Microchannel continuous production process for synthesizing phenoxyethanol

Abstract

The invention relates to the technical field of phenoxyethanol production processes, solves the problems of low phenoxyethanol synthesis efficiency and incomplete raw material reaction in the existing production process, and particularly discloses a microchannel continuous production process for synthesizing phenoxyethanol. Comprising the following steps: respectively preheating phenol and ethylene oxide through a micro-channel heater, and leading the preheated phenol and ethylene oxide to a reactor group; the preheated phenol and ethylene oxide are sequentially fed into a first-order micro-channel reactor, a second-order micro-channel reactor and a third-order micro-channel reactor for reaction, and the first-order micro-channel reactor, the second-order micro-channel reactor and the third-order micro-channel reactor are connected in series end to end; and feeding a phenoxyethanol crude product obtained by the reaction into a fractionating tower, and carrying out split-flow purification to obtain a phenoxyethanol product. By adopting the production process, the reaction of the raw materials in each stage can be promoted to be fully carried out, the reaction conversion rate is improved, the main product generation rate is high, and the controllability is strong.

Description

Technical Field

[0001] The invention relates to the technical field of phenoxyethanol production technology, and in particular to a microchannel continuous production process for synthesizing phenoxyethanol. Background Art

[0002] Phenoxyethanol is an organic compound with the molecular formula C8H 10 O2, which has antibacterial effects, is often used as a substitute for highly toxic sodium azide in biological buffer solutions. Because phenoxyethanol has low toxicity and is not chemically active against copper and lead, it usually functions as a preservative in cosmetics, skin care products, vaccines and medicines. In current industrial production, phenoxyethanol is usually synthesized by the reaction of phenol and ethylene carbonate, which involves multiple reaction steps and the formation of intermediates. Therefore, controlling the orderly progress of the reaction is crucial to the synthesis of phenoxyethanol.

[0003] For example, the patent with publication number CN117065678A provides a device and method for synthesizing phenoxyethanol, including an ethylene carbonate buffer tank, a phenol buffer tank, a reactor, an evaporator, a phenoxyethanol crude product buffer tank and a catalyst concentrate buffer tank; the material outlet of the ethylene carbonate buffer tank is connected to the inlet of a preheating mixer through an ethylene carbonate pump; the material outlet of the phenol buffer tank is connected to the inlet of the preheating mixer through a phenol pump, and the outlet of the preheating mixer is connected to the material inlet of the reactor; the bottom material outlet of the reactor is connected to the material inlet of the evaporator through a reactor discharge pump; the upper material outlet of the evaporator is connected to the material inlet of the phenoxyethanol crude product buffer tank through an evaporative condenser, and the bottom material outlet of the phenoxyethanol crude product buffer tank is also connected to a phenoxyethanol crude product pump; the bottom material outlet of the evaporator is connected to the material inlet of the catalyst concentrate buffer tank, and the bottom material outlet of the catalyst concentrate buffer tank is connected to the material inlet of the reactor through a catalyst circulation pump.

[0004] However, in the existing process of performing the synthesis reaction in a reactor as described above, the reactants and raw materials are not sufficiently combined, thus resulting in a problem of low production efficiency. Summary of the invention

[0005] The purpose of the present invention is to solve the problem of low production efficiency of phenoxyethanol in the existing production process.

[0006] The present invention is achieved through the following technical solutions:

[0007] The present invention provides a microchannel continuous production process for synthesizing phenoxyethanol, comprising the following steps:

[0008] S1 preheats phenol and ethylene oxide through a microchannel heater respectively, and then passes them to the reactor group;

[0009] The preheated phenol and ethylene oxide in S2 react in the reactor group:

[0010] The first-order microchannel reactor, the second-order microchannel reactor and the third-order microchannel reactor are sequentially sent to react, and the first-order microchannel reactor, the second-order microchannel reactor and the third-order microchannel reactor are connected in series end to end;

[0011] S3 sends the crude phenoxyethanol obtained by the reaction into a fractionation tower for splitting and purification to obtain a phenoxyethanol product.

[0012] Preferably, in step S2, in the first-stage microchannel reactor, the mass ratio of the amount of phenol introduced to the amount of ethylene oxide introduced is 0.90-0.95:1; the reaction temperature of phenol and ethylene oxide in the first-stage microchannel reactor is 100-150°C, the reaction residence time is 0.15-0.45h, and the reaction obtains the first intermediate material.

