Production system and method of anhydrous organic peroxy acid

Abstract

The invention relates to the technical field of chemical engineering, and particularly discloses an anhydrous organic peroxy acid production system and method.The anhydrous organic peroxy acid production system comprises a peroxidation reaction distiller, a first oil-water separator, an azeotropic distillation tower and a second oil-water separation and light component removal tower, and moisture is brought out of a reaction system through two times of azeotropy and two times of oil-water separation; and the solvent and the entrainer are respectively recovered through the azeotropic distillation tower and the light component removal tower, and the recovered materials can be recycled. According to the present invention, with the method, the hydrogen peroxide conversion rate and the organic peroxy acid selectivity are high, the prepared anhydrous organic peroxy acid has characteristics of excellent quality and water content of less than 0.01%, and the process has advantages of short reaction time, high raw material utilization rate, high heat energy utilization rate and good economy.

Description

Technical Field

[0001] This invention relates to the field of chemical technology, specifically to a production system and method for anhydrous organic peroxyacid. Background Technology

[0002] In chemical production processes, certain reactions have extremely strict requirements regarding water content, as the water content in the solution directly affects the selectivity of the reaction. For example, in the reaction of cyclohexanone with peroxyacid to prepare caprolactone, the presence of trace amounts of water can cause the resulting caprolactone to undergo hydrolysis or polymerization, affecting the selectivity of the reaction and ultimately impacting product quality.

[0003] Organic peroxides are generally prepared by reacting organic acids with hydrogen peroxide solution. However, because the hydrogen peroxide solution contains water and water is generated during the reaction, it is difficult to directly obtain anhydrous organic peroxides. Typically, azeotropic distillation is used during the reaction, with ester-based azeotropic agents showing good water-carrying effects. However, these agents have some compatibility with water, with water solubility reaching 2-3 g / 100g. This results in high reflux rates and energy consumption during the preparation of anhydrous peroxide solutions, and the reaction time for water removal is very long, generally exceeding 24 hours, significantly reducing production efficiency.

[0004] CN106349140A discloses a method for preparing anhydrous peroxy organic carboxylic acid solution. The method involves using a stirred reactor with a distillation column to first remove water from the reaction system via azeotropic distillation, then separating the free water by condensation and sedimentation, and finally removing saturated water from the azeotropic agent using an adsorbent, returning the water to the distillation column. However, since the azeotropic agent also contains a small amount of peroxy acid, which readily reacts with metal ions in conventional adsorbents, causing the metal ions to dissolve, affecting the reaction preparation process, reducing the adsorption effect, and making it difficult to reduce the water content to below 0.01% through simple adsorption alone. Summary of the Invention

[0005] To address the aforementioned problems, this invention provides a production system and method for anhydrous organic peroxyacids, which can promptly remove moisture from the reaction system, promote the reaction, shorten the reaction time, improve production efficiency, save energy, and separate the solvent and azeotropic agent for recycling.

[0006] The technical solution of this invention is a production system for anhydrous organic peroxyacid, comprising a peroxidation reaction distillation unit. The top outlet of the distillation section is connected to a gas-liquid separator via a first condenser. The liquid phase outlet of the gas-liquid separator is connected to a first oil-water separator. The oil phase outlet of the first oil-water separator is connected to an azeotropic distillation column. The liquid phase outlet of the azeotropic distillation column is connected to a light-light removal column. The top outlet of the light-light removal column is connected to a reuse storage tank via a second condenser. The gas phase outlet of the azeotropic distillation column is connected to a second oil-water separator via a third condenser. The oil phase outlet of the second oil-water separator is connected to the reuse storage tank. The material outlet of the reuse storage tank is connected to the azeotropic agent inlet of the azeotropic distillation column. The lower part of the peroxidation reaction distillation unit is provided with an anhydrous organic peroxyacid solution discharge outlet.

[0007] Optionally, the peroxidation reaction distillation apparatus includes a feed inlet for the reaction raw materials and a solvent feed inlet; the bottom outlet of the light-weight removal tower is connected to the solvent feed inlet of the peroxidation reaction distillation apparatus via a pipeline; and a vacuum pump is connected to the top of the gas-liquid separator.

