An expandable flow reactor and continuous flow gas-liquid reaction system

Abstract

The utility model relates to a kind of scalable flow reactor and continuous flow gas-liquid reaction system.The reactor includes planar end plate, the gas and liquid flow channel board of alternative superposition, and the oil-wicking gas-permeable membrane interposed therebetween.The reactor is separated by membrane gas-liquid phase, forms efficient gas-liquid interface, significantly improves oxygen mass transfer efficiency, and avoids the security risks caused by direct contact of gas and liquid.The device structure is modular, and the reaction scale can be flexibly expanded by adjusting the number of flow channel boards to adapt to different production requirements.The continuous flow aerobic oxidation method based on the reactor can achieve high-selectivity oxidation of various alcohol substrates at normal temperature and pressure to generate carboxylic acid products.

Description

Technical Field

[0001] This utility model relates to the field of flow reaction equipment technology, specifically to a scalable flow reactor continuous flow gas-liquid reaction system. Background Technology

[0002] The oxidation of alcohols to aldehydes, ketones, and carboxylic acids is an important class of oxidation reactions in organic synthetic chemistry. Traditional methods typically employ stoichiometric or excess oxidants, such as oxides of chromium and manganese (Rocek, J. Am. Chem. Soc., 1971, 93, 5455; Powell, Org. Process Res. Dev., 1999, 3, 363). However, these reagents contain heavy metals, generate toxic waste liquids, and the reactions often require harsh, strongly acidic conditions, making the process complex and environmentally unfriendly (Rocek, J. Am. Chem. Soc., 1971). In contrast, oxygen is an inexpensive, readily available, and environmentally friendly oxidant. Air is even more ideal as an oxidant, requiring no preparation or transportation and readily available. Using oxygen or air as an oxidant in alcohol oxidation reactions not only improves atom economy but also significantly reduces environmental pollution and production costs. In oxygen-oxidized alcohol systems, catalysts are typically added to control product selectivity, with oxygen oxidizing the active catalytic substance to complete the catalytic cycle (Marsden, React. Chem. Eng., 2016, 1, 595). Significant progress has been made in this field over the past two decades, with researchers discovering inexpensive and efficient catalysts to achieve high selectivity. For example, Stahl et al. used (bpy)Cu... Ⅰ Using TEPMO as a catalyst and air as an indirect oxidant, primary alcohols can be selectively oxidized to aldehydes (Stahl, J. Am. Chem. Soc., 2013, 135, 2357). The Asahi Akira group used ferric nitrate, TEMPO, and inorganic halides as co-catalysts, and by introducing oxygen or air into the system, they were able to oxidize alcohols to carboxylic acids with yields exceeding 95% at room temperature and pressure (Ma, J. Am. Chem. Soc., 2016, 138, 8344).

[0003] Most experiments use laboratory round-bottom flasks as reaction vessels for small-scale (1 mmol) synthesis (Lumb, J. Am. Chem. Soc., 2014, 136, 7662; Jean, Org. Process Res. Dev., 2020, 24, 856). In such apparatus, a gas-liquid interface is formed between the reaction liquid and the gas above, with oxygen dissolving into the solvent to participate in the reaction. However, this type of apparatus faces two major challenges in scaling up synthesis: 1. Direct mixing of organic solvents and oxygen poses a risk of fire and explosion; 2. Oxygen has low solubility in commonly used organic solvents. In traditional round-bottom flasks, the gas-liquid contact area is limited, making oxygen mass transfer the rate-determining step and limiting the reaction rate. To address the problem of limited oxygen mass transfer, studies have shown that increasing the system pressure to 10-30 bar can improve oxygen solubility, thereby accelerating the reaction rate (Thompson, Tetrahedron, 2004, 60, 2917). However, this method requires expensive and complex pressure control devices, increasing equipment costs and operational complexity. Other studies have used gas-liquid mixing flow reactors, which increase the gas-liquid interface through thorough mixing of bubbles and liquid to accelerate oxygen mass transfer (Stahl, Org. Process Res. Dev., 2015, 19, 1548), but this simultaneously exacerbates the safety hazards associated with solvent and oxygen mixing. Therefore, efficiently and safely conducting oxygen oxidation reactions remains a challenge. Utility Model Content

