CN111333559A - A kind of method for continuous flow rapid preparation of peracetic acid - Google Patents

Abstract

The invention provides a continuous flow method for rapidly preparing peracetic acid. The continuous flow microchannel reactor is used to carry out the reaction, and the reaction includes the following steps: 1) acetic acid, hydrogen peroxide solution, catalyst and stabilizer are mixed and passed into the microchannel together Reaction preheating module; 2) Make the preheated mixture in step 1) continuously enter the microchannel reaction module, the reaction temperature range is 80-150 ° C, the pressure is maintained at 0.5-2.0 MPa, and the residence time is 10-200 seconds; 3) Step 2 ) The product obtained from the outlet of the microchannel reaction module enters the cooling module. The invention utilizes the characteristics of the microchannel reactor, and can realize the rapid preparation of peracetic acid by continuous flow. Compared with the traditional process, the invention greatly shortens the reaction time, improves the production efficiency, effectively reduces the safety risk, and is easy to carry out industrialized amplification. and produce.

Description

A kind of method for continuous flow rapid preparation of peracetic acid

technical field

The invention belongs to the fields of fine chemical industry and pharmaceutical chemical industry, and particularly relates to a method for rapidly preparing peracetic acid by continuous flow.

Background technique

Peracetic acid (CH ₃ COOOH) is a colorless and transparent liquid with strong oxidizing properties. It is widely used in material synthesis in the chemical industry, diesel desulfurization in the petroleum industry, fabric bleaching in the light textile industry, and medical and health fields. sterilization and disinfection. More specifically, in chemical synthesis, peracetic acid can be used as an epoxidizing agent to carry out olefin epoxidation to prepare epoxy monomers for the synthesis of propylene oxide, caprolactam, glycerol, epoxy plasticizer, valerolactone and caprolactone. In the medical field, peracetic acid is a kind of high-efficiency broad-spectrum chemical disinfectant, which has the advantages of low concentration, strong bactericidal effect, short disinfection time, non-toxic decomposition products, etc. It is widely used in disinfection, sterilization and During the SARS epidemic in 2003, it was used as the main force of disinfectants for sterilization and disinfection in hospitals and other public places.

There are two main methods for the synthesis of peracetic acid: acetaldehyde air/oxygen oxidation and hydrogen peroxide. Among them, although the cost of acetaldehyde air/oxygen oxidation is relatively low, the required equipment is complex, the investment is large, and the safety risk is high. The risk is high; if heavy metal acid catalyst is used to inhibit the formation of acetaldehyde monoperacetate, the heavy metal acid catalyst needs to be removed later, otherwise the stability of peracetic acid will be affected. The hydrogen peroxide rule is to prepare peracetic acid by reacting 30 to 90 wt% hydrogen peroxide with glacial acetic acid in the presence of a strong acid catalyst (sulfuric acid or sulfonic acid ion exchange resin) for 4 to 36 hours. The reaction formula is shown in (I) . In addition, also can adopt acetic anhydride to replace acetic acid as raw material, although can improve the concentration of peracetic acid, but can generate explosive diacyl peroxide by-product in the reaction process, therefore still use acetic acid-hydrogen peroxide more in industrial production The reaction proceeds to the production of peracetic acid.

The acetic acid-hydrogen peroxide method also has great challenges in terms of process synthesis: First, the exothermicity of the reaction system is very obvious. During the reaction process, it is necessary to slowly add materials and continuously and vigorously stir to remove the heat of reaction, so as to prevent production accidents such as explosion caused by the overheating of the reaction, and slow feeding will inevitably lead to prolonged reaction time and low production efficiency; secondly, hydrogen peroxide and peroxygen Acetic acid is unstable. The traditional process is generally carried out at a relatively low temperature (40-60 °C), the reaction is close to the equilibrium time for at least several hours, and a large reactor volume is required. Although increasing the hydrogen peroxide concentration can speed up the reaction speed, the production efficiency is still very low; although increasing the reaction temperature can speed up the reaction speed and improve the production efficiency, the hydrogen peroxide begins to decompose exothermically above 35°C.