[0008] Optionally, the aqueous phase outlet of the first oil-water separator and the aqueous phase outlet of the second oil-water separator are connected to a wastewater pipeline and then connected to a subsequent wastewater treatment process.

[0009] Optionally, the oil phase outlet of the first oil-water separator is connected to the top inlet of the azeotropic distillation column via a first intermediate storage tank and a first liquid transfer pump, and the liquid phase outlet of the azeotropic distillation column is also connected to the first reboiler and returned to the azeotropic distillation column via a pipeline. Optionally, the cooling medium outlet of the second condenser is connected to the heating medium inlet of the first reboiler, and the heating medium outlet of the first reboiler is connected to the cooling medium inlet of the second condenser. Optionally, the liquid phase outlet of the azeotropic distillation column is connected to the light phase removal column via a second liquid pump; the outlet at the bottom of the light phase removal column is connected to the second reboiler via a pipeline and returns to the light phase removal column; a reflux tank is also provided between the second condenser and the reuse storage tank, and the liquid phase outlet of the reflux tank is provided with a branch pipe to return to the light phase removal column.

[0010] Optionally, a second intermediate storage tank is also provided between the third condenser and the second oil-water separator.

[0011] The present invention also relates to a method for producing anhydrous organic peroxyacids using the above-described apparatus, comprising the following steps: S1. The reactants and solvents are added to the peroxide reaction distillation apparatus to react. The water generated is azeotropic with the solvent. At the top temperature of 30~80℃ and pressure of 10-50KPa, it comes out from the top of the distillation section. After condensation, gas-liquid separation is performed. The liquid part enters the first oil-water separator for oil-water separation. S2. The oil phase is fed into the azeotropic distillation column and comes into countercurrent contact with the azeotropic agent. At 40~80℃ and 20~101kpa, the water in the azeotropic distillation column undergoes azeotroping with the azeotropic agent. The oil phase comes out from the top of the azeotropic distillation column, and after condensation, it enters the second oil-water separator for separation. The oil phase obtained is reused as the azeotropic agent in the azeotropic distillation column. S3. Part of the bottom material of the azeotropic distillation column enters the reboiler for heat exchange to maintain the temperature at the bottom of the column at 50~90℃ and the pressure at 20~105Kpa. The other part enters the light-light removal column. Under the controlled temperature of 60-100℃ and 20~101Kpa in the light-light removal column, the azeotropic agent vaporizes and comes out from the top of the column. After condensation, part of it is returned to the light-light removal column, and the other part enters the recycling storage tank. Part of the bottom material of the light-light removal column is heated and returned to the light-light removal column to maintain the bottom temperature at 70~105℃. The other part is recycled as solvent to the peroxide reaction distiller.

[0012] Optionally, the reaction raw materials include organic acid, hydrogen peroxide, catalyst, and stabilizer, wherein the organic acid is one or more of acetic acid, propionic acid, butyric acid, isobutyric acid, valeric acid, isovaleric acid, and pterovaleric acid; the catalyst is one or more of boric acid, metaboric acid, sodium bisulfate, sodium bisulfite, disodium hydrogen phosphate, and sodium monohydrogen phosphate; and the stabilizer is at least one compound selected from 2-methylpyridine, phosphate ester, and pyridinedicarboxylic acid.

[0013] Optionally, the solvent is any one of methyl ester, ethyl ester, isopropyl ester, n-propyl ester, n-butyl ester, or isobutyl ester of a fatty acid with 2 to 4 carbon atoms; the azeotropic agent forms an azeotrope with water, and the azeotropic point is at least 10°C lower than the azeotropic point of the solvent and water. The azeotropic agent can be any one of straight-chain alkanes, cycloalkanes, aromatics, or chlorinated low-carbon alkanes, such as n-hexane, cyclohexane, cyclohexene, benzene, toluene, dichloroethane, chloroform, or carbon tetrachloride.