[0004] To address the aforementioned technical problems and shortcomings in this field, this invention provides a scalable flow reactor. This reactor uses an oleophobic and breathable membrane to separate the flowing air from the reaction liquid, preventing direct gas-liquid mixing and thus improving production safety. Simultaneously, multiple flow channel plates in the reactor can be stacked alternately, allowing air and reaction liquid to be introduced separately, forming a gas-liquid interface, increasing the gas-liquid contact area, improving oxygen mass transfer efficiency, and allowing the number of flow channel plates to be flexibly adjusted according to the synthesis scale.

[0005] This utility model proposes an expandable flow reactor, comprising: a planar end plate, a flow channel plate, and an oleophobic and breathable membrane; wherein, the planar end plate includes: a first planar end plate and a second planar end plate; the flow channel plate includes: a flow channel plate body; an inlet and an outlet are respectively provided on both sides of the flow channel plate body; a cavity is provided in the middle of the flow channel plate body; the inlet and outlet respectively pass through the flow channel plate body and communicate with the cavity; a gasket is provided on at least one side of the flow channel plate; the gasket has the same shape as the cavity; the oleophobic and breathable membrane is disposed between the two flow channel plates to separate the gas and liquid phases and can be permeated by oxygen; the first planar end plate, at least two flow channel plates, and the second planar end plate are arranged in sequence and each is provided with a through hole at a corresponding position, and are fixed to each other by a connector passing through the through hole; the oleophobic and breathable membrane is squeezed and fixed during assembly by the gasket.

[0006] In this invention, the inner wall of the through hole of the first planar end plate or the second planar end plate is provided with threads, and each component is sealed by screws passing through each through hole.

[0007] In this invention, the flow channel plate is an open flow channel plate or a thin liquid layer flow channel plate; wherein, the cavity of the open flow channel plate is used for the flow of the reaction liquid; the cavity of the thin liquid layer flow channel plate is mostly filled, with only one window opened near the inlet and outlet for the liquid to enter and exit.

[0008] In this invention, the outer side length of the flow channel plate is 4~15 cm and the thickness is 4~10 mm (less than 4 mm makes it difficult to process the inlet and outlet pipes; excessive thickness will reduce the surface area / volume ratio and limit the gas-liquid contact area of ​​the reactor); the side length of the internal cavity window of the open flow channel plate is 2~10 cm; the side length of the internal cavity window of the thin liquid layer flow channel plate is 1~10 mm.

[0009] Preferably, the outer side length of the flow channel plate is 10–20 cm and the thickness is 3–10 mm; the side length of the internal cavity window of the open flow channel plate is 8–15 cm; and the side length of the internal cavity window of the thin liquid layer flow channel plate is 3–6 mm.

[0010] Alternatively, for synthesis of less than 1 g, a smaller pool, 4–64 cm, can be used. 2 (2–8 cm * 2–8 cm). The choice of 8–15 cm is mainly for a larger gas-liquid contact area, thereby increasing the reaction scale.

[0011] In this invention, the oleophobic and breathable membrane is a polytetrafluoroethylene membrane with an oleophobic surface treatment.

[0012] In this invention, the pore size of the oleophobic and breathable membrane is 0.1~1 μm (too small a pore size is not conducive to gas permeation through the membrane to reach the reaction site; too large a pore size makes it easy for liquid to permeate); the thickness of the oleophobic and breathable membrane is 0.1~0.3 mm (the 0.14 mm selected in this example mainly depends on the thickness of the membranes sold on the market); the side length of the oleophobic and breathable membrane is slightly larger than the side length of the cavity window.

