CN110698333A - Method for continuously synthesizing o-phthalaldehyde by using microchannel reaction device - Google Patents
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Abstract
The invention discloses a method for continuously synthesizing o-phthalaldehyde by a microchannel reactor, which takes 1, 3-dihydroisobenzofuran and nitric acid as raw materials, adopts a microchannel reactor to continuously synthesize the o-phthalaldehyde, and obtains the o-phthalaldehyde product by the process steps of extracting, distilling, drying and the like. Compared with the prior art, the process reaction of the invention fully utilizes the characteristics of the microchannel reactor of strengthening heat transfer and mass transfer and realizing accurate control, overcomes the problems of long reaction time, incapability of continuous production, low safety performance, large amount of acid inhibitor required in the reaction, large pollution and the like in the prior intermittent reactor for producing the o-phthalaldehyde, can realize automatic control of continuous production and process, has high-efficiency and safe production, mild reaction conditions, short reaction time, high product purity, high yield, low energy consumption, greenness and economy, and is beneficial to popularization and use of the o-phthalaldehyde in the industries of chemical industry, medical treatment and the like.
Description
Technical Field
The invention belongs to the technical field of chemical synthesis processes, and relates to a method for continuously synthesizing o-phthalaldehyde by using a microchannel reaction device.
Background
O-phthalaldehyde (O-phthalaldehyde OPA) is used as an important pharmaceutical chemical intermediate, has been widely applied to the aspects of amine alkaloid, fluorometer histamine determination and medical inspection in the past, and has been developed into a new generation of efficient medical disinfectant through various researches on the disinfection performance of researchers for a long time. Compared with the traditional glutaraldehyde disinfectant, the o-phthalaldehyde has the characteristics of short time consumption, excellent bactericidal performance and the like, and can be widely applied to disinfection of medicines and medical instruments.
The prior art reports about the synthetic route of o-phthalaldehyde are more, and mainly include: the method comprises the steps of o-xylene bromination hydrolysis method, o-xylene chlorination hydrolysis method, nitric acid direct oxidation method, naphthalene ozonization hydrogenation method, high-temperature oxidation method and the like. Wherein: the o-xylene bromination hydrolysis method needs bromine as a raw material, so the cost is higher; the o-xylene chlorination hydrolysis method is easy to be hindered by space in structure due to the chlorination reaction, so that the one-way yield is low and the loss is large; the nitric acid direct oxidation method has the disadvantages that the reaction heat release is severe, the oxidation depth is difficult to control, the reaction conversion rate is not high (lower than 70%), and a large amount of acetic acid is required to be added in the reaction to be used as an inhibitor for the generation of organic acid, so that not only is waste caused, but also the acid gas pollution is serious; the ozonization hydrogenation method of naphthalene has the problems that noble metal is used as a catalyst in the reaction, products are not easy to separate after the reaction, the process conditions are difficult to control, the product purity is low, the catalyst is inconvenient to recycle, the equipment investment of the reaction is high, and the like, and the industrial production is difficult to realize; the reaction conditions of the high-temperature oxidation method are harsh, the operation is inconvenient, the control is not easy, and the product selectivity is poor.
In addition, the existing synthesis methods are all prepared by adopting a traditional reaction kettle (bottle), and correspondingly have the defects of low selectivity and yield, higher cost, more violent reaction heat release in the production process, difficult control of process operation, insecurity, low equipment and automatic control level, incapability of continuous production, complicated production operation and the like, and the defects also limit the popularization and the use of the o-phthalaldehyde as a new generation of high-efficiency disinfectant in various industries to a great extent.
Disclosure of Invention
The invention aims to overcome the defects in the prior art and provides a method for continuously synthesizing o-phthalaldehyde by using a microchannel reaction device with easily available 1, 3-dihydroisobenzofuran as a starting material.
The technical solutions adopted to achieve the above objects of the invention are as follows.