[0013] Preferably, the reaction temperature of the first intermediate material in the second-stage microchannel reactor is 100-150° C., the reaction residence time is 0.15-0.45 h, and the second intermediate material is obtained by reaction.

[0014] Preferably, the reaction temperature of the second intermediate material in the three-stage microchannel reactor is 150-180° C., the reaction residence time is 0.5-1.5 h, and the reaction obtains crude phenoxyethanol and gas phase by-products.

[0015] Preferably, in step S3, the treatment temperature of the crude phenoxyethanol fed into the fractionation tower is 160-180° C., and the fractionation time is 0.5-1.5 h.

[0016] Preferably, in step S1, the feed end of the reactor group is connected to the phenol microchannel heater and the ethylene oxide microchannel heater respectively; the feed end of the phenol microchannel heater is connected to the phenol raw material tank, and the feed end of the ethylene oxide microchannel heater is connected to the ethylene oxide tank.

[0017] Preferably, the discharge ends of the phenol raw material tank and the ethylene oxide tank are respectively provided with flow valves, and the discharge ends of the phenol microchannel heater and the ethylene oxide microchannel heater are respectively provided with flow meters.

[0018] Preferably, the pipeline connecting the phenol microchannel heater and the first-stage microchannel reactor and the pipeline connecting the ethylene oxide microchannel heater and the first-stage microchannel reactor are both equipped with raw material one-way valves.

[0019] Preferably, the pipeline connecting the first-order microchannel reactor and the second-order microchannel reactor is equipped with a second-order one-way valve, and the pipeline connecting the second-order microchannel reactor and the third-order microchannel reactor is equipped with a third-order one-way valve.

[0020] Preferably, the feed end of the first-stage microchannel reactor is also equipped with a feed pipe, and the feed end of the second-stage microchannel reactor is also equipped with a liquid inlet pipe.

[0021] The technical solution of the present invention has the following beneficial effects:

[0022] The present invention adopts a specific microchannel equipment system, performs microchannel preheating treatment on raw materials respectively, and performs microchannel synthesis reaction in stages. Specifically, a first-order microchannel reactor, a second-order microchannel reactor and a third-order microchannel reactor connected in series are used as a reactor group, so that the raw materials react in sequence in a controllable process, and the reaction conditions in the microchannel reactor of each stage are adjusted according to the reaction and change process of the reactants, so that the reaction process of each stage can be carried out in a more efficient and favorable environment, which can promote the reaction of each stage to a greater extent, improve the overall reaction conversion rate, and have a high main product generation rate and strong controllability. BRIEF DESCRIPTION OF THE DRAWINGS

[0023] Figure 1 The figure is a schematic diagram of the structure of the process system for synthesizing phenoxyethanol in the present invention.

[0024] Figure markings: 11-phenol raw material tank, 12-phenol microchannel heater, 13-ethylene oxide tank, 14-ethylene oxide microchannel heater, 15-flow valve, 16-flow meter, 21-first-order microchannel reactor, 22-raw material one-way valve, 23-feeding pipe, 31-second-order microchannel reactor, 32-second-order one-way valve, 33-liquid inlet pipe, 41-third-order microchannel reactor, 42-third-order one-way valve, 51-distillation tower, 52-feeding valve, 53-catalyst recovery pipe, 54-phenoxyethanol pipe, 55-feeding pump. DETAILED DESCRIPTION

[0025] In order to make the purpose, technical scheme and advantages of the embodiments of the present invention clearer, the technical scheme in the embodiments of the present invention will be described clearly and completely below. Where specific conditions are not specified in the embodiments, they are carried out under conventional conditions or conditions recommended by the manufacturer; where the manufacturers of the instruments, equipment, reagents and raw materials used are not specified, they are all conventional products that can be purchased commercially.

[0026] The present invention provides a microchannel continuous production process for synthesizing phenoxyethanol, comprising the following steps:

[0027] (1) Loading stage

[0028] The phenol in the phenol raw material tank 11 is preheated by the phenol microchannel heater 12, and the ethylene oxide in the ethylene oxide tank 13 is also preheated by the ethylene oxide microchannel heater 14, and then the preheated phenol and ethylene oxide are respectively passed to the first-stage microchannel reactor 21.