[0013] Preferably, the pore size of the oleophobic and breathable membrane is 0.15–0.3 μm; the thickness of the oleophobic and breathable membrane is 0.1–0.2 mm; and the side length of the oleophobic and breathable membrane is slightly larger than the side length of the cavity window.

[0014] Based on the above, this utility model also proposes a continuous flow gas-liquid reaction system, which includes the scalable flow reactor of this utility model, a peristaltic pump, a gas pump, and a reaction liquid container; wherein, the initial reaction liquid is stored in the reaction liquid container and transported to the flow channel plate for reaction by the peristaltic pump, and flows back to the reaction liquid container for circulation, and after the reaction is completed, the reaction products are taken out from the reaction liquid container; the gas pump provides oxygen-containing gas to the flow channel plate.

[0015] The beneficial effects of this utility model include, but are not limited to:

[0016] This invention proposes a scalable flow reactor designed to optimize the safety and efficiency of oxygen oxidation reactions. The reactor separates the flowing reaction liquid from the air via an oleophobic and permeable membrane, avoiding the safety hazards associated with direct gas-liquid mixing in traditional reactors, while simultaneously enhancing oxygen mass transfer efficiency. This design allows for flexible expansion of the number of flow channels to accommodate reaction needs of varying scales. Experiments verified the reactor's high efficiency in the oxidation of 10 g of dodecanol to produce dodecanoic acid, achieving high yields at ambient temperature and pressure. In the future, this design holds promise for application in other substrates and other aerobic oxidation reactions, providing a wider range of solutions for green synthesis. Attached Figure Description

[0017] To more clearly illustrate the technical solutions in the embodiments of this utility model or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this utility model. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0018] Figure 1a , Figure 1b This is an exploded view of the scalable flow reactor assembly of this utility model.

[0019] Figure 2 This is a schematic diagram of the complete structure of the scalable flow reactor of this utility model after installation.

[0020] Figure 3 This is a schematic diagram of the reaction principle of the expandable flow reactor of this utility model (the reactor consists of three gas flow channel plates and two liquid flow channel plates).

[0021] Figure 4a , 4b This is a schematic diagram of the open flow channel plate and thin liquid layer flow channel plate of the expandable flow reactor of this utility model.

[0022] Figure 5a , 5b This is a schematic diagram of the liquid flow in the open flow channel plate and the thin liquid layer flow channel plate of the expandable flow reactor of this utility model. Detailed Implementation

[0023] The present invention will be further described below with reference to specific embodiments, and the advantages and features of the present invention will become clearer as the description proceeds. However, the embodiments are merely exemplary and do not constitute any limitation on the scope of the present invention. Those skilled in the art should understand that modifications or substitutions can be made to the details and form of the technical solution of the present invention without departing from the spirit and scope of the present invention, but all such modifications and substitutions fall within the protection scope of the present invention.

[0024] The following description of at least one exemplary embodiment is merely illustrative and is in no way intended to limit the present invention or its application or use. All other embodiments obtained by those skilled in the art based on the embodiments of the present invention without inventive effort are within the scope of protection of the present invention.

[0025] In all examples shown and discussed herein, any specific values ​​should be interpreted as merely exemplary and not as limitations. Therefore, other examples of exemplary embodiments may have different values.

[0026] Figures 1a-5b middle,

[0027] 1 - Planar end plate; 11 - First planar end plate; 12 - Second planar end plate;

[0028] 2 - Flow channel plate; 21 - Flow channel plate body; 22 - Outlet; 23 - Cavity; 24 - Open flow channel plate; 25 - Thin liquid layer flow channel plate; 26 - Inlet;

[0029] 3 - Oleophobic and breathable membrane;

[0030] 4 - Gaskets;

[0031] 5 - Through hole; 51 - Screw;

[0032] 6 - Peristaltic pump;

[0033] 7 - Gas pump;

[0034] 8 - Reaction liquid container;

[0035] 9-Flow meter.