[0014] The present invention has the following beneficial effects: This invention involves adding hydrogen peroxide solution, a catalyst, an organic acid, and a solvent to a stirred peroxide reactive distillation apparatus. Water introduced from the raw materials and water generated during the reaction are continuously carried away by the azeotropic distillation, promoting the sustained reaction. The azeotropic distillation separation system further removes water from the distilled reaction solvent. After separation by a light-light-removal column, an anhydrous solvent is obtained and recycled back to the peroxide reactive distillation apparatus, achieving solvent recycling. The heat from the gaseous components of the light-light-removal column is recycled as a heat source for the reboiler of the second azeotropic distillation column, achieving system heat energy recycling. This invention rapidly removes water, shifting the peroxide reaction equilibrium to the right, improving the conversion rate and selectivity of the reaction, and increasing the production efficiency of peroxide preparation. The conversion rate of hydrogen peroxide and the selectivity of organic peroxide are both high, and the prepared anhydrous organic peroxide is of excellent quality with a water content of <0.01%. Simultaneously, this process has a short reaction time, high raw material utilization, high heat energy utilization, and good economic efficiency. Due to the rapid removal of water, the catalyst is also easily precipitated, which can be removed by filtration or centrifugation without affecting downstream use.

[0015] In addition, the reactive distillation apparatus in this invention performs organic peroxidation reaction, achieving the coupling of reaction and separation, which greatly improves the thermal energy utilization efficiency and saves the investment cost of the device; the hot gaseous material in the device serves as the heat source for the reboiler, further realizing energy saving and consumption reduction of the entire device. Attached Figure Description

[0016] Figure 1 The present invention provides a schematic diagram of the production system, in which 1-peroxide reaction distillation apparatus, 2-first condenser, 3-vacuum pump, 4-gas-liquid separator, 5-first oil-water separator, 6-first intermediate storage tank, 7-first delivery pump, 8-azeotropic distillation column, 9-first reboiler, 10-second delivery pump, 11-light weight removal column, 12-second condenser, 13-reflux tank, 14-second reboiler, 15-third condenser, 16-second intermediate storage tank, 17-second oil-water separator, 18-reuse storage tank, and 19-third delivery pump.

[0017] 101 - Reactants, 102 - Solvent, 103 - Azeotropic agent, 104 - Peroxyacid solution, 105 - Wastewater. Detailed Implementation

[0018] Unless otherwise specified, the experimental methods used in the following examples are conventional methods. Unless otherwise specified, all raw materials and reagents used are commercially available.

[0019] The embodiments of the present invention will now be described in detail with reference to the accompanying drawings and examples. However, those skilled in the art will understand that the following examples are for illustrative purposes only and should not be considered as limiting the scope of the present invention.

[0020] Example 1 The anhydrous organic peroxy acid production system provided by this invention is as follows: Figure 1 As shown, the apparatus includes a peroxidation reaction still 1, with a raw material inlet 101 and a solvent inlet 102 at the top, and an anhydrous organic peroxyacid solution outlet 104 at the bottom. The top outlet of the distillation section of the peroxidation reaction still 1 is connected to a gas-liquid separator 4 via a first condenser 2, and a vacuum pump 3 is connected to the top of the gas-liquid separator 4. The liquid phase outlet of the gas-liquid separator is connected to a first oil-water separator 5, and the aqueous phase outlet of the first oil-water separator is connected to a subsequent wastewater treatment process via a wastewater pipe 105. The oil phase outlet of the first oil-water separator is connected to the upper part of the azeotropic distillation column 8 via the first intermediate storage tank 6 and the first transfer pump 7. The lower part of the azeotropic distillation column has an azeotropic agent inlet 103. The two components come into countercurrent contact in the azeotropic distillation column, where the water and azeotropic agent undergo azeotroping and are drawn from the top. After passing through the third condenser 15, the water is condensed into the second intermediate storage tank 16, and then connected to the second oil-water separator 17. The oil phase outlet of the second oil-water separator is connected to the reuse storage tank 18, and the water phase outlet is connected to the subsequent wastewater treatment process via the wastewater pipeline 105. The material in the reuse storage tank is the separated azeotropic agent, which is collected here and then reused in the azeotropic distillation column 8 via the third transfer pump 19.