A method for continuously synthesizing o-phthalaldehyde by a microchannel reaction device comprises the following synthesis steps:
a. constructing and configuring a microchannel reaction device, wherein the microchannel reaction device consists of a heat-conducting oil heating furnace, two oil bath raw material storage tanks, two filters, two plunger type metering pumps, a micro mixer, a microchannel reactor, a constant-temperature oil bath tank, a cooling tank, a product storage tank, a tail gas absorption device and a nitrogen bottle, the micro mixer and the microchannel reactor are arranged in the constant-temperature oil bath tank controlled at the temperature of 30-80 ℃, the heat source output end of the heat-conducting oil heating furnace is respectively connected with a first oil bath raw material storage tank and a second oil bath raw material storage tank through connecting pipelines provided with ball valves, the outlet end of the first oil bath raw material storage tank is connected to the inlet end of the first plunger type metering pump through a first filter, the outlet end of the second oil bath raw material storage tank is connected to the inlet end of the second plunger type metering pump through a second filter, the outlet ends of the first plunger type metering pump and the second plunger type metering pump are connected, the outlet end of the micro mixer is connected to the inlet end of a cooling tank filled with tap water or saline water through a micro-channel reactor, the outlet end of the cooling tank and the outlet end of a nitrogen bottle both enter a product storage tank through a pipeline provided with a ball valve, and a byproduct tail gas outlet end of the product storage tank is connected into a tail gas absorption device through a pipeline provided with a ball valve;
b. respectively putting raw materials 1, 3-dihydroisobenzofuran and nitric acid into two oil bath raw material storage tanks, and preheating the raw materials to 30-80 ℃ by using a heat conduction oil heating furnace;
c. respectively feeding the preheated 1, 3-dihydroisobenzofuran and nitric acid into a micro mixer according to the flow volume ratio of 1: 0.5-4 to mix through a first plunger type metering pump and a second plunger type metering pump, further feeding the mixture into a microchannel reactor to stay for 5-30 min to perform oxidation reaction to synthesize phthalic dicarboxaldehyde product mixed solution, and then feeding the product mixed solution into a product storage tank;
d. blowing nitrogen into the product storage tank at a rate of 1-10 mL/min through a nitrogen bottle via a nitrogen pipeline, blowing the generated nitrogen oxide byproduct into a tail gas absorption device, and carrying out an oxidation-reduction reaction on the nitrogen oxide byproduct and urea with the concentration of 5-10% under the catalysis of nitric acid with the pH value of 1-3 to reduce the nitrogen oxide byproduct into nitrogen; adding deionized water with the volume twice that of the reaction product subjected to nitrogen purging, stirring for 30min, cooling to room temperature, standing to separate out a water phase, extracting for 3 times by using ethyl acetate with the same volume, combining extract liquor, and distilling to recover ethyl acetate to obtain o-phthalaldehyde;
e. and (3) drying the distilled o-phthalaldehyde in a vacuum drying oven with the vacuum degree of 50-60 Pa and the temperature of 50 ℃ for 4 hours to obtain an o-phthalaldehyde product.
The further technical solution of the present invention further comprises: in the step a, the pipe diameter of the microchannel reactor is 0.1-5 mm.
The further technical solution of the present invention further comprises: in the step b, the concentration of the nitric acid is 30-98%, and the preferable concentration is 50-69%; the preheating temperature of the raw materials is preferably 60-80 ℃.
The further technical solution of the present invention further comprises: the flow volume ratio of the 1, 3-dihydroisobenzofuran to the nitric acid in the step c is preferably 1: 1-2, and the preferable retention time of the mixed solution in the microchannel reactor is 10-20 min.
In conclusion, the invention designs 1, 3-dihydroisobenzofuran (C)8H8O) and nitric acid are taken as raw materials, and a microchannel reaction device is adopted to carry out the continuous synthesis of the O-phthalaldehyde.Compared with the prior art, the process reaction of the invention fully utilizes the characteristics of the microchannel reactor of strengthening heat transfer and mass transfer and realizing accurate control, overcomes the problems of long reaction time, incapability of continuous production, low safety performance, large amount of acid inhibitor required in the reaction, large pollution and the like in the prior intermittent reactor for producing the o-phthalaldehyde, can realize automatic control of continuous production and process, has high-efficiency and safe production, mild reaction conditions, short reaction time, high product purity, high yield, low energy consumption, greenness and economy, and is beneficial to popularization and use of the o-phthalaldehyde in the industries of chemical industry, medical treatment and the like.