[0036] The scalable flow reactor provided in this embodiment of the invention includes the following:

[0037] (1) Two flat end plates: serving as supports and seals. One end plate has a round hole, and the other has threads. The components are sealed by pressing with screws. The flat end plate materials include, but are not limited to, polytetrafluoroethylene and polyetheretherketone. In this embodiment of the present invention, the flat end plate material is polyetheretherketone.

[0038] (2) Flow channel plates: Each plate has an opening on each side, one side being the gas / liquid inlet and the other side being the gas / liquid outlet. Multiple flow channel plates alternately introduce air and reaction liquid to form a gas / liquid interface. The number of flow channel plates can be adjusted to adjust the total gas-liquid contact area of ​​the reactor. The outer side length of the flow channel plate is 15 cm, and the thickness is 4 mm. The geometry of the flow channel plate can be adjusted according to requirements. This utility model uses two shapes of flow channel plates, in which the open flow channel plate has an internal window side length of 10 cm; the thin liquid layer flow channel plate is mostly filled with space, with only a 5 mm side window near the inlet and outlet for liquid to enter and exit; in the thin liquid layer flow channel plate, the liquid only flows in the area of ​​the gasket bulge, greatly reducing the thickness of the flowing liquid. The materials of the flow channel plates include, but are not limited to, polytetrafluoroethylene (PTFE) and polyetheretherketone (PEEK). In this embodiment of the utility model, the flow channel plate material is PTFE.

[0039] (3) Oleophobic and breathable membrane: Located between the gas and liquid flow channels, separating the gas and liquid phases. Oxygen can permeate the oleophobic and breathable membrane and dissolve in the reaction solution. The oleophobic and breathable membrane is a polytetrafluoroethylene membrane with an oleophobic surface treatment, a pore size of 0.22 μm, and a thickness of 0.14 mm. The side length of the oleophobic and breathable membrane is slightly larger than the side length of the gasket window.

[0040] (4) Gaskets: Placed between the flow channel plate and the oleophobic and breathable membrane to ensure the flow cell is sealed. The gaskets are made of fluororubber, with an outer side length of 15 cm, an inner window side length of 10 cm, and a thickness of 0.5 mm. The two gaskets are pressed together during assembly to fix the oleophobic and breathable membrane. When using a thin liquid layer flow channel plate, the gaskets also create a liquid flow area, with the liquid flowing only within the 0.5 mm gasket on the side closest to the oleophobic and breathable membrane.

[0041] Two or more liquid flow channel plates can be placed inside the flow reactor to adjust the total gas-liquid contact area according to the reaction specifications.

[0042] Flow reactors can use thin-layer flow channels instead of open flow channels. The interior of a thin-layer flow channel is mostly filled, with only a thin layer of liquid remaining near the oleophobic, permeable membrane for flow. This thin-layer design reduces internal volume, allowing for an increase in the number of flow channels while maintaining the same reaction liquid volume, thereby increasing the total gas-liquid contact area and thus increasing oxygen flux.

[0043] Inside the flow reactor, multiple gas and liquid flow channel plates are placed alternately and separated by an oleophobic and breathable membrane.

[0044] The workflow of the flow reactor provided in this embodiment of the present invention includes the following:

[0045] The reaction solution is stored in a glass container and transported in parallel to each liquid flow channel plate at a constant flow rate by a peristaltic pump for reaction, and then flows back to the reaction solution container for circulation. Air is supplied by a gas pump, and the flow rate is controlled by a mass flow meter (MFC) to enter the gas flow channel plate at a constant flow rate, and then enters each flow channel plate in series to continuously supply oxygen to the system.