[0021] The liquid phase outlet of azeotropic distillation column 8 is also connected to the first reboiler 9 via a pipeline and returns to azeotropic distillation column 8. The liquid phase outlet of azeotropic distillation column 8 is connected to the light-weight removal column 11 via the second liquid transfer pump 10. The liquid phase outlet of azeotropic distillation column 8 is also connected to the first reboiler 9 via a pipeline and returns to azeotropic distillation column 8 for heating the material in azeotropic distillation column 8. The top of the light-weight removal column is connected to the reflux tank 13 via the second condenser 12. The liquid phase outlet of the reflux tank 13 has a branch pipe for returning to the light-weight removal column 11, and is also connected to the reuse storage tank 18 via a pipeline.

[0022] The outlet at the bottom of the light-light-removal tower 11 is connected to the second reboiler 14 via a pipeline and returns to the light-light-removal tower 11. It is also connected to the solvent feed port 102 of the peroxidation reaction distillation apparatus via a pipeline. This allows for full utilization of thermal energy.

[0023] In a preferred embodiment, the peroxidation reaction still 1 is a reaction distillation coupling device, wherein the reaction section includes a stirring device, and the rectification section is a distillation column containing 5 to 30 trays. The tray structure is one or a mixture of several of the following: bubble cap trays, sieve trays, float trays, and grid trays. Preferably, the azeotropic distillation column 8 is a packed column, with 10 to 45% of the upper height of the column being a packed section. The packing is preferably bulk packing and / or structured packing. The light-weight removal column 11 is a tray column containing 3 to 15 trays, with the tray structure being one or a mixture of several of the following: bubble cap trays, sieve trays, float trays, and grid trays.

[0024] In a preferred embodiment, the cooling medium outlet of the second condenser 12 is connected to the heating medium inlet of the first reboiler 9, and the heating medium outlet of the first reboiler 9 is connected to the cooling medium inlet of the second condenser 12. When producing anhydrous organic peroxyacids using this system, the raw materials include organic acids, hydrogen peroxide, catalysts, stabilizers, solvents, and azeotropic agents. The organic acids are one or more selected from acetic acid, propionic acid, butyric acid, isobutyric acid, valeric acid, isovaleric acid, and pteropenic acid. The catalyst is one or more selected from boric acid, metaboric acid, sodium bisulfate, sodium bisulfite, disodium hydrogen phosphate, and sodium monohydrogen phosphate. The stabilizer is at least one compound selected from 2-methylpyridine, phosphate esters, and pyridinedicarboxylic acid. The solvent is any one of methyl esters, ethyl esters, isopropyl esters, n-propyl esters, n-butyl esters, and isobutyl esters of fatty acids with 2 to 4 carbon atoms. The azeotropic agent forms an azeotrope with water, and its azeotropic point is at least 10°C lower than the azeotropic point of the solvent and water. The azeotropic agent can be any one of straight-chain alkanes, cycloalkanes, aromatics, or chlorinated low-carbon alkanes, such as n-hexane, cyclohexane, cyclohexene, benzene, toluene, dichloroethane, chloroform, and carbon tetrachloride.