Drawings
FIG. 1 is a schematic diagram of a microchannel reactor used in the present invention, and is also a schematic diagram of a reaction route of the present invention.
FIG. 2 is an IR chart of ortho-phthalaldehyde prepared according to an example (example 1) of the present invention.
FIG. 3 is a process for preparing o-phthalaldehyde shown in FIG. 2 (example 1)1HNMR map.
Fig. 4 is a GC diagram of ortho-phthalaldehyde prepared as shown in fig. 2 (example 1).
The names of the numerical labels in the drawings are as follows: 1-a first oil bath raw material storage tank, 2-a ball valve, 3-a first filter, 4-a first plunger type metering pump, 5-a second oil bath raw material storage tank, 6-a ball valve, 7-a second filter, 8-a first plunger type metering pump, 9-a heat transfer oil heating furnace, 10-a ball valve, 11-a first high-temperature oil pump, 12-a ball valve, 13-a constant-temperature oil bath tank, 14-a micro mixer, 15-a micro-channel reactor, 16-a cooling tank, 17-a ball valve, 18-a product storage tank, 19-a ball valve, 20-a tail gas absorption device, 21-a ball valve, 22-a nitrogen bottle, 23- (for the constant-temperature oil bath) a heat transfer oil heating furnace, 24-a ball valve, 25-a ball valve and 26-a second high-temperature.
Detailed Description
The present invention will be further explained with reference to the accompanying drawings.
Referring to the drawings, the synthetic process steps of the present invention are as follows.
Firstly, constructing and configuring a microchannel reaction device, wherein the microchannel reaction device is composed of a heat conduction oil heating furnace 9, a first oil bath raw material storage tank 1, a second oil bath raw material storage tank 5, a first filter 3, a second filter 7, a first plunger type metering pump 4, a second plunger type metering pump 8, a micromixer 14, a microchannel reactor 15, a constant temperature oil bath 13, a cooling tank 16, a product storage tank 18, an exhaust gas absorption device 20, a nitrogen bottle 22, a first high temperature oil pump 11, a second high temperature oil pump 26 and a plurality of ball valves (2, 6, 10, 12, 17, 19, 21, 24 and 25) which are respectively arranged on connecting pipelines and connected through corresponding pipelines as shown in figure 1. In a specific implementation structure, the heat-conducting oil heating furnace 9 is provided with two paths of heat source output ends, one path of the heat source output end is connected with the first oil bath raw material storage tank 1 through a connecting pipeline provided with a ball valve 12 and used for preheating raw materials in the first oil bath raw material storage tank 1, and the other path of the heat source output end is connected with the second oil bath raw material storage tank 5 through a connecting pipeline provided with a ball valve 10 and a first high-temperature oil pump and used for preheating raw materials in the second oil bath raw material storage tank 5; the outlet end of a first oil bath raw material storage tank 1 is connected to the inlet end of a first plunger type metering pump 4 through a first filter 3 through a pipeline provided with a ball valve 2, the outlet end of a second oil bath raw material storage tank 5 is connected to the inlet end of a second plunger type metering pump 8 through a second filter 7 through a pipeline provided with a ball valve 6, the outlet ends of the first plunger type metering pump 4 and the second plunger type metering pump 8 are connected in parallel and then enter a constant temperature oil bath tank 13 and then are connected to the inlet end of a micro mixer 14, the outlet end of the micro mixer 14 is connected to the inlet end of a cooling tank 16 filled with tap water or saline water through a micro channel reactor 15, the outlet end of the cooling tank 16 enters a product storage tank 18 through a pipeline provided with a ball valve 17, and the byproduct tail gas outlet end of the product storage tank 18 is connected. In addition, the outlet end of the nitrogen bottle 22 also enters the product storage tank 18 through a pipeline on which the ball valve 21 is arranged, nitrogen can be blown into the product storage tank 18 at a rate of 1-10 mL/min through the nitrogen bottle 22 during work, and the byproduct of nitrogen oxide is subjected to oxidation-reduction reaction with urea with the concentration of 5-10% under the catalysis of nitric acid with the pH value of 1-3, so that the byproduct of nitrogen oxide is reduced into nitrogen. The pipe diameter of the microchannel reactor 15 is 0.1-5 mm, the micro mixer 14 and the microchannel reactor 15 are arranged in a constant temperature oil bath 13 and are immersed in heat-conducting oil, the oil temperature is controlled at 30-80 ℃, and a heat-conducting oil heating furnace 23 for the constant temperature oil bath 13 in the figure 1 is communicated with the constant temperature oil bath 13 through a ball valve 24, a second high temperature oil pump 26 and a ball valve 25 and is used for controlling the reaction temperature of raw materials.