[0046] Based on the above scalable flow reactor, this invention also proposes a continuous flow aerobic oxidation method for synthesizing carboxylic acids from alcohols. The initial reaction solution is stored in a reaction solution container and transported to the flow channel plate for reaction by a peristaltic pump, and then flows back to the reaction solution container for circulation. After the reaction is completed, the reaction product is taken out from the reaction solution container. A gas pump provides oxygen-containing gas to the flow channel plate.

[0047] The initial reaction solution comprises a reaction substrate alcohol, a catalyst, and a solvent; wherein the catalyst comprises nitrates, nitroxide radical compounds, and inorganic halides, etc.

[0048] The reaction products contain carboxylic acid or ketone compounds;

[0049] The oxygen-containing gas is selected from pure oxygen, air, or other oxygen-containing mixtures. For economic reasons, air is preferred.

[0050] The reaction process of the method includes: an initial reaction solution circulating in a liquid flow channel plate at a set flow rate, oxygen-containing gas flowing in a gas flow channel plate at a set flow rate, and oxidizing the reaction substrate alcohol to the corresponding carboxylic acid or ketone compound at a temperature of 20~30℃, as shown in the following reaction formula:

[0051]

[0052] Reaction formula (I);

[0053] in,

[0054] The nitrate includes one or more of ferric nitrate nonahydrate, copper nitrate trihydrate, etc.; preferably, it is ferric nitrate nonahydrate.

[0055] The nitroxide free radical compound includes one or more of 2,2,6,6-tetramethylpiperidine-1-oxy radical (TEMPO), 4-hydroxy-2,2,6,6-tetramethylpiperidine-1-oxy radical (4-OH-TEMPO), etc.; preferably, it is 2,2,6,6-tetramethylpiperidine-1-oxy radical (TEMPO).

[0056] The inorganic halide includes one or more of potassium chloride, sodium chloride, etc.; preferably, it is potassium chloride.

[0057] The molar ratio of the reaction substrate alcohol, nitrate, nitroxide radical compound and inorganic halide is 100: (1~20): (1~30): (1~20); preferably, it is 40–60: 5–15: 10–20: 5–15.

[0058] The solvent includes one or more of dichloromethane, 1,2-dichloroethane, 1,1-dichloroethane, chloroform, toluene, acetonitrile, ethyl acetate, etc.; preferably, it is 1,2-dichloroethane.

[0059] The amount of solvent used is 100-1000 mL; preferably, it is 300-600 mL; based on the amount of nitrate used.

[0060] The concentration of nitrate in the solvent is 1.25–25 mmol / L; preferably, it is 5–25 mmol / L.

[0061] The reaction time is 6 to 48 hours; preferably, it is 24 hours.

[0062] The initial reaction liquid is circulated into each liquid flow channel plate at a flow rate of 1~20 sccm (too low a flow rate is not conducive to circulation, and too high a flow rate will generate large hydraulic pressure, causing the liquid to penetrate the diaphragm, which is not conducive to the stability of the system); the flow rate of the oxygen-containing gas is 50~300 sccm; the reactor contains at least two flow channel plates, preferably 5~20, which serve as gas flow channel plates and liquid flow channel plates respectively during feeding, and the gas flow channel plates and liquid flow channel plates are arranged alternately.

[0063] In one embodiment, the reactor consists of three gas flow channels and two liquid flow channels.

[0064] In another embodiment, the reactor consists of four open gas flow channel plates and three open liquid flow channel plates.

[0065] In another embodiment, the reactor may use thin-layer liquid flow channels instead of open flow channels, consisting of six open gas flow channels and five thin-layer liquid flow channels. This thin-layer design reduces the internal volume, and with the same volume of reaction liquid, the number of flow channels can be increased, thereby increasing the total gas-liquid contact area and thus increasing the oxygen flux.

[0066] To improve experimental convenience, this embodiment of the invention adopts a design scheme of air series connection and liquid parallel connection.

[0067] 1. For air series connection, a single mass flow meter (MFC) can be used for control, ensuring that the flow velocity within each flow channel plate is approximately consistent. If parallel connection is required (e.g., three plates), three MFCs are needed.