[0025] Example 2 This invention also relates to a method for producing anhydrous organic peroxyacids, comprising the following steps: S1. Reactant 101 (molar composition: propionic acid: hydrogen peroxide: sodium bisulfate: 2-methylpyridine = 2:1:0.05:0.008, wherein the mass concentration of hydrogen peroxide is 50%) with a mass flow rate of 223 kg / h and solvent methyl propionate with a mass flow rate of 153 kg / h are introduced into the peroxidation reaction still 1 for reaction. The stirring speed is 500 rpm. The generated water and methyl propionate are azeotropic. At the top temperature of 45°C and pressure of 30 kPa, the water comes out from the top of the distillation section of the peroxidation reaction still 1. After being cooled by condenser 2, it enters intermediate storage tank 4 for gas-liquid separation. The liquid part enters the first oil-water separator 5. S2. The aqueous phase material from the first oil-water separator 5 and the aqueous phase material from the second oil-water separator 17 are combined as wastewater 105 and sent to sewage treatment. The oil phase material from the first azeotropic oil-water separator 5 is sent to the first intermediate storage tank 6, and then sent to the azeotropic distillation tower 8 through the first liquid transfer pump 7. It comes into countercurrent contact with the azeotropic agent n-hexane. At 50°C and 30 kPa, the water in it undergoes azeotroping with the azeotropic agent. It comes out from the top of the azeotropic distillation tower 8, and after being condensed by the condenser 15, it enters the second intermediate storage tank 16. S3. The material in the second intermediate storage tank 16 enters the second oil-water separator 17, wherein the azeotropic agent as the oil phase component enters the reuse storage tank 18, and is then sent back to the azeotropic distillation tower 8 via the third liquid transfer pump 19. S4. Part of the bottom material of the azeotropic distillation column 8 enters the first reboiler 9 and maintains the bottom temperature of 60°C and pressure of 28 kPa after heat exchange. The other part of the material is sent to the light-light removal column 11 by the second liquid pump 10. At 65°C and 25 kPa, the azeotropic agent vaporizes and comes out from the top of the column. It is condensed by the second condenser 12 and enters the reflux tank 13. Part of it is refluxed back to the light-light removal column 11 with a reflux ratio of 1:1, and part of it enters the reuse storage tank 18. S5. Part of the bottom material of the light-light removal tower 11 passes through the second reboiler 14 and is returned to the light-light removal tower 11 after heat exchange with 0.3 MPa low-pressure steam, maintaining the bottom temperature of 75°C. The other part is combined with the solvent 102 pipeline and enters the peroxidation reaction distillation unit 1.

[0026] The peroxidation reaction time in S1 is 3 hours, and the resulting anhydrous peroxyacid solution is 325 kg / h, containing 26.9% wt peroxyacid, 0.008% water, and 0.01% hydrogen peroxide. The conversion rate of hydrogen peroxide is 99.8%, and the selectivity of peroxyacid is 97%.

[0027] Example 3 Reactant 101 (molar composition: propionic acid: hydrogen peroxide: sodium monohydrogen phosphate: 2-methylpyridine = 2:1:0.05:0.008, wherein the mass concentration of hydrogen peroxide is 50%) with a mass flow rate of 224 kg / h and solvent methyl propionate with a mass flow rate of 153 kg / h were introduced into the peroxidation reaction. The rest was the same as in Example 2. The resulting anhydrous peroxyacid solution was 353 kg / h, containing 25.0% wt peroxyacid, 0.009% water, and 0.03% hydrogen peroxide. The conversion rate of hydrogen peroxide was 99.1%, and the selectivity of peroxyacid was 96%.

[0028] Example 4 Reactant 101 (molar composition: isobutyric acid: hydrogen peroxide: sodium bisulfate: 2-methylpyridine = 2:1:0.05:0.008, wherein the mass concentration of hydrogen peroxide is 50%) with a mass flow rate of 251 kg / h and solvent methyl propionate with a mass flow rate of 153 kg / h were introduced into the peroxidation reaction. The rest was the same as in Example 2. The resulting anhydrous peroxyacid solution was 370 kg / h, containing 26.9% wt peroxyacid, 0.006% water, and 0.05% hydrogen peroxide. The conversion rate of hydrogen peroxide was 98.6%, and the selectivity of peroxyacid was 98%.

[0029] Example 5 Reactant 101 (molar composition: propionic acid: hydrogen peroxide: sodium bisulfate: 2,3-pyridinedicarboxylic acid = 2:1:0.05:0.008, wherein the mass concentration of hydrogen peroxide is 50%) with a mass flow rate of 224 kg / h and solvent methyl propionate with a mass flow rate of 153 kg / h were introduced into the peroxidation reaction. The rest was the same as in Example 2. The resulting anhydrous peroxyacid solution was 343 kg / h, containing 25.2% wt peroxyacid, 0.009% water, and 0.07% hydrogen peroxide. The conversion rate of hydrogen peroxide was 99.2%, and the selectivity of peroxyacid was 96.5%.

