CN221663031U - Modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation - Google Patents

Abstract

The utility model discloses a modularized flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation, which comprises a raw material system, an integrated condensation reaction system and a cooling liquid supply system, wherein the raw material system is a reactor tank; the integrated condensation reaction system comprises at least one integrated condensation reactor module, wherein the integrated condensation reactor module comprises two anode end plates, a cathode end plate arranged between the two anode end plates, and an electrode assembly arranged between the anode end plates and the cathode end plate; gas diffusion layers are arranged on two sides of the cathode end plate; the anode end plate facing the cathode end plate one end is provided with a net anode current collecting layer; the electrode assembly comprises an integrated membrane electrode and sealing gaskets arranged on two sides of the integrated membrane electrode. According to the utility model, an integrated condensing anode end plate is adopted, the temperature of electrolyte is reduced through a cooling chamber arranged in the reactor, the rate of non-electrochemical reaction of biomass derived platform molecules is reduced, and the electrochemical reaction proportion is improved; and a plurality of reactor modules are integrated, so that the reaction scale is enlarged.

Description

Modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation

Technical Field

The utility model belongs to the field of electrocatalytic oxidation, and in particular relates to a modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation.

Background Art

Biomass is the most abundant carbon-containing organic renewable resource on earth, which can replace fossil resources to produce fuels and chemicals. Biomass has a high oxygen content (40-45%) and is an ideal raw material for the preparation of oxygen-containing chemicals. Derivative platform molecules containing aldehyde and ketone functional groups can be converted into various commercial chemicals, including formic acid, 2,5-furandicarboxylic acid, furoic acid, adipic acid, etc. through a series of oxidation reactions. However, the inherent high reactivity of such functional groups makes them unstable under extreme conditions (strong acid, strong base, high temperature, etc.), and adverse side reactions will occur (especially under high substrate concentrations), affecting the reactivity. For example, glucose will spontaneously generate a series of organic acids (such as arabinose and lactic acid) under alkaline conditions, and 5-hydroxymethylfurfural can undergo polycondensation under alkaline conditions to produce dark brown humin.

Electrocatalytic oxidation can be driven by renewable electricity, which is in line with the concept of sustainable development. The reaction conditions are mild, and the cathode is coupled to produce hydrogen, making it a favorable tool for the preparation of high-value oxygenated chemicals from biomass-derived platform molecules. In recent years, the electrocatalytic oxidation of biomass-derived molecules has developed rapidly, especially in the development of catalysts. Professor Hu Chuangang of Beijing University of Chemical Technology reported the use of InOOH-Ov for the electrocatalytic oxidation of 5-hydroxymethylfurfural. The oxidation was carried out in 30 mL of an electrolyte containing 10 mmol L ^-1 of 5-hydroxymethylfurfural to obtain 8.75 mmol L ^-1 of 2,5-furandicarboxylic acid (Nat. Commun. 2023, 14, 2040). The article (Appl. Catal. B-Environ. 2023, 323, 122126) reported a NiMo ₃ S ₄ -R catalyst for the electrosynthesis of 2,5-furandicarboxylic acid. When 10 mmol L ^-1 of 5-hydroxymethylfurfural was used for electrocatalytic oxidation, 9.8 mmol L ^-1 of 2,5-furandicarboxylic acid was obtained. In order to improve the reaction activity, most studies were carried out under alkaline conditions, but 5-hydroxymethylfurfural will undergo non-electrochemical side reactions under alkaline conditions, especially polycondensation reactions, which is not conducive to the improvement of the selectivity of 2,5-furandicarboxylic acid. Therefore, current research focuses on low-concentration substrates and does not meet the needs of industrial production. Krebs demonstrated a stable strategy to convert unstable HMF into base-stable 5-hydroxymethyl-2-furancarboxylic acid and dihydroxymethylfuran through a base-catalyzed Cannizzaro reaction, which can be further oxidized to 2,5-furandicarboxylic acid. However, when the substrate concentration is 250 mM, the overall carbon balance is still low (~80%). Therefore, further research is still needed to improve the reaction carbon balance and target product selectivity.

Industrial production requires high reaction rate, large volume and continuous production, so it is necessary to explore how to achieve high concentration, high selectivity and high Faraday efficiency target product preparation under high substrate concentration and large reaction volume conditions. Reactors based on flow chemistry have the advantages of continuity and modularity, so the construction of modular flow chemical reactors is conducive to the industrial production of biomass molecular electrocatalytic oxidation coupled hydrogen production.