The traditional tank reactor has poor mass transfer and heat transfer (liquid-liquid mass transfer coefficient is 0.05～0.1s ^-1 , and the total heat transfer coefficient is 1～10KW/m ³ ·K), the backflow phenomenon cannot be avoided, and liquid retention The amount is large, which is easy to cause uneven local material concentration and temperature, and there is a huge safety risk in the process of synthesizing peracetic acid; static mixer or tubular reactor, the heat exchange area is much higher than that of the tank reactor (liquid-liquid mass transfer coefficient). 0.1～10s ^-1 , the total heat transfer coefficient is 200～800KW/m ³ ·K), and the reverse flow problem is solved, but the mixing is still done in a dispersion-turbulent flow method, which takes a long time to achieve uniform mixing. The requirements for mass transfer are high, and the reaction involving two-phase materials still cannot achieve the ideal mass transfer effect and reaction selectivity; continuous flow microchannel reactor refers to a small reaction system manufactured by micromachining and precision machining technology, including chemical unit reactions The required mixers, heat exchangers, reactors and controllers, etc., but the pipe size is much smaller than the conventional tubular reactor, generally in the order of micrometers to millimeters. In the continuous flow microchannel reactor, because of the separation effect of the phase interface on the fluid and the friction effect of the microchannel on the fluid, there is a strong internal circulation and secondary flow in the reactor, which strengthens the mass transfer between the reactants. It plays an important role. In addition, by means of strengthening mixing, such as separation and remixing, laminar diffusion, etc., the reaction can be completed in milliseconds to seconds (the liquid-liquid mass transfer coefficient is 1 to 41s ^-1 ); The small size of the reaction channel shortens the molecular diffusion distance and increases the mass transfer efficiency, while the liquid holdup in the reaction zone is very small, the specific surface area with the heat exchange zone is very large, and the heat transfer capacity is very strong (the total heat transfer coefficient is 1500KW/m ³ · Above K), the temperature rise effect is not obvious, and the "number increase magnification" can be realized, and there is no magnification effect, and the safety factor is high. Therefore, the use of microchannel reactors can often complete the reaction quickly in a very short residence time, and the obtained product selectivity is higher than that of the traditional process, and the by-products are lower, especially suitable for severe exotherm, unstable reactants or products, The ratio of reactants is strict, the risk factor is high, and the reaction is flammable and explosive.

How to realize the purpose of rapid preparation of peracetic acid by continuous flow has become an urgent problem to be solved.

SUMMARY OF THE INVENTION

In view of this, the present invention aims to propose a method for the rapid preparation of peracetic acid in a continuous flow, to overcome the long reaction time, low production efficiency, relatively complex process, large equipment investment, high manufacturing cost and safety risk in the prior art. higher issues.

In order to achieve the above object, the technical scheme of the present invention is achieved in this way:

A method for preparing peracetic acid in a continuous flow, utilizes a continuous flow microchannel reactor to react, comprising the following steps,

1) acetic acid, hydrogen peroxide solution, catalyst and stabilizer are mixed together and passed into the microchannel reaction preheating module;

2) Make the preheated mixture in step 1) continuously enter the microchannel reaction module, the reaction temperature range is 80～150℃, the pressure is maintained at 0.5～2.0MPa, and the residence time is 10～200 seconds;

3) The product obtained from the outlet of the microchannel reaction module in step 2) enters the cooling module.

Utilizing the characteristics of small reaction channel size, low liquid holdup, no back-mixing, fast mass transfer and heat transfer, and narrow residence time distribution, the reaction efficiency and stability of the microchannel reactor are greatly improved, and the runaway temperature caused by the reaction is greatly reduced. resulting security risks.

Preferably, the mass transfer coefficient of the continuous flow microchannel reactor is 1-41 s ^-1 , and the total heat transfer coefficient is 1500KW/m ³ ·K or more.

Preferably, the catalyst is one or more of concentrated sulfuric acid, methanesulfonic acid and benzenesulfonic acid, preferably concentrated sulfuric acid; the stabilizer is sodium phosphate, sodium pyrophosphate, hydroxyethylidene diphosphoric acid, ethyl acetate One or more of diaminetetraacetic acid, 8-hydroxyquinoline, and pyridine-2,6-dicarboxylic acid, preferably a mixture of one or two of 8-hydroxyquinoline and ethylenediaminetetraacetic acid .

Preferably, in step 1), the molar ratio of acetic acid to hydrogen peroxide is (1-10): 1, and the preferred ratio is (1.5-4): 1; the concentration of the hydrogen peroxide solution is 25-75wt%, preferably 30 ～70wt%; the catalyst addition amount is 0.5-10wt% of the total reaction material, preferably 1-5wt%; the stabilizer addition amount is 0.01-0.5wt% of the total reaction material; preferably 0.15-0.3wt%.