Secondly, respectively putting the raw material 1, 3-dihydroisobenzofuran and nitric acid with the concentration of 30-98 percent (preferably 50-69 percent) into two raw material storage tanks, and preheating the raw materials to 30-80 ℃ by a heat-conducting oil heating furnace, preferably 60-80 ℃.
And thirdly, respectively enabling the preheated 1, 3-dihydroisobenzofuran and nitric acid to enter a micro mixer 14 through a first plunger type metering pump 4 and a second plunger type metering pump 8 according to the flow volume ratio of 1: 0.5-4 (preferably 1: 1-2) for mixing, further enabling the mixture to enter a microchannel reactor 15 for staying for 5-30 min (preferably for 10-20 min) for oxidation reaction to synthesize a phthalic dicarboxaldehyde product mixed solution, and then enabling the phthalic dicarboxaldehyde product mixed solution to enter a product storage tank.
Blowing nitrogen into the product storage tank 18 through a nitrogen bottle via a nitrogen pipeline at a rate of 1-10 mL/min, blowing the generated nitrogen oxide byproduct into a tail gas absorption device 20, and carrying out an oxidation-reduction reaction with urea with a concentration of 5-10% under the catalysis of nitric acid with a pH value of 1-3 to reduce the nitrogen oxide byproduct into nitrogen; adding deionized water with the volume twice that of the reaction product subjected to nitrogen purging, stirring for 30min, cooling to room temperature, standing to separate out a water phase, extracting for 3 times by using ethyl acetate with the same volume, combining extract liquor, and distilling to recover ethyl acetate to obtain the o-phthalaldehyde.
Fifthly, drying the distilled o-phthalaldehyde in a vacuum drying oven with the vacuum degree of 50-60 Pa and the temperature of 50 ℃ for 4 hours to obtain the o-phthalaldehyde product.
Example 1
Preheating raw materials 1, 3-dihydroisobenzofuran and 98% nitric acid to 30 ℃, respectively pumping the preheated 1, 3-dihydroisobenzofuran and 98% nitric acid into a micro mixer according to the flow volume ratio of 1:0.5 for mixing, further passing through a microchannel reactor, wherein the pipe diameter of the microchannel reactor is 0.3mm, and staying at the temperature of 30 ℃ for reaction for 10min to obtain the target product of the o-phthalaldehydeThe mixture is passed to the product reservoir 18. Blowing nitrogen into the product storage tank 18 through a nitrogen bottle 22 via a nitrogen pipeline at a rate of 5ml/min, blowing the generated nitrogen oxide byproduct into a tail gas absorption device 20, and carrying out oxidation-reduction reaction with urea with the concentration of 5% under the catalysis of nitric acid with the pH value of 2 so as to reduce the nitrogen oxide byproduct into nitrogen. After nitrogen purging, adding deionized water with the volume twice that of the reaction product mixed solution, stirring for 30min, cooling to room temperature, standing to separate out a water phase, extracting for 3 times by using ethyl acetate with the same volume, combining extract liquor, and distilling to recover ethyl acetate to obtain o-phthalaldehyde; placing the o-phthalaldehyde in a vacuum drying oven with the vacuum degree of 50-60 Pa and the temperature of 50 ℃ for drying for 4 hours to obtain an o-phthalaldehyde product, wherein the o-phthalaldehyde product has the content of 95.5% and the yield of 69.7%. IR chart for the preparation of orthophthalaldehyde of this example,1The HNMR and GC patterns are shown in FIG. 2, FIG. 3 and FIG. 4, respectively.