[0030] Example 6 The reaction feedstock 101 (molar composition: propionic acid: hydrogen peroxide: sodium bisulfate: 2-methylpyridine = 2:1:0.05:0.008, wherein the mass concentration of hydrogen peroxide is 50%) with a mass flow rate of 223 kg / h and the solvent methyl propionate with a mass flow rate of 153 kg / h were introduced into the peroxidation reaction. The rest was the same as in Example 2. The resulting anhydrous peroxyacid solution was 342 kg / h, containing 25.5% wt peroxyacid, 0.004% water, and 0.03% hydrogen peroxide. The conversion rate of hydrogen peroxide was 99.6%, and the selectivity of peroxyacid was 97.3%.

[0031] Example 7 The azeotropic agent was carbon tetrachloride, and the rest was the same as in Example 2. The resulting anhydrous peroxy acid solution was 342 kg / h, containing 25.4% wt peroxy acid, 0.009% water, and 0.05% hydrogen peroxide. The conversion rate of hydrogen peroxide was 98.5%, and the selectivity of peroxy acid was 98.1%.

[0032] Comparative Example 1 There is no azeotropic distillation tower, second oil-water separation tower, or light component removal tower. Specifically, the outlet of the pump 7 is connected to the peroxide reaction distiller 1 via a pipeline that merges with the feed inlet 102. The aqueous phase outlet of the first oil-water separator 5 is connected to the subsequent wastewater treatment process via wastewater pipeline 105, and is not connected to the water tank outlet of the second oil-water separator. The rest is the same as in Example 1.

[0033] Comparative Example 2 Using the apparatus of Comparative Example 1, with the same feed as in Example 2, an anhydrous peroxy acid solution of 342 kg / h was obtained, containing 9.1% wt peroxy acid, 2.6% water, and 4.8% hydrogen peroxide. The conversion rate of hydrogen peroxide was 51.0%, and the selectivity of peroxy acid was 68%.

[0034] Comparative Example 3 The peroxyacid reaction time was 8 hours, and other parameters were the same as in Comparative Example 2. The resulting anhydrous peroxyacid solution was 342 kg / h, containing 9.1% wt peroxyacid, 2.3% water, and 3.2% hydrogen peroxide. The conversion rate of hydrogen peroxide was 59.0%, and the selectivity of peroxyacid was 65%.

[0035] The above embodiments describe preferred embodiments of the present invention, but the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combinations of various technical features in any other way. These simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention. Therefore, the protection scope of this patent should be determined by the appended claims.

Claims

1. A production system for anhydrous organic peroxyacid, characterized in that: The apparatus includes a peroxidation reaction still (1), the top outlet of which is connected to a gas-liquid separator (4) via a first condenser (2), the liquid phase outlet of which is connected to a first oil-water separator (5), the oil phase outlet of which is connected to an azeotropic distillation column (8), the liquid phase outlet of which is connected to a light-duty removal column (11), the top outlet of which is connected to a recycling tank (18) via a second condenser (12), the gas phase outlet of which is connected to a second oil-water separator (17) via a third condenser (15), the oil phase outlet of which is connected to a recycling tank (18), and the material outlet of which is connected to the azeotropic agent inlet (103) of the azeotropic distillation column; the lower part of the peroxidation reaction still is provided with an anhydrous organic peroxy acid solution outlet (104).

2. The production system according to claim 1, characterized in that: The peroxidation reaction distillation apparatus (1) includes a reaction raw material inlet (101) and a solvent inlet (102); the bottom outlet of the light removal tower (11) is connected to the solvent inlet (102) of the peroxidation reaction distillation apparatus (1) via a pipeline; a vacuum pump (3) is connected to the top of the gas-liquid separator (4).