Preferably, in step 2), the reaction temperature of the microchannel reaction module is 100-130 °C, the reaction pressure is 1.2-1.5 MPa, and the residence time is 15-45 seconds.

Preferably, in step 1), the preheating temperature of the microchannel reaction preheating module is 80-150°C, preferably 100-130°C; in step 3), the cooling temperature of the cooling module is 0-30°C, Preferably it is 5-20 degreeC.

Preferably, the continuous flow microchannel reactor is an enhanced hybrid microchannel reactor, a thin-layer continuous split microchannel reactor, a micropore array microchannel reactor, a fin-type microchannel reactor, a capillary microchannel reactor or Multi-strand co-flow microreactors.

Preferably, the microchannel structure in the reaction module of the microchannel reactor is a direct current channel structure or an enhanced mixed channel structure; preferably, the direct current channel structure is a tubular structure, and the enhanced mixed channel structure It is a T-shaped structure, a spherical structure, a spherical structure with baffles, a droplet-shaped structure, a heart-shaped structure, a zigzag-shaped or an umbrella-shaped structure, and the diameter of the channel is 0.5-10 mm.

The present invention also provides the application of the above-mentioned method in the preparation of peracetic acid.

In the method provided by the present invention, the oxidation reaction of acetic acid and hydrogen peroxide is carried out in a continuous microchannel reactor, and a preheating module, a reaction module, a cooling module and a heat transfer module can be connected as required. After the microchannel reactor is connected, heat transfer oil can be used for heat transfer, and ethanol/ethylene glycol can be used for cooling.

With respect to the prior art, the method for rapidly preparing peracetic acid with continuous flow of the present invention has the following advantages:

(1) method of the present invention adopts acetic acid and hydrogen peroxide to react in continuous flow microchannel reactor. Taking advantage of the characteristics of the microchannel reactor, that is, the size of the reaction channel is from micrometers to millimeters, the molecular diffusion distance is short, there is no backmixing, mass and heat transfer is fast, and the residence time distribution is narrow. In the preparation of peracetic acid, the traditional process can be used. The reaction temperature is greatly increased to 80-150 °C, which greatly improves the reaction efficiency, and the residence time is reduced to 10-200s, and the extremely short residence time makes the hydrogen peroxide not decompose in time before the end of the reaction, which greatly reduces the hydrogen peroxide. Tendency to decompose and exothermic at high temperature. The heat released by the reaction module with extremely small liquid holding capacity is quickly removed under the action of the large specific surface area per unit volume and the ultra-fast heat transfer rate, which greatly reduces the safety risk caused by the uncontrolled reaction temperature and realizes intrinsically safe production.

(2) The method of the present invention can realize the combination of "size amplification" and "number amplification" at the same time by using the microchannel reactor, and has no amplification effect. Small investment, high production flexibility and safety.

(3) The method of the present invention makes the conversion rate of hydrogen peroxide reach more than 99%, and the prepared peracetic acid concentration is high, and the concentration is between 20～35%. At the same time, because of the existence of stabilizer, peracetic acid is stably preserved at normal temperature and high concentration, and degradation rate is lower, overcoming the shortcoming of peracetic acid being easily decomposed and intolerant of storage in the prior art. The peracetic acid solution prepared by the invention can be directly used as a medical disinfectant after being diluted with distilled water to a prescribed concentration.

Description of drawings

Fig. 1 is an example of a continuous flow microchannel reactor system device diagram of an enhanced mixed microchannel reactor used in the present invention.

Detailed ways

Unless otherwise defined, technical terms used in the following examples have the same meanings as commonly understood by those skilled in the art to which the present invention belongs. The test reagents used in the following examples are conventional biochemical reagents unless otherwise specified; the experimental methods are conventional methods unless otherwise specified.

The present invention will be described in detail below with reference to the embodiments.

Example 1

One enhanced hybrid microchannel module was selected as the premix preheating module, six enhanced hybrid microchannel modules were used as the reaction module, and one enhanced hybrid microchannel module was used as the cooling module, and a continuous flow microchannel reaction system was formed according to the reaction process.

The microchannel structure of each module is an enhanced hybrid channel heart-shaped structure, and the diameter of the channel is 0.5-10mm; as for the number of modules, it is mainly to ensure that there is enough residence time.