Example 2
The starting materials 1, 3-dihydroisobenzofuran and nitric acid were preheated to 50 ℃. Pumping the preheated 1, 3-dihydroisobenzofuran and 50% nitric acid into a micro mixer according to the flow volume ratio of 1:2 respectively for mixing, further passing through a microchannel reactor, keeping the pipe diameter of the microchannel and the reactor at 0.3mm for reaction for 10min at the temperature of 50 ℃ to obtain target product mixed liquid of the o-phthalaldehyde, and enabling the mixed liquid to enter a product storage tank 18. Blowing nitrogen into the product storage tank 18 through a nitrogen bottle 22 via a nitrogen pipeline at a rate of 5ml/min, blowing the generated nitrogen oxide byproduct into a tail gas absorption device 20, and carrying out oxidation-reduction reaction with urea with the concentration of 10% under the catalysis of nitric acid with the pH value of 2.5 to reduce the nitrogen oxide byproduct into nitrogen. After nitrogen purging, adding deionized water with the volume twice that of the reaction product mixed solution, stirring for 30min, cooling to room temperature, standing to separate out a water phase, extracting for 3 times by using ethyl acetate with the same volume, combining extract liquor, and distilling to recover ethyl acetate to obtain o-phthalaldehyde; placing the o-phthalaldehyde in a vacuum drying oven with the vacuum degree of 50-60 Pa and the temperature of 50 ℃ for drying for 4 hours to obtain an o-phthalaldehyde product, wherein the content is 96.1%, and the yield is 81.6%.
Example 3
The raw materials 1, 3-dihydroisobenzofuran and nitric acid were preheated to 40 ℃. Pumping the preheated 1, 3-dihydroisobenzofuran and 60% nitric acid into a micro mixer according to the flow volume ratio of 1:1.3 respectively for mixing, further passing through a micro-channel reactor, keeping the pipe diameter of the micro-channel and the reactor at the temperature of 40 ℃ for 20min for reaction, and obtaining target product mixed liquid of o-phthalaldehyde, so that the mixed liquid enters a product storage tank 18. Nitrogen is blown into the product storage tank 18 through a nitrogen bottle 22 via a nitrogen pipeline at a rate of 3ml/min, and the generated nitrogen oxide byproduct is blown into a tail gas absorption device 20 and undergoes an oxidation-reduction reaction with urea with a concentration of 10% under the catalysis of nitric acid with a pH value of 3, so that the nitrogen is reduced into nitrogen. After nitrogen purging, adding deionized water with the volume twice that of the reaction product mixed solution, stirring for 30min, cooling to room temperature, standing to separate out a water phase, extracting for 3 times by using ethyl acetate with the same volume, combining extract liquor, and distilling to recover ethyl acetate to obtain o-phthalaldehyde; placing the o-phthalaldehyde in a vacuum drying oven with the vacuum degree of 50-60 Pa and the temperature of 50 ℃ for drying for 4 hours to obtain an o-phthalaldehyde product, wherein the content is 96.4%, and the yield is 70.4%.
Example 4
The raw materials 1, 3-dihydroisobenzofuran and nitric acid are preheated to 60 ℃. Pumping the preheated 1, 3-dihydroisobenzofuran and 68% nitric acid into a micro mixer according to the flow volume ratio of 1:1.5 respectively for mixing, further passing through a micro-channel reactor, keeping the pipe diameter of the micro-channel and the reactor at 60 ℃ for 15min for reaction, and obtaining target product mixed liquid of o-phthalaldehyde, which is led to a product storage tank 18. Nitrogen is blown into the product storage tank 18 through a nitrogen bottle 22 via a nitrogen pipeline at a rate of 10ml/min, the generated nitrogen oxide byproduct is blown into a tail gas absorption device 20, and is subjected to oxidation-reduction reaction with urea with the concentration of 8% under the catalysis of nitric acid with the pH value of 2.5, so that the nitrogen oxide byproduct is reduced into nitrogen. After nitrogen purging, adding deionized water with the volume twice that of the reaction product mixed solution, stirring for 30min, cooling to room temperature, standing to separate out a water phase, extracting for 3 times by using ethyl acetate with the same volume, combining extract liquor, and distilling to recover ethyl acetate to obtain o-phthalaldehyde; placing the o-phthalaldehyde in a vacuum drying oven with the vacuum degree of 50-60 Pa and the temperature of 50 ℃ for drying for 4 hours to obtain an o-phthalaldehyde product, wherein the content is 99.2%, and the yield is 88.4%.