[0029] Among them, the discharge ends of the phenol raw material tank 11 and the discharge ends of the ethylene oxide tank 13 are respectively equipped with flow valves 15 for regulating the amount of raw materials leading to the first-order microchannel reactor 21; and the discharge ends of the phenol microchannel heater 12 and the discharge ends of the ethylene oxide microchannel heater 14 are respectively equipped with flow meters 16 to observe the flow rate and rate of the raw materials flowing to the reaction equipment.

[0030] The above-mentioned devices are all connected by pipelines, and the pipelines for introducing phenol and ethylene oxide connected to the feed end of the first-order microchannel reactor 21 are respectively equipped with raw material one-way valves 22 to allow the raw materials to flow into the first-order microchannel reactor 21 in one direction.

[0031] (2) First reaction stage

[0032] The preheated raw materials phenol and ethylene oxide are respectively introduced into the first-order microchannel reactor 21, and the first-order microchannel reactor 21 is also equipped with a feeding pipe 23. While the raw materials are introduced, the first-order catalyst is also introduced from the feeding pipe 23; from the beginning of introducing the raw materials into the first-order microchannel reactor 21, the reaction temperature in the first-order microchannel reactor 21 is controlled to be 100-150°C, and the material residence time in the first-order microchannel reactor 21 is 0.15-0.45h.

[0033] In order to orderly control the reaction process, when the raw materials are introduced into the first-order microchannel reactor 21, the one-way valve configured at the feed end of the first-order microchannel reactor 21 is required to control the feed mass ratio of phenol to ethylene oxide to be 0.90-0.95:1, and the total feed time of phenol is basically equal to the total feed time of ethylene oxide.

[0034] In this reaction stage, the first-order catalyst used can be an acidic catalyst such as H2SO4, NaOH, or a basic catalyst to enhance the nucleophilicity of phenol and promote the reaction.

[0035] (3) Intermediate reaction stage

[0036] After the first-order microchannel reactor 21 reaches the reaction residence time, the one-way valve at the feed end of the second-order microchannel reactor 31 is opened, and all the reacted materials in the first-order microchannel reactor 21 are passed to the second-order microchannel reactor 31, and the pipeline connecting the first-order microchannel reactor 21 and the second-order microchannel reactor 31 is equipped with a second-order one-way valve 32; and at the same time, alcohol or ether solvents are injected from the liquid inlet pipe 33 of the second-order microchannel reactor 31 to react. The injected alcohol or ether solvent can help dissolve the reactants and stabilize the intermediate structure; and the reaction temperature in the second-order microchannel reactor 31 is controlled to be 100-150°C, and the material residence time in this reaction is 0.15-0.45h.

[0037] (4) Terminal reaction stage

[0038] The formed materials after the reaction in the second-stage microchannel reactor 31 are all sent to the third-stage microchannel reactor 41, and the pipeline connecting the second-stage microchannel reactor 31 and the third-stage microchannel reactor 41 is equipped with a third-stage one-way valve 42; and the reaction temperature in the third-stage channel reactor is controlled to be 150-180°C, the reaction residence time is 0.5-1.5h, and the reaction products continue to pass to the next treatment process.

[0039] (5) Post-processing

[0040] The crude phenoxyethanol formed in the three-stage microchannel reactor 41 is further fed into a fractionation tower 51, and a feed valve 52 is provided in the pipeline connecting the three-stage microchannel reactor 41 and the fractionation tower 51. By utilizing the characteristics of phenoxyethanol having a high boiling point and impurity components having a low boiling point, fractionation and purification are carried out, and the treatment temperature in the fractionation tower 51 is controlled to be 160-180° C. and the fractionation time is 2-6 hours, so that the components in the crude phenoxyethanol can be fully separated to obtain a high-quality phenoxyethanol product.

[0041] Wherein, the discharge end of fractionating tower 51 is equipped with catalyst recovery pipe 53 and phenoxyethanol pipe 54, and phenoxyethanol pipe 54 is equipped with feed pump 55, in order to collect the product and catalyst after fractionation respectively. In the present invention, adopt the first-order microchannel reactor, second-order microchannel reactor and three-order microchannel reactor in series as reactor group, make raw material react successively with controllable process. When reaction starts, the oxygen atom of phenol attacks the carbon atom of ethylene oxide, and phenol is a nucleophilic reagent, and its hydroxyl has stronger nucleophilicity, and the carbon atom of ethylene oxide is an electron-deficient carbon, has stronger electrophilicity, and is therefore easily attacked by the oxygen atom of phenol, and the structure of ethylene oxide makes it have annular stress, is easy to open the ring under nucleophilic attack, generates alcohol product. Can promote the reaction of each stage to a greater extent all to fully carry out, improve overall reaction conversion rate, main product generation rate is high, and controllability is strong.