Utility Model Content

The utility model is proposed to realize the continuous and large-scale production of biomass-derived oxygen-containing chemicals. Its purpose is to provide a modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation, so as to solve the problems of low energy efficiency, uneven substrate distribution, limited mass transfer, low product selectivity, etc. in the process of reaction scale expansion, and realize modular continuous production of high-concentration commercial chemicals and simultaneous cathode co-production of high-purity hydrogen.

The utility model is realized by the following technical solutions:

A modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation, comprising a raw material system, an integrated condensation reaction system and a coolant supply system which are interconnected; the integrated condensation reaction system comprises at least one integrated condensation reactor module, the integrated condensation reactor module comprises two anode end plates, a cathode end plate arranged between the two anode end plates, and an electrode assembly arranged between the anode end plate and the cathode end plate; gas diffusion layers are arranged on both sides of the cathode end plate; a mesh anode current collecting layer is arranged at one end of the anode end plate facing the cathode end plate; the electrode assembly comprises an integrated membrane electrode and sealing gaskets arranged on both sides of the integrated membrane electrode.

In the above technical solution, the raw material system includes an electrolyte supply system, a substrate supply system and a static mixer; the electrolyte supply system includes an electrolyte storage tank and an electrolyte feed pump connected by a pipeline, and the electrolyte feed pump is connected to the inlet of the static mixer through a pipeline; the substrate supply mechanism includes a substrate storage tank and a substrate feed pump connected by a pipeline, and the substrate feed pump is connected to the inlet of the static mixer through a pipeline; the static mixer outlet is connected to the electrolyte feed port of the integrated condensation reaction system.

In the above technical solution, when the integrated condensation reaction system includes a plurality of integrated condensation reactor modules, the plurality of integrated condensation reactor modules are connected in parallel and/or in series.

In the above technical solution, the modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation also includes a direct current power supply.

In the above technical scheme, cathode reaction chambers are formed at both ends of the cathode end plate, a gas connector is formed at the upper end of the cathode reaction chamber, and a gas channel is formed at the lower end; a plurality of parallel gas channels are formed at the bottom of the cathode reaction chamber, and the two ends of the gas channels are respectively connected to the gas connector and the gas channel; the cathode reaction chambers at both ends of the cathode end plate are connected through the gas connector; the bottom of the gas channel is inclined so that the hydrogen generated by the cathode can be discharged smoothly to reduce the pressure inside the reaction chamber; a gas outlet is formed on the side wall of the cathode end plate, the gas outlet is connected to the gas channel, and the gas outlet is arranged at the lowest end of the bottom surface of the gas channel.

In the above technical solution, a pole ear is provided on the side of the cathode end plate, and the pole ear is used to connect the cathode wire.

In the above technical scheme, an anode reaction chamber and a cooling chamber are respectively formed on both sides of the anode end plate; an electrolyte feed port and an electrolyte discharge port connected to the anode reaction chamber, as well as a coolant inlet and a coolant outlet connected to the cooling chamber are respectively formed on the side walls of the anode end plate; the electrolyte feed port and the electrolyte discharge port are diagonally distributed; the coolant inlet and the coolant outlet are diagonally distributed; and an interlaced columnar flow trough is arranged inside the anode reaction chamber.

In the above technical solution, the sizes of the mesh anode current collecting layer and the gas diffusion layer are respectively the same as the bottom sizes of the anode reaction chamber and the cathode reaction chamber, and the mesh anode current collecting layer is embedded in the anode reaction chamber of the anode end plate.

In the above technical solution, the integrated membrane electrode comprises an anion exchange membrane, an anode catalyst layer arranged at the anode end of the anion exchange membrane and a cathode catalyst layer arranged at the cathode end of the anion exchange membrane, wherein the anode catalyst layer contacts the mesh anode current collecting layer 23; the cathode catalyst layer contacts the gas diffusion layer.

In the above technical solution, the size of the anode catalyst layer and the cathode catalyst layer is the same as the size of the anode reaction chamber and the cathode reaction chamber; the size of the anion exchange membrane is larger than the anode reaction chamber.