[0068] 2. Parallel connection of liquids facilitates collection of the reaction solution after the reaction. At the start of the reaction, the liquid flows from the bottom to the top of the flow channel plates. After the reaction, simply changing the direction of the peristaltic pump allows the liquid to flow back to the storage bottle from the bottom. If connected in series, the liquid from the first flow channel plate must be connected from the top to the bottom of the second flow channel plate via a hose. If this is done, reversing the peristaltic pump after the reaction will cause the liquid to become stuck at the connection point between the two plates, making collection difficult.

[0069] Example 1

[0070] This embodiment of the method for aerobic oxidation using air includes the following steps:

[0071] S1: Constructing a flow reactor: See Figure 1a , Figure 1b A flow reactor with multiple gas and liquid flow channels separated by an oleophobic and breathable membrane includes planar end plates at both ends, and alternately placed flow channels and oleophobic and breathable membranes. Air and liquid are alternately introduced into the flow channels to construct the gas-liquid interface required for the reaction.

[0072] S2: Aerobic Oxidation Reaction: The initial reaction solution is stored in a glass container and transported in parallel to each liquid flow channel plate at a flow rate of 5 sccm using a peristaltic pump, and then flows back to the reaction solution container for circulation. Air is supplied by a gas pump, with the flow rate controlled by a mass flow meter (MFC), entering the gas flow channel plate at a flow rate of 150 sccm, and then entering each flow channel plate in series to continuously supply oxygen to the system.

[0073] In Example 1, the flow reactor consisted of four open gas flow channels and three open liquid flow channels, and the conversion of dodecanol to dodecanoic acid was carried out at a temperature of 25°C.

[0074] (1) Weigh 10 mmol Fe(NO3)3·9H2O (4040 mg), 10 mmol TEMPO (1563 mg), and 10 mmol KCl (746 mg), place them in a 500 mL reagent bottle, and add 400 mL of 1,2-dichloroethane. After stirring for ten minutes, add 53 mmol dodecanol (10 g) and continue stirring.

[0075] (2) The above initial reaction solution was fed into three liquid flow channels in parallel through a peristaltic pump, and air was fed into four gas flow channels in series. The reaction was carried out for 24 hours.

[0076] (3) After the reaction is complete, return all the reaction solution to the reagent bottle. Take 0.2 mL of the reaction solution and add 0.4 mL of deuterated chloroform solution containing 0.05 M dibromomethane as an internal standard. Quantitative nuclear magnetic resonance (NMR) spectroscopy (1H NMR) is then performed. 1 The yield of dodecanoic acid was 93% as determined by ¹H NMR.

[0077] Example 2

[0078] To further improve the efficiency of aerobic oxidation in this invention, in Example 2, the flow reactor consisted of 6 open gas flow channels and 5 thin-layer liquid flow channels to increase the total gas-liquid contact area. All other conditions remained the same as in Example 1. After 12 hours of reaction, quantitative 1H NMR spectroscopy was performed. 1 The yield of dodecanoic acid was 93% as determined by ¹H NMR. This example further demonstrates that the method of this invention can flexibly change the total gas-liquid contact area by adjusting the number and geometry of the flow channel plates, thereby optimizing the reaction efficiency.

[0079] The above detailed embodiments are a description of the present utility model. It should not be considered that the specific embodiments of the present utility model are limited to these descriptions. For those skilled in the art, several simple deductions and substitutions can be made without departing from the concept of the present utility model, and all of these should be considered to fall within the protection scope of the present utility model.