[0042] Example 1

[0043] The microchannel equipment system used in this embodiment includes a feeding mechanism, a reaction mechanism and a purification mechanism connected in sequence end to end. The feeding mechanism includes a phenol feeding line and an ethylene oxide feeding line connected in parallel. The phenol feeding line includes a phenol raw material tank and a phenol microchannel heater connected in sequence, and the tail end of the phenol microchannel heater is connected to the reaction mechanism. The ethylene oxide feeding line includes an ethylene oxide tank and an ethylene oxide microchannel heater connected in sequence, and the tail end of the ethylene oxide microchannel heater is connected to the reaction mechanism; the discharge end of the phenol raw material tank and the discharge end of the ethylene oxide tank are respectively provided with flow valves, and the discharge end of the phenol microchannel heater and the discharge end of the ethylene oxide microchannel heater are respectively provided with flow meters.

[0044] The reaction mechanism comprises a first-order microchannel reactor, a second-order microchannel reactor and a third-order microchannel reactor connected in series, and the feed end of the first-order microchannel reactor is connected to the tail end of the phenol microchannel heater and the tail end of the ethylene oxide microchannel heater respectively; the top of the first-order microchannel reactor and the top of the second-order microchannel reactor are respectively provided with a feed pipe and a liquid inlet pipe. In addition, the pipeline connecting the phenol microchannel heater with the first-order microchannel reactor and the pipeline connecting the ethylene oxide microchannel heater with the first-order microchannel reactor are both provided with a raw material one-way valve; the pipeline connecting the first-order microchannel reactor with the second-order microchannel reactor is provided with a second-order one-way valve, and the pipeline connecting the second-order microchannel reactor with the third-order microchannel reactor is provided with a third-order one-way valve.

[0045] The purification mechanism comprises a fractionation tower, the feed end of the fractionation tower is connected with the bottom of the three-stage microchannel reactor, the discharge end of the fractionation tower is respectively provided with a phenoxyethanol tube and a catalyst recovery tube, and the phenoxyethanol tube is provided with a feed pump.

[0046] Using the above-mentioned microchannel equipment system, phenol and ethylene oxide with a mass ratio of 0.92:1 are first fed through the phenol feed line and the ethylene oxide feed line respectively, and passed into the first-order microchannel reactor, and H2SO4 is introduced into the first-order microchannel reactor through the feeding pipe as a catalyst, and the amount of H2SO4 is about 5% of the total mass of the raw materials. The temperature is controlled at 120±10°C, and the reaction is carried out for 0.25h to form a first liquid intermediate material.

[0047] Subsequently, the first intermediate product is introduced into the second-stage microchannel reactor, and ether solvent is added to the second-stage microchannel reactor through the liquid inlet pipe. The temperature is controlled at 120±10°C and the reaction is carried out for 0.25h to form a liquid second intermediate material.

[0048] Then, the second intermediate product was introduced into a three-stage microchannel reactor, the temperature was controlled at 165±5° C., and the reaction was carried out for 1.25 hours. After the reaction was completed, the liquid phase material formed was the crude phenoxyethanol.

[0049] Finally, the crude phenoxyethanol is fed into a distillation tower through a feed pipe and a feed pump, the temperature in the distillation tower is controlled at 170±5°C, and fractional distillation and purification are performed for 4.5 hours to recover the phenoxyethanol product.

[0050] The recovered phenoxyethanol product was weighed, and the recovery rate of the product was calculated by phenoxyethanol product / (phenol raw material+ethylene oxide raw material). It was found that in this embodiment, under the condition that the total reaction time was 1.75 h, the phenoxyethanol product generation rate was 99.65%.

[0051] Example 2

[0052] The difference between this embodiment and embodiment 1 is that the mass ratio of phenol to ethylene oxide introduced into the first-stage microchannel reactor is 0.90:1.

[0053] After weighing and calculation, in this embodiment, under the condition that the total reaction time is 1.75h, the product yield of phenoxyethanol is 99.52%.