The heat exchange medium of the preheating module and the reaction module adopts heat conduction oil, and the heat exchange medium of the cooling module adopts ethylene glycol/ethanol. According to the principle of forced heat transfer in the microchannel reactor, two temperature measurement points are set at the inlet and outlet of the reactor. Before the reaction, the microchannel reaction system and the connecting pipelines were dewatered and deoiled respectively, and the air tightness of the system was checked by nitrogen gas at 1.0MPa.

Step (1): according to the molar ratio of acetic acid and hydrogen peroxide of 2:1, acetic acid and 50wt% hydrogen peroxide solution are mixed, and then the mass concentration of 1wt% of the total mass of the reaction solution is 98% concentrated sulfuric acid and 0.2wt% are added respectively. 8-hydroxyquinoline was mixed uniformly, and the reaction mixture was continuously and stably pumped into the microchannel reaction system through a plunger pump, and the temperature of the preheating module heat exchanger was set to 100°C.

Step (2): Make the reaction mixture continuously enter the microchannel reaction module after preheating in step (1), set the temperature of the heat exchanger of the reaction module to 100°C, adjust the back pressure valve to maintain the pressure of the reaction system at 1.0MPa, set the column The plug pump flow was such that the reaction residence time was 15 s.

Step (3): The product obtained from the outlet of the microchannel reaction module in step (2) is allowed to enter the cooling module, the cooling module heat exchange temperature is 10°C, and the reaction product is finally collected.

The peracetic acid content was determined to be 24 wt % by iodometry.

Example 2

The same microchannel reactor as in Example 1 was used, and the same connection method and control method were used. This example changes the reaction conditions.

Step (1): According to the molar ratio of acetic acid and hydrogen peroxide of 1.1:1, acetic acid and 70wt% hydrogen peroxide are mixed, and then the total mass of the reaction solution is 0.5wt% and 98% concentrated sulfuric acid and 0.3wt% are respectively added. Ethylenediaminetetraacetic acid was mixed evenly, and the reaction mixture was continuously and stably pumped into the microchannel reaction system through a plunger pump, and the temperature of the preheating module heat exchanger was set to 80°C.

Step (2): Make the reaction mixture continuously enter the microchannel reaction module after preheating in step (1), set the temperature of the heat exchanger of the reaction module to 80°C, adjust the back pressure valve to maintain the pressure of the reaction system at 0.5MPa, set the column The plug pump flow was such that the reaction residence time was 33 s.

Step (3): The product obtained from the outlet of the microchannel reaction module in step (2) is put into a cooling module, and the heat exchange temperature of the cooling module is 15°C, and the reaction product is finally collected.

The peracetic acid content was determined to be 32 wt% by iodometry.

Example 3

The same microchannel reactor as in Example 1 was used, and the same connection method and control method were used. This example changes the reaction conditions.

Step (1): according to the molar ratio of acetic acid and hydrogen peroxide of 4:1, acetic acid and 30wt% hydrogen peroxide are mixed, and then 5wt% methanesulfonic acid and 0.5wt% sodium phosphate of the total mass of the reaction solution are respectively added and mixed. Evenly, the reaction mixture was continuously and stably pumped into the microchannel reaction system through a plunger pump, and the temperature of the preheating module heat exchanger was set to 148°C.

Step (2): Make the reaction mixture continuously enter the microchannel reaction module after preheating in step (1), set the temperature of the heat exchanger of the reaction module to 148°C, adjust the back pressure valve to maintain the pressure of the reaction system at 1.3MPa, set the column The plug pump flow was such that the reaction residence time was 10 s.

Step (3): the product obtained from the outlet of the microchannel reaction module in step (2) is put into a cooling module, and the heat exchange temperature of the cooling module is 18°C, and the reaction product is finally collected.

The peracetic acid content was determined to be 16.5 wt % by iodometry.

Example 4

The same microchannel reactor as in Example 1 was used, and the same connection method and control method were used. This example changes the reaction conditions.

Step (1): according to the molar ratio of acetic acid and hydrogen peroxide 10:1, acetic acid and 30wt% hydrogen peroxide are mixed, then 10wt% benzenesulfonic acid and 0.01wt% sodium pyrophosphate of the total mass of the reaction solution are added respectively, Mix evenly, continuously and stably pump the reaction mixture into the microchannel reaction system through a plunger pump, and set the temperature of the preheating module heat exchanger to 130°C.