Example 5
The raw materials 1, 3-dihydroisobenzofuran and nitric acid are preheated to 80 ℃. Pumping the preheated 1, 3-dihydroisobenzofuran and 30% nitric acid into a micro mixer according to the flow volume ratio of 1:4 respectively for mixing, further passing through a microchannel reactor, keeping the pipe diameter of the microchannel and the reactor at the temperature of 80 ℃ for 25min for reaction, and obtaining target product mixed liquor of the o-phthalaldehyde, so that the mixed liquor enters a product storage tank 18. Blowing nitrogen into the product storage tank 18 through a nitrogen bottle 22 via a nitrogen pipeline at a rate of 5ml/min, blowing the generated nitrogen oxide byproduct into a tail gas absorption device 20, and carrying out oxidation-reduction reaction with urea with the concentration of 10% under the catalysis of nitric acid with the pH value of 1.5 to reduce the nitrogen oxide byproduct into nitrogen. After nitrogen purging, adding deionized water with the volume twice that of the reaction product mixed solution, stirring for 30min, cooling to room temperature, standing to separate out a water phase, extracting for 3 times by using ethyl acetate with the same volume, combining extract liquor, and distilling to recover ethyl acetate to obtain o-phthalaldehyde; placing the o-phthalaldehyde in a vacuum drying oven with the vacuum degree of 50-60 Pa and the temperature of 50 ℃ for drying for 4 hours to obtain an o-phthalaldehyde product, wherein the content is 99.5%, and the yield is 84.7%.
Example 6
The starting materials 1, 3-dihydroisobenzofuran and nitric acid were preheated to 70 ℃. Pumping the preheated 1, 3-dihydroisobenzofuran and 40% nitric acid into a micro mixer according to the flow volume ratio of 1:3.5 respectively for mixing, further passing through a micro-channel reactor, keeping the pipe diameter of the micro-channel and the reactor at the temperature of 70 ℃ for 30min for reaction, and obtaining target product mixed liquid of o-phthalaldehyde, so that the mixed liquid enters a product storage tank 18. Nitrogen is blown into the product storage tank 18 through a nitrogen bottle 22 via a nitrogen pipeline at a rate of 10ml/min, and the generated nitrogen oxide byproduct is blown into a tail gas absorption device 20 and undergoes an oxidation-reduction reaction with urea at a concentration of 5% under the catalysis of nitric acid with a pH value of 3, so that the nitrogen is reduced into nitrogen. After nitrogen purging, adding deionized water with the volume twice that of the reaction product mixed solution, stirring for 30min, cooling to room temperature, standing to separate out a water phase, extracting for 3 times by using ethyl acetate with the same volume, combining extract liquor, and distilling to recover ethyl acetate to obtain o-phthalaldehyde; placing the o-phthalaldehyde in a vacuum drying oven with the vacuum degree of 50-60 Pa and the temperature of 50 ℃ for drying for 4 hours to obtain an o-phthalaldehyde product, wherein the o-phthalaldehyde product has the content of 97.8 percent and the yield of 79.3 percent.