[0054] Example 3

[0055] The difference between this embodiment and embodiment 1 is that the mass ratio of phenol to ethylene oxide introduced into the first-stage microchannel reactor is 0.95:1.

[0056] After weighing and calculation, in this embodiment, under the condition that the total reaction time is 1.75h, the product yield of phenoxyethanol is 99.34%.

[0057] Example 4

[0058] The difference between this embodiment and Embodiment 1 is that the reaction temperature in the first-stage microchannel reactor is 145±5°C, the reaction temperature in the second-stage microchannel reactor is 145±5°C, and the reaction temperature in the third-stage microchannel reactor is 155±5°C.

[0059] After weighing and calculation, in this embodiment, under the condition that the total reaction time is 1.75h, the product yield of phenoxyethanol is 99.27%.

[0060] Example 5

[0061] The difference between this embodiment and Embodiment 1 is that the reaction temperature in the first-stage microchannel reactor is 110±10°C, the reaction temperature in the second-stage microchannel reactor is 110±10°C, and the reaction temperature in the third-stage microchannel reactor is 175±5°C.

[0062] After weighing and calculation, the product yield of phenoxyethanol prepared in this embodiment was 98.89% under the condition that the total reaction time was 1.75 h.

[0063] Comparative Example 1

[0064] The difference between this comparative example and Example 1 is that the reaction mechanism includes only one synthesis reactor, and the raw materials phenol and ethylene oxide are introduced into the synthesis reactor after preheating, the temperature in the synthesis reactor is controlled to be 160±10°C, and the reaction is carried out for 2 hours to obtain a crude phenoxyethanol product and a gaseous by-product; then, the crude phenoxyethanol product is sent to a purification mechanism for treatment to obtain a phenoxyethanol product.

[0065] After weighing and calculation, the product yield of phenoxyethanol prepared in this comparative example under the condition of a total reaction time of 2 h is only 95.60%.

[0066] Comparative Example 2

[0067] The difference between this comparative example and Example 1 is that the reaction mechanism includes two synthesis reactors, and the raw materials phenol and ethylene oxide are introduced into the first synthesis reactor after preheating, and the temperature in the synthesis reactor is controlled to be 120±10°C, and the reaction is carried out for 1.5 hours, and then introduced into the second synthesis reactor, and the temperature in the synthesis reactor is controlled to be 160±10°C, and the reaction is carried out for 1.5 hours to obtain a crude phenoxyethanol product and a gaseous by-product; subsequently, the crude phenoxyethanol product is sent to a purification mechanism for treatment to obtain a phenoxyethanol product.

[0068] After weighing and calculation, the product yield of phenoxyethanol prepared in this comparative example under the condition of a total reaction time of 3 h is only 96.76%.

[0069] Comparative Example 3

[0070] The difference between this comparative example and Example 1 is that the mass ratio of phenol to ethylene oxide introduced into the first-stage microchannel reactor is 1.05:1.

[0071] After weighing and calculation, in this embodiment, under the condition that the total reaction time is 1.75h, the product yield of phenoxyethanol is only 94.64%.

[0072] Comparative Example 4

[0073] The difference between this comparative example and Example 1 is that the reaction time in the first-order microchannel reactor is 0.1 h, the reaction time in the second-order microchannel reactor is 0.1 h, and the reaction time in the third-order microchannel reactor is 0.35 h.

[0074] After weighing and calculation, the product yield of phenoxyethanol prepared in this embodiment was only 89.03% under the condition that the total reaction time was 0.55 h.

[0075] Comparative Example 5

[0076] The difference between this comparative example and Example 1 is that the reaction time in the first-order microchannel reactor is 0.2 h, the reaction time in the second-order microchannel reactor is 0.1 h, and the reaction time in the third-order microchannel reactor is 0.35 h.

[0077] After weighing and calculation, the product yield of phenoxyethanol prepared in this embodiment is 91.28%.

[0078] In the above Examples 1-5 and Comparative Examples 1-5, the product generation rates of phenoxyethanol are the average product generation rates calculated after three repeated experiments, and the above experiments can illustrate that the microchannel continuous production process for synthesizing phenoxyethanol proposed in the present invention can effectively improve the generation rate of phenoxyethanol products, and in a multi-stage reaction system, by regulating the reaction conditions of each stage, the overall synthesis process can be more accurately regulated, so as to more efficiently and orderly regulate the synthesis process of phenoxyethanol in the actual production.

