0037] In a preferred embodiment, the triamide compounds include, but are not limited to, 1,3,5-tris(methylcarbonylamino)benzene, 1,3,5-tris(ethylcarbonylamino)benzene, 1,3,5-tris(propylcarbonylamino)benzene, 1,3,5-tris(isopropylcarbonylamino)benzene, 1,3,5-tris(n-butylcarbonylamino)benzene, 1,3,5-tris(2-methylpropylcarbonylamino)benzene, 1,3,5-tris(3-methylpropylcarbonylamino)benzene, and 1,3,5-tris(2,2- Dimethylpropamidobenzene, 1,3,5-tris(n-pentylcarbonylamino)benzene, 1,3,5-tris(isopentylcarbonylamino)benzene, 1,3,5-tris(neopentylcarbonylamino)benzene, 1,3,5-tris(sec-pentylcarbonylamino)benzene, 1,3,5-tris(tert-pentylcarbonylamino)benzene, 1,3,5-tris(n-hexylcarbonylamino)benzene, 1,3,5-tris(2-methylpentylcarbonylamino)benzene, 1,3,5-tris(3-methylpentylcarbonylamino)benzene, 1,3,5-tris(n-hexylcarbonylamino)benzene (4-Methylpentylcarbonylamino)benzene, 1,3,5-tris(3-methyl-2-ethylpropylcarbonylamino)benzene, 1,3,5-tris(2,2-dimethylbutylcarbonylamino)benzene, 1,3,5-tris(2,3-dimethylbutylcarbonylamino)benzene, 1,3,5-tris(2,4-dimethylbutylcarbonylamino)benzene, 1,3,5-tris(3,3-dimethylbutylcarbonylamino)benzene, 1,3,5-tris(3-ethylbutylcarbonylamino)benzene, 1,3,5-tris(2,4-dimethylbutylcarbonylamino)benzene At least one of 2,3-trimethylpropylcarbonylamino)benzene, 1,3,5-tris(2,3,3-trimethylpropylcarbonylamino)benzene, 1,3,5-tris(2,3,4-trimethylpropylcarbonylamino)benzene, 1,3,5-tris(2-ethyl-2-methylpropylcarbonylamino)benzene, 1,3,5-tris(2-isopropylpropylcarbonylamino)benzene, 1,3,5-tris(2-sec-butylethylcarbonylamino)benzene, and 1,3,5-tris(3-isopropylpropylcarbonylamino)benzene.
[0038] According to a second aspect of the present invention, the method described in any of the above-mentioned methods is provided for use in the production of nucleating agents, which is beneficial for achieving low-cost, high-efficiency and large-scale production of triamide nucleating agents.
[0039] The present invention will be further illustrated by the following examples. Unless otherwise specified, the materials in the examples are prepared according to existing methods or purchased directly from the market.
[0040] Example 1 A continuous synthesis method for triamide compounds includes the following steps: (a) Weigh 2 g of cyclohexyltrione oxime, 30 ml of N-methylpyrrolidone and 0.5 g of 5% Pd catalyst. The molar ratio of oxime to catalyst is 150:1.34. Place the catalyst into the channel of a packed bed hydrogenation microchannel reactor. Preheat the channel of the microchannel reactor (5 microchannel reaction plates, microchannel inner diameter of 0.2 mm, total liquid volume of 48.8 ml, material of 316 L) to 40 °C. Dissolve cyclohexyltrione oxime in 30 ml of N-methylpyrrolidone and deliver it to the channel at a rate of 0.407 ml / min. Introduce hydrogen at a rate of 2 ml / min, pressurize to 0.3 MPa and control the pressure to be stable at 0.3 MPa. Control the residence time to 2 h. The oxime undergoes hydrogenation reaction. After 2 h, the liquid moves to the outlet end of the hydrogenation microchannel reactor and is an amine intermediate. (b) Connect the hydrogenation microchannel reactor and the continuous microchannel reactor. Heat the channels of the microchannel reactor (5 microchannel reaction plates, microchannel inner diameter of 0.2 mm, total liquid volume of 48.8 ml, material of 316 L) to 40 °C. Purge with nitrogen gas at a rate of 10 ml / min for at least 15-30 min. After purging, reduce the nitrogen flow rate to 0.5-1 ml / min as a protective gas to maintain positive pressure in the system. Then, add 3 ml of 3,3-dimethylbutyryl chloride and 10 ml of pyridine (acid-binding agent) at a rate of 40 ml / min from the inlet of the continuous microchannel. Control the residence time to 60 s and keep the temperature constant at 60 °C. The reaction with the amine intermediate will undergo amidation. After 60 s, the liquid will move to the outlet of the continuous microchannel reactor. The crude product will be purified by extraction, recrystallization, and vacuum distillation to finally obtain a pure triamide compound, 1,3,5-tris(2,2-dimethylbutylcarbonylamino)benzene.