Claims (4)
1. A method for continuously synthesizing o-phthalaldehyde by a microchannel reaction device is characterized by comprising the following synthesis steps:
a. the method comprises the steps of constructing and configuring a microchannel reaction device, wherein the microchannel reaction device comprises a heat-conducting oil heating furnace (9), two oil bath raw material storage tanks (1, 5), two filters (3, 7), two plunger type metering pumps (4, 8), a micro mixer (14), a microchannel reactor (15), a constant-temperature oil bath (13), a cooling tank (16), a product storage tank (18), a tail gas absorption device (20) and a nitrogen bottle (22), wherein the micro mixer (14) and the microchannel reactor (15) are arranged in the constant-temperature oil bath (13) with the temperature controlled at 30-80 ℃, a heat source output end of the heat-conducting oil heating furnace (9) is respectively connected with a first oil bath raw material storage tank (1) and a second oil bath raw material storage tank (5) through a connecting pipeline with ball valves arranged on the heat source output end, an outlet end of the first oil bath raw material storage tank (1) is connected to an inlet end of the first plunger type metering pump (4) through the first filter, the outlet end of a second oil bath raw material storage tank (5) is connected to the inlet end of a second plunger type metering pump (8) through a second filter (7), the outlet ends of the first plunger type metering pump (4) and the second plunger type metering pump (8) are connected in parallel and then enter a constant temperature oil bath groove (13) and then are connected to the inlet end of a micro mixer (14), the outlet end of the micro mixer (14) is connected to the inlet end of a cooling groove (16) filled with tap water or saline water through a micro channel reactor (15), the outlet end of the cooling groove (16) and the outlet end of a nitrogen bottle (22) both enter a product storage tank (18) through a pipeline provided with a ball valve, and the byproduct tail gas outlet end of the product storage tank (18) is connected to a tail gas absorption device (20) through a pipeline provided with a;
b. respectively putting raw materials 1, 3-dihydroisobenzofuran and nitric acid into two oil bath raw material storage tanks (1, 5), and preheating the raw materials to 30-80 ℃ by using a heat conduction oil heating furnace (9);
c. the preheated 1, 3-dihydroisobenzofuran and nitric acid respectively enter a micro mixer (14) through a first plunger type metering pump (4) and a second plunger type metering pump (8) according to the flow volume ratio of 1: 0.5-4 for mixing, and further enter a microchannel reactor (15) for staying for 5-30 min for oxidation reaction to synthesize a phthalic dicarboxaldehyde product mixed solution, and then the phthalic dicarboxaldehyde product mixed solution enters a product storage tank (18);
d. blowing nitrogen into the product storage tank (18) through a nitrogen bottle (22) through a nitrogen pipeline at a rate of 1-10 mL/min, blowing the generated nitrogen oxide byproduct into a tail gas absorption device (20), and carrying out an oxidation-reduction reaction on the nitrogen oxide byproduct and urea with the concentration of 5-10% under the catalysis of nitric acid with the pH value of 1-3 to reduce the nitrogen oxide byproduct into nitrogen; adding deionized water with the volume twice that of the reaction product subjected to nitrogen purging, stirring for 30min, cooling to room temperature, standing to separate out a water phase, extracting for 3 times by using ethyl acetate with the same volume, combining extract liquor, and distilling to recover ethyl acetate to obtain o-phthalaldehyde;
e. and (3) drying the distilled o-phthalaldehyde in a vacuum drying oven with the vacuum degree of 50-60 Pa and the temperature of 50 ℃ for 4 hours to obtain an o-phthalaldehyde product.
2. The method for continuously synthesizing o-phthalaldehyde by using the microchannel reaction device according to claim 1, wherein the method comprises the following steps: in the step a, the pipe diameter of the microchannel reactor (15) is 0.1-5 mm.
3. The method for continuously synthesizing o-phthalaldehyde by using the microchannel reaction device according to claim 1, wherein the method comprises the following steps: in the step b, the concentration of the nitric acid is 30-98%, and the preferable concentration is 50-69%; the preheating temperature of the raw materials is preferably 60-80 ℃.
4. The method for continuously synthesizing o-phthalaldehyde by using the microchannel reaction device according to claim 1, wherein the method comprises the following steps: the flow volume ratio of the 1, 3-dihydroisobenzofuran to the nitric acid in the step c is preferably 1: 1-2, and the preferable retention time of the mixed solution in the microchannel reactor (15) is 10-20 min.
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| CN114524718A (en) * | 2022-01-25 | 2022-05-24 | 上海巽田科技股份有限公司 | Method for preparing high-purity o-phthalaldehyde from diester phthalate |
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| CN114524718B (en) * | 2022-01-25 | 2023-09-22 | 上海巽田科技股份有限公司 | Method for preparing high-purity phthalic dicarboxaldehyde from phthalic diester |
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