[0079] The above are only preferred embodiments of the present invention and are not intended to limit the present invention. For those skilled in the art, the present invention may have various modifications and variations. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included in the protection scope of the present invention.

Claims

1. A microchannel continuous production process for synthesizing phenoxyethanol, characterized in that: The following steps are involved: S1 preheats phenol and ethylene oxide through a microchannel heater respectively, and then passes them to the reactor group; The preheated phenol and ethylene oxide in S2 react in the reactor group: The first-stage microchannel reactor (21), the second-stage microchannel reactor (31) and the third-stage microchannel reactor (41) are sequentially fed into a first-stage microchannel reactor (21), a second-stage microchannel reactor (31) and a third-stage microchannel reactor (41) for reaction, wherein the first-stage microchannel reactor (21), the second-stage microchannel reactor (31) and the third-stage microchannel reactor (41) are connected in series end to end; S3: The crude phenoxyethanol obtained by the reaction is sent to a fractionation tower (51) for splitting and purification to obtain a phenoxyethanol product.

2. The microchannel continuous production process for synthesizing phenoxyethanol according to claim 1, characterized in that: In step S2, in the first-stage microchannel reactor (21), the mass ratio of the amount of phenol introduced to the amount of ethylene oxide introduced is 0.90-0.95:1; The reaction temperature of phenol and ethylene oxide in the first-stage microchannel reactor (21) is 100-150°C, the reaction residence time is 0.15-0.45h, and the first intermediate material is obtained by reaction.

3. The microchannel continuous production process for synthesizing phenoxyethanol according to claim 2, characterized in that: The reaction temperature of the first intermediate material in the second-stage microchannel reactor (31) is 100-150°C, the reaction residence time is 0.15-0.45h, and the second intermediate material is obtained by reaction.

4. The microchannel continuous production process for synthesizing phenoxyethanol according to claim 3, characterized in that: The reaction temperature of the second intermediate material in the three-stage microchannel reactor (41) is 150-180°C, the reaction residence time is 0.5-1.5h, and the reaction obtains crude phenoxyethanol and gas phase by-products.

5. The microchannel continuous production process for synthesizing phenoxyethanol according to claim 1, characterized in that: In step S3, the crude phenoxyethanol is fed into the fractionation tower (51) at a treatment temperature of 160-180°C and a fractionation time of 2-6 hours.

6. The microchannel continuous production process for synthesizing phenoxyethanol according to any one of claims 1 to 5, characterized in that: In step S1, the feed ends of the reactor group are connected to the phenol microchannel heater (12) and the ethylene oxide microchannel heater (14) respectively; The feed end of the phenol microchannel heater (12) is connected to the phenol raw material tank (11), and the feed end of the ethylene oxide microchannel heater (14) is connected to the ethylene oxide tank (13).

7. The microchannel continuous production process for synthesizing phenoxyethanol according to claim 6, characterized in that: The discharge ends of the phenol raw material tank (11) and the ethylene oxide tank (13) are respectively provided with flow valves (15), and the discharge ends of the phenol microchannel heater (12) and the ethylene oxide microchannel heater (14) are respectively provided with flow meters (16).

8. The microchannel continuous production process for synthesizing phenoxyethanol according to claim 6, characterized in that: The pipeline connecting the phenol microchannel heater (12) and the first-stage microchannel reactor (21), and the pipeline connecting the ethylene oxide microchannel heater (14) and the first-stage microchannel reactor (21) are both provided with a raw material one-way valve (22).

9. The microchannel continuous production process for synthesizing phenoxyethanol according to claim 6, characterized in that: The pipeline connecting the first-stage microchannel reactor (21) and the second-stage microchannel reactor (31) is provided with a second-stage one-way valve (32), the pipeline connecting the second-stage microchannel reactor (31) and the third-stage microchannel reactor (41) is provided with a third-stage one-way valve (42), and the pipeline connecting the third-stage microchannel reactor (41) and the distillation tower (51) is provided with a feed valve (52).

10. The microchannel continuous production process for synthesizing phenoxyethanol according to claim 1, characterized in that: The feed end of the first-stage microchannel reactor (21) is also provided with a feed pipe (23), and the feed end of the second-stage microchannel reactor (31) is also provided with a liquid inlet pipe (33).

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