[0041] Example 2 The difference between this embodiment and Embodiment 1 is that in step (a), the dwell time is controlled to be 0.5h; Everything else is the same as in Example 1.
[0042] Example 3 The difference between this embodiment and Embodiment 1 is that in step (a), the dwell time is controlled to be 1 hour; Everything else is the same as in Example 1.
[0043] Example 4 The difference between this embodiment and Embodiment 1 is that in step (a), the dwell time is controlled to be 5 hours. Everything else is the same as in Example 1.
[0044] Example 5 The difference between this embodiment and Embodiment 1 is that in step (a), the dwell time is controlled to be 10 hours. Everything else is the same as in Example 1.
[0045] Example 6 The difference between this embodiment and Embodiment 1 is that in step (a), the hydrogen gas introduction rate is 1 ml / min; Everything else is the same as in Example 1.
[0046] Example 7 The difference between this embodiment and Embodiment 1 is that in step (a), the hydrogen gas introduction rate is 10 ml / min; Everything else is the same as in Example 1.
[0047] Example 8 The difference between this embodiment and Embodiment 1 is that in step (a), the hydrogen gas introduction rate is 100 ml / min; Everything else is the same as in Example 1.
[0048] Example 9 The difference between this embodiment and Embodiment 1 is that, in step (a), the hydrogen gas introduction rate is 250 ml / min; Everything else is the same as in Example 1.
[0049] Example 10 The difference between this embodiment and Embodiment 1 is that in step (b), the dwell time is controlled to be 30 seconds. Everything else is the same as in Example 1.
[0050] Example 11 The difference between this embodiment and Embodiment 1 is that in step (b), the dwell time is controlled to be 100s; Everything else is the same as in Example 1.
[0051] Example 12 The difference between this embodiment and Embodiment 1 is that in step (b), the dwell time is controlled to be 300s; Everything else is the same as in Example 1.
[0052] Example 13 The difference between this embodiment and Embodiment 1 is that in step (b), the dwell time is controlled to be 600s; Everything else is the same as in Example 1.
[0053] Example 14 The difference between this embodiment and Embodiment 1 is that, in step (b), the acyl chloride is acetyl chloride; Everything else is the same as in Example 1.
[0054] Example 15 The difference between this embodiment and Embodiment 1 is that, in step (b), the acyl chloride is propionyl chloride; Everything else is the same as in Example 1.
[0055] Example 16 The difference between this embodiment and Embodiment 1 is that, in step (b), the acyl chloride is isopropionyl chloride; Everything else is the same as in Example 1.
[0056] Example 17 The difference between this embodiment and Embodiment 1 is that, in step (b), the acyl chloride is n-butyryl chloride; Everything else is the same as in Example 1.
[0057] Example 18 The difference between this embodiment and Embodiment 1 is that, in step (b), the acyl chloride is isobutyryl chloride; Everything else is the same as in Example 1.
[0058] Comparative Example 1 The difference between this comparative example and Example 1 is that, in step (a), a microchannel reactor was not used for the reaction; instead, a traditional batch reactor was used. The process steps are as follows: (a) Weigh 2 g of cyclohexyltrione oxime, 30 ml of N-methylpyrrolidone and 0.5 g of 5% Pd catalyst (molar ratio of oxime to catalyst is 150:1.34), add the above materials together into a high-pressure batch reactor, and seal the reactor; preheat the reactor to 40°C, turn on the stirrer and set the speed to 500 rpm; introduce hydrogen into the reactor, pressurize to 0.3 MPa, and control the pressure to be stable at 0.3 MPa, maintain the reaction temperature at 40°C, continue to introduce hydrogen to maintain constant pressure, react for 6 hours, after the reaction is completed, cool, depressurize, take out the reaction liquid to obtain amine intermediate; Step (b) is the same as in Example 1.
[0059] Comparative Example 2 The difference between this comparative example and Example 1 is that, in step (b), a traditional batch reactor was used instead of a microchannel reactor for the reaction, and the process steps are as follows: The amine intermediate prepared according to step (a) of Example 1 was added to hydrochloric acid to precipitate it into a hydrochloride solid. The solid was then added to 50 ml of N-methylpyrrolidone. After stirring to dissolve / disperse, the solid was transferred to a batch reactor equipped with stirring and temperature control. 3 ml of 3,3-dimethylbutyryl chloride and 10 ml of pyridine (acid-binding agent) were added. The reactor was sealed, and the air inside was replaced with nitrogen three times. The reactor was then heated to 60°C, and stirring was started (500 rpm). The reaction was carried out at this temperature for 5 h. After the reaction was completed, the reactor was cooled to room temperature, the pressure was released, and the reaction solution was removed. The solution was purified by extraction, recrystallization, and vacuum distillation to obtain a triamide compound, namely 1,3,5-tris(2,2-dimethylbutylcarbonylamino)benzene. Step (a) is the same as in Example 1.