Claims

1. A scalable flow reactor, characterized in that, include: Planar end plate (1), flow channel plate (2), and oleophobic and breathable membrane (3); among which, The planar end plate (1) includes: a first planar end plate (11) and a second planar end plate (12); The flow channel plate (2) includes: a flow channel plate body (21); an inlet (26) and an outlet (22) are respectively provided on both sides of the flow channel plate body (21); a cavity (23) is provided in the middle of the flow channel plate body (21); the inlet (26) and the outlet (22) respectively pass through the flow channel plate body (21) and communicate with the cavity (23); a gasket (4) is provided on at least one side of the flow channel plate (2); The oleophobic and breathable membrane (3) is disposed between the two flow channel plates (2) to separate the gas and liquid phases and can be permeated by oxygen; The first planar end plate (11), at least two flow channel plates (2), and the second planar end plate (12) are arranged and fixed in sequence.

2. The scalable flow reactor as described in claim 1, characterized in that, The first planar end plate (11), at least two flow channel plates (2) and the second planar end plate (12) are provided with through holes (5) at corresponding positions, and are fixed to each other by connecting members passing through the through holes (5); the oleophobic and breathable membrane (3) is squeezed and fixed during assembly by the gasket (4).

3. The scalable flow reactor as described in claim 2, characterized in that, The inner wall of the through hole (5) of the first planar end plate (11) or the second planar end plate (12) is provided with threads, and each component is squeezed and sealed by screws passing through each through hole (5).

4. The scalable flow reactor as described in claim 1, characterized in that, The flow channel plate (2) is an open flow channel plate (24) and / or a thin liquid layer flow channel plate (25); wherein, The cavity (23) of the open flow channel plate (24) is used for the flow of the reaction liquid; The cavity (23) of the thin liquid layer flow channel plate (25) is mostly filled, with only one window near the inlet and outlet for liquid to enter and exit.

5. The scalable flow reactor as described in claim 1 or 4, characterized in that, The outer side length of the flow channel plate (2) is 4–25 cm; the thickness is 3–10 mm; And / or, The side length of the internal cavity window of the open flow channel plate (24) is 2–20 cm; And / or, The side length of the internal cavity window of the thin liquid layer flow channel plate (25) is 1–10 mm.

6. The scalable flow reactor as described in claim 5, characterized in that, The outer side length of the flow slab (2) is 10–20 cm; the thickness is 4–6 mm.

7. The scalable flow reactor as described in claim 5, characterized in that, The side length of the internal cavity window of the open flow channel plate (24) is 8–15 cm.

8. The scalable flow reactor as described in claim 5, characterized in that, The internal cavity window of the thin liquid layer flow channel plate (25) has a side length of 3–6 mm.

9. The scalable flow reactor as described in claim 1, characterized in that, The oleophobic and breathable membrane (3) is a polytetrafluoroethylene membrane with an oleophobic surface treatment.

10. The scalable flow reactor as claimed in claim 1, characterized in that, The oleophobic and breathable membrane (3) has a pore size of 0.1–1 μm; And / or, The thickness of the oleophobic and breathable membrane (3) is 0.1–0.3 mm.

11. The scalable flow reactor as described in claim 10, characterized in that, The oleophobic and breathable membrane (3) has a pore size of 0.15–0.3 μm.

12. The scalable flow reactor as described in claim 10, characterized in that, The thickness of the oleophobic and breathable membrane (3) is 0.1–0.2 mm.

13. The scalable flow reactor as described in claim 1, characterized in that, The side length of the oleophobic and breathable membrane (3) is greater than the side length of the cavity (23) window.

14. The scalable flow reactor as described in claim 1, characterized in that, The shape of the gasket (4) is consistent with that of the cavity (23).

15. A continuous flow gas-liquid reaction system, characterized in that, The system includes a scalable flow reactor as described in any one of claims 1-14, a peristaltic pump (6), a gas pump (7), and a reaction liquid container (8); wherein, The initial reaction solution is stored in the reaction solution container (8) and transported to the flow channel plate (2) by the peristaltic pump (6) for reaction, and then flows back to the reaction solution container (8) for circulation; the gas pump (7) provides oxygen-containing gas to the flow channel plate (2).

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