3. The production system according to claim 1, characterized in that: The water phase outlet of the first oil-water separator and the water phase outlet of the second oil-water separator (17) are connected to the subsequent wastewater treatment process via a wastewater pipeline (105).

4. The production system according to claim 1, characterized in that: The oil phase outlet of the first oil-water separator is connected to the top inlet of the azeotropic distillation column (8) via the first intermediate storage tank (6) and the first liquid pump (7). The liquid phase outlet of the azeotropic distillation column (8) is also connected to the first reboiler (9) via a pipeline and returns to the azeotropic distillation column (8).

5. The production system according to claim 4, characterized in that: The cooling medium outlet of the second condenser (12) is connected to the heating medium inlet of the first reboiler (9), and the heating medium outlet of the first reboiler (9) is connected to the cooling medium inlet of the second condenser (12).

6. The production system according to claim 1, characterized in that: The liquid phase outlet of the azeotropic distillation column (8) is connected to the light removal column (11) via the second liquid pump (10); the outlet at the bottom of the light removal column (11) is connected to the second reboiler (14) via a pipeline and returns to the light removal column (11); a reflux tank (13) is also provided between the second condenser (12) and the reuse storage tank (18), and the liquid phase outlet of the reflux tank (13) is provided with a branch pipe to return to the light removal column (11).

7. The production system according to claim 1, characterized in that: A second intermediate storage tank (16) is also provided between the third condenser (15) and the second oil-water separator (17).

8. A method for producing anhydrous organic peroxyacid using the production system according to any one of claims 1 to 7, characterized in that, Includes the following steps: S1. Add the reactants and solvent to the peroxide reaction distillation apparatus and react at a temperature of 30-80℃ and a pressure of 10-50KPa. The generated water and solvent azeotropically exit from the top of the distillation section. After condensation, gas-liquid separation is performed, and the liquid part enters the first oil-water separator for oil-water separation. S2. The oil phase is fed into the azeotropic distillation column and comes into countercurrent contact with the azeotropic agent. At 40~80℃ and 20~101kpa, the water in the azeotropic distillation column undergoes azeotroping with the azeotropic agent. The oil phase comes out from the top of the azeotropic distillation column, and after condensation, it enters the second oil-water separator for separation. The oil phase obtained is reused as the azeotropic agent in the azeotropic distillation column. S3. Part of the bottom material of the azeotropic distillation column (8) enters the reboiler for heat exchange and maintains the temperature at the bottom of the column at 50~90℃ and the pressure at 20~105Kpa. The other part enters the light-light removal column. The light-light removal column is controlled at a temperature of 60-100℃ and a pressure of 20~101Kpa. After the azeotropic agent is vaporized, it comes out from the top of the column. After condensation, part of it is returned to the light-light removal column and the other part enters the recycling tank. Part of the bottom material of the light-light removal column is heated and returned to the light-light removal column to maintain the bottom temperature at 70~105℃. The other part is recycled as a solvent to the peroxide reaction distiller.

9. The method according to claim 8, characterized in that: The reaction raw materials include organic acid, hydrogen peroxide, catalyst and stabilizer, wherein the organic acid is one or more of acetic acid, propionic acid, butyric acid, isobutyric acid, valeric acid, isovaleric acid and pterovaleric acid; the catalyst is one or more of boric acid, metaboric acid, sodium bisulfate, sodium bisulfite, disodium hydrogen phosphate and sodium monohydrogen phosphate; and the stabilizer is at least one compound of 2-methylpyridine, phosphate ester and pyridinedicarboxylic acid.

10. The method according to claim 8, characterized in that: The solvent is any one of methyl ester, ethyl ester, isopropyl ester, n-propyl ester, n-butyl ester, or isobutyl ester of a fatty acid with 2 to 4 carbon atoms; the azeotropic agent forms an azeotrope with water, and the azeotropic point is more than 10°C lower than the azeotropic point of the solvent and water; the azeotropic agent is any one of n-hexane, cyclohexane, cyclohexene, benzene, toluene, dichloroethane, chloroform, or carbon tetrachloride.

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