Step (2): After preheating in step (1), the reaction mixture continuously enters the microchannel reaction module, the temperature of the heat exchanger in the reaction module is set to 130°C, the back pressure valve is adjusted to maintain the pressure of the reaction system at 1.9MPa, and the column is set The plug pump flow was such that the reaction residence time was 162 s.

Step (3): the product obtained from the outlet of the microchannel reaction module in step (2) is allowed to enter the cooling module, the cooling module heat exchange temperature is 25°C, and the reaction product is finally collected.

The peracetic acid content was determined to reach 10 wt% by iodometric method.

Example 5

The same microchannel reactor as in Example 1 was used, and the same connection method and control method were used. This example changes the reaction conditions.

Step (1): mix acetic acid and 50wt% hydrogen peroxide in a molar ratio of 1.5:1 according to the molar ratio of acetic acid and hydrogen peroxide, then add 98% concentrated sulfuric acid and 0.15wt% hydroxyl group of 2wt% of the total mass of the reaction solution respectively Ethylene diphosphoric acid was mixed uniformly, and the reaction mixture was continuously and stably pumped into the microchannel reaction system through a plunger pump, and the temperature of the preheating module heat exchanger was set to 120°C.

Step (2): After preheating in step (1), the reaction mixture continuously enters the microchannel reaction module, the temperature of the heat exchanger in the reaction module is set to 120°C, the back pressure valve is adjusted to maintain the pressure of the reaction system at 0.9MPa, and the column is set The plug pump flow was such that the reaction residence time was 44 s.

Step (3): the product obtained from the outlet of the microchannel reaction module in step (2) is allowed to enter the cooling module, the cooling module heat exchange temperature is 5°C, and the reaction product is finally collected.

The peracetic acid content was determined to be 25.6 wt % by iodometry.

Example 6

The same microchannel reactor as in Example 1 was used, and the same connection method and control method were used. This example changes the reaction conditions.

Step (1): according to the acetic acid and hydrogen peroxide molar ratio of 2.5:1, acetic acid and 70wt% hydrogen peroxide are mixed, and then 98% concentrated sulfuric acid and 0.2wt% pyridine- 2,6-dicarboxylic acid was mixed evenly, the reaction mixture was continuously and stably pumped into the microchannel reaction system through a plunger pump, and the temperature of the preheating module heat exchanger was set to 125°C.

Step (2): Make the reaction mixture continuously enter the microchannel reaction module after preheating in step (1), set the temperature of the heat exchanger of the reaction module to 125°C, adjust the back pressure valve to maintain the pressure of the reaction system at 1.5MPa, set the column The plug pump flow was such that the reaction residence time was 20 s.

Step (3): The product obtained from the outlet of the microchannel reaction module in step (2) is put into a cooling module, and the heat exchange temperature of the cooling module is 15°C, and the reaction product is finally collected.

The peracetic acid content was determined to be 30.8 wt % by iodometry.

Example 7

The same microchannel reactor as in Example 1 was used, and the same connection method and control method were used. This example changes the reaction conditions.

Step (1): according to the molar ratio of acetic acid and hydrogen peroxide of 2:1, acetic acid and 50wt% hydrogen peroxide are mixed, and then 1wt% methanesulfonic acid and 0.2wt% 8-hydroxyquinoline of the total mass of the reaction solution are added respectively. The reaction mixture was continuously and stably pumped into the microchannel reaction system through a plunger pump, and the temperature of the preheating module heat exchanger was set to 110 °C.

Step (2): Make the reaction mixture continuously enter the microchannel reaction module after preheating in step (1), set the temperature of the heat exchanger of the reaction module to 110°C, adjust the back pressure valve to maintain the pressure of the reaction system at 0.8MPa, set the column The plug pump flow was such that the reaction residence time was 18 s.

Step (3): the product obtained from the outlet of the microchannel reaction module in step (2) is allowed to enter the cooling module, the cooling module heat exchange temperature is 20°C, and the reaction product is finally collected.

The peracetic acid content was determined to be 22 wt% by iodometry.

Example 8

The same microchannel reactor as in Example 1 was used, and the same connection method and control method were used. This example changes the reaction conditions.

Step (1): according to the molar ratio of acetic acid and hydrogen peroxide 2:1, acetic acid and 70wt% hydrogen peroxide are mixed, and then 1wt% benzenesulfonic acid and 0.08wt% ethylenediaminetetraacetic acid of the total mass of the reaction solution are added respectively. The mixture was mixed evenly, and the reaction mixture was continuously and stably pumped into the microchannel reaction system through a plunger pump, and the temperature of the preheating module heat exchanger was set to 110°C.