[0060] Comparative Example 3 The difference between this comparative example and Example 1 is that no acid-binding agent was added in step (b); Everything else is the same as in Example 1.
[0061] Test case The yields and production efficiencies of the final triamide compounds in the examples and comparative examples are shown in Table 1.
[0062] Table 1
[0063] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, and not to limit them; although the present invention 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 the present invention.
Claims
1. A continuous synthesis method for triamide compounds, characterized in that, Includes the following steps: (a) A ketoxime and a solvent are passed into a microchannel reactor to undergo a hydrogenation reaction, yielding an amine intermediate; (b) The amine intermediate, acyl chloride and acid-binding agent are passed into a microchannel reactor to undergo an amidation reaction to obtain the triamide compound.
2. The method according to claim 1, characterized in that, In step (a), the hydrogenation reaction is carried out at a temperature of 30°C-60°C for 1-10 hours.
3. The method according to claim 2, characterized in that, In step (a), the catalyst for the hydrogenation reaction includes at least one of Pd / C, Pd / Al2O3, Pd / CaCO3, Pt / C, PtO2, Pt / Al2O3, Ru / C, Ru / Al2O3, Rh / C, Rh / Al2O3, RhCl(PPh3)3, Ni, Ni / Al2O3, Cu, Co, and Co / Al2O3; Preferably, the molar ratio of the ketoxime to the catalyst compound is 150:0.5-5; Preferably, the mass concentration of the catalyst compound is 5%-20%.
4. The method according to claim 3, characterized in that, The hydrogen flow rate for the hydrogenation reaction is 1 ml / min to 500 ml / min.
5. The method according to claim 1, characterized in that, In step (b), the amidation reaction is carried out at a temperature of 60°C-100°C for a time of 60s-600s.
6. The method according to claim 5, characterized in that, The molar ratio of the acyl chloride to the ketoxime is 3-10:1; Preferably, the molar ratio of the acyl chloride to the acid binder is 1:1-10.
7. The method according to any one of claims 1-6, characterized in that, The pressure of the microchannel reactor is 0.01 MPa-10 MPa.
8. The method according to claim 7, characterized in that, The microchannel reactor includes at least one of a wall-mounted microchannel reactor, a packed bed microchannel reactor, and a quasi-homogeneous microchannel reactor.
9. The method according to claim 1, characterized in that, The triamide compounds include 1,3,5-tris(methylcarbonylamino)benzene, 1,3,5-tris(ethylcarbonylamino)benzene, 1,3,5-tris(propylcarbonylamino)benzene, 1,3,5-tris(isopropylcarbonylamino)benzene, 1,3,5-tris(n-butylcarbonylamino)benzene, 1,3,5-tris(2-methylpropylcarbonylamino)benzene, 1,3,5-tris(3-methylpropylcarbonylamino)benzene, 1,3,5-tris(2,2-dimethylpropionamido)benzene, 1 3,5-Tris(n-pentylcarbonylamino)benzene, 1,3,5-Tris(isopentylcarbonylamino)benzene, 1,3,5-Tris(neopentylcarbonylamino)benzene, 1,3,5-Tris(sec-pentylcarbonylamino)benzene, 1,3,5-Tris(tert-pentylcarbonylamino)benzene, 1,3,5-Tris(n-hexylcarbonylamino)benzene, 1,3,5-Tris(2-methylpentylcarbonylamino)benzene, 1,3,5-Tris(3-methylpentylcarbonylamino)benzene, 1,3,5-Tris(4-methylpentyl)benzene Carbonylamino)benzene, 1,3,5-tris(3-methyl-2-ethylpropylcarbonylamino)benzene, 1,3,5-tris(2,2-dimethylbutylcarbonylamino)benzene, 1,3,5-tris(2,3-dimethylbutylcarbonylamino)benzene, 1,3,5-tris(2,4-dimethylbutylcarbonylamino)benzene, 1,3,5-tris(3,3-dimethylbutylcarbonylamino)benzene, 1,3,5-tris(3-ethylbutylcarbonylamino)benzene, 1,3,5-tris(2,2,3-dimethylbutylcarbonylamino)benzene At least one of the following: 1,3,5-tris(2,3,3-trimethylpropylcarbonylamino)benzene, 1,3,5-tris(2,3,4-trimethylpropylcarbonylamino)benzene, 1,3,5-tris(2-ethyl-2-methylpropylcarbonylamino)benzene, 1,3,5-tris(2-isopropylpropylcarbonylamino)benzene, 1,3,5-tris(2-sec-butylethylcarbonylamino)benzene, and 1,3,5-tris(3-isopropylpropylcarbonylamino)benzene.
10. The use of the method according to any one of claims 1-9 in the production of nucleating agents.