Step (2): Make the reaction mixture continuously enter the microchannel reaction module after preheating in step (1), set the temperature of the heat exchanger of the reaction module to 110°C, adjust the back pressure valve to maintain the pressure of the reaction system at 1.1MPa, set the column The plug pump flow was such that the reaction residence time was 26 s.

Step (3): the product obtained from the outlet of the microchannel reaction module in step (2) is allowed to enter the cooling module, the cooling module heat exchange temperature is 30°C, and the reaction product is finally collected.

The peracetic acid content was determined to be 28.7 wt % by iodometry.

The above descriptions are only preferred embodiments of the present invention, and are not intended to limit the present invention. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included in the scope of the present invention. within the scope of protection.

Claims (9)

1. a method for the rapid preparation of peracetic acid in a continuous flow, is characterized in that: utilize the continuous flow microchannel reactor to react, comprising the following steps, 1) After mixing acetic acid, hydrogen peroxide solution, catalyst and stabilizer, pass into the microchannel reaction preheating module together; 2) Make the preheated mixture in step 1) continuously enter the microchannel reaction module, the reaction temperature range is 80-150° C., the pressure is maintained at 0.5-2.0 MPa, and the residence time is 10-200 seconds; 3) The product obtained from the outlet of the microchannel reaction module in step 2) enters the cooling module. 2. the method for rapidly preparing peracetic acid by continuous flow according to claim 1, is characterized in that: the mass transfer coefficient of the continuous flow microchannel reactor is 1～41s ⁻¹ , and the total heat transfer coefficient is 1500KW/m ³ · above K. 3. the method for the rapid preparation of peracetic acid by continuous flow according to claim 1, is characterized in that: described catalyzer is one or more in vitriol oil, methanesulfonic acid, benzenesulfonic acid, preferably vitriol oil; The stabilizer is one or more of sodium phosphate, sodium pyrophosphate, hydroxyethylidene diphosphate, ethylenediaminetetraacetic acid, 8-hydroxyquinoline, and pyridine-2,6-dicarboxylic acid, preferably One or a mixture of 8-hydroxyquinoline and ethylenediaminetetraacetic acid. 4. the method for rapid preparation of peracetic acid by continuous flow according to claim 1, is characterized in that: in step 1), the mol ratio of acetic acid and hydrogen peroxide is (1～10): 1, and preferred ratio is (1.5 ~4): 1; the concentration of the hydrogen peroxide solution is 25-75wt%, preferably 30-70wt%; the catalyst addition amount is 0.5-10wt% of the total reaction material, preferably 1-5wt%; the stabilizer is added The amount is 0.01-0.5wt% of the total reaction material; preferably 0.15-0.3wt%. 5. The method for rapidly preparing peracetic acid by continuous flow according to claim 1, characterized in that: in step 2), the reaction temperature of the microchannel reaction module is 100-130°C, the reaction pressure is 1.2-1.5MPa, and the The time is 15 to 45 seconds. 6. The method for rapidly preparing peracetic acid by continuous flow according to claim 1, wherein in step 1), the preheating temperature of the microchannel reaction preheating module is 80-150°C, preferably 100-130°C; In step 3), the cooling temperature of the cooling module is 0-30°C, preferably 5-20°C. 7. the method for the rapid preparation of peracetic acid by continuous flow according to claim 1, it is characterized in that: described continuous flow microchannel reactor is enhanced mixing type microchannel reactor, thin layer continuous cutting type microchannel reactor, microchannel reactor Well array microchannel reactors, finned microchannel reactors, capillary microchannel reactors or multi-strand co-flow microreactors. 8. the method for the rapid preparation of peracetic acid by continuous flow according to claim 1, is characterized in that: the microchannel structure in the reaction module of described microchannel reactor is direct current type channel structure or enhanced mixed type channel structure; Preferably The straight-through channel structure is a tubular structure, the enhanced hybrid channel structure is a T-shaped structure, a spherical structure, a spherical baffled structure, a drop-shaped structure, a heart-shaped structure, a zigzag-shaped or an umbrella-shaped structure, and The diameter of the channel is 0.5 to 10 mm. 9. The application of the method according to any one of claims 1 to 8 in the preparation of peracetic acid.

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