The beneficial effects of the utility model are:

The utility model provides a modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation. The electrolyte and the substrate are simultaneously introduced into a static mixer, and the substrate and the electrolyte are mixed more evenly in the static mixer, thereby avoiding insufficient alkali supply during the reaction due to uneven mixing of the alkaline electrolyte and the substrate, thereby affecting the selectivity and Faraday efficiency of the target product; the integrated membrane electrode is prepared by catalyst coating membrane technology, and the cathode and anode catalysts are tightly combined with the anion exchange membrane, which greatly reduces the distance between the electrodes, thereby reducing the reaction internal resistance and improving energy efficiency; an integrated condensing anode end plate is designed, and the electrolyte temperature is reduced by a built-in cooling chamber in the reactor, thereby reducing the rate of non-electrochemical reactions of unstable biomass-derived platform molecules and increasing the proportion of electrochemical reactions; multiple reactor modules are integrated to expand the reaction scale, realize continuous production of high-concentration commercial chemicals on a larger scale, and simultaneously produce high-purity hydrogen at the cathode, which provides the possibility for industrial production of biomass molecular electrocatalytic oxidation.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG1 is a schematic diagram of the structure of a modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation according to the present invention;

FIG2 is a schematic diagram of the structure of an integrated condensation reactor module in the present invention;

FIG3 is a schematic diagram of the structure of the cathode end plate of the utility model;

Figure 4 is a cross-sectional view of the side of the cathode end plate of the utility model

FIG5 is a schematic diagram of the structure of the anode end plate reaction chamber of the utility model;

FIG6 is a schematic diagram of the structure of the anode end plate cooling cavity of the utility model;

FIG7 is a schematic diagram of the composition of the integrated membrane electrode in the utility model;

8 is a schematic structural diagram of an integrated condensing reactor system in Example 2 of the present invention in which four reactor modules are connected in parallel;

9 is a schematic structural diagram of an integrated condensing reactor system in Example 3 of the present utility model with 10 reactor modules connected in parallel;

FIG. 10 is a comparison diagram of the Faraday efficiency and reactor operating voltage of 2,5-furandicarboxylic acid at different current densities in Application Example 1 of the present invention.

in:

1. Raw material system

11 Electrolyte storage tank 12 Substrate storage tank

13 Electrolyte feed pump 14 Substrate feed pump

15. Static mixer

2 Integrated condensation reactor module

21 Anode terminal plate

211 electrolyte inlet 212 electrolyte outlet

213 Coolant inlet 214 Coolant outlet

215 Anode reaction chamber 216 Cooling chamber

217 Anode wire hole slot

22 Cathode terminal plate

221 Gas outlet 222 Gas channel

223 Gas connector 224 Tab

225 cathode reaction chamber

23. Mesh anode current collector

24 Gasket

25 Integrated membrane electrode

251 Anode catalyst layer 252 Anion exchange membrane

253 Cathode catalyst layer

26 Gas Diffusion Layer

3 Coolant supply system

31. Low temperature constant temperature circulation device

For ordinary technicians in this field, other relevant drawings can be obtained based on the above drawings without any creative work.

DETAILED DESCRIPTION

In order to enable those skilled in the art to better understand the technical solution of the present invention, the technical solution of the present invention is further described below in conjunction with the accompanying drawings and through specific implementation methods.

As shown in FIG1 , a modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation includes a raw material system 1, an integrated condensation reaction system 2, and a coolant supply system 3 that are interconnected;

The raw material system includes an electrolyte supply system, a substrate supply system and a static mixer 15; the electrolyte supply system includes an electrolyte storage tank 11 and an electrolyte feed pump 13 connected by a pipeline, and the electrolyte feed pump 13 is connected to the inlet of the static mixer 15 through a pipeline; the substrate supply mechanism includes a substrate storage tank 12 and a substrate feed pump 14 connected by a pipeline, and the substrate feed pump 14 is connected to the inlet of the static mixer 15 through a pipeline; the outlet of the static mixer 15 is connected to the electrolyte feed port of the integrated condensation reaction system 2.

The cooling liquid supply system includes a low temperature constant temperature circulation device 31, which is connected to the cooling liquid inlet and outlet of the integrated condensation reaction system 2 through a pipeline. In this embodiment, the low temperature constant temperature circulation device 31 is a cooling circulation device integrating condensation and circulation.

The integrated condensation reaction system includes at least one integrated condensation reactor module. When the integrated condensation reaction system includes multiple integrated condensation reactor modules, the multiple integrated condensation reactor modules are connected in parallel and/or in series.

In this embodiment, the integrated condensing reactor unit includes two anode end plates, and the two anode end plates are connected in series.

The modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation also includes a direct current power supply.

In this embodiment, the DC power supply is an adjustable current-stabilized and voltage-stabilized DC power supply.

As shown in Figure 2, the integrated condensing reactor module includes two anode end plates 21, a cathode end plate 22 arranged between the two anode end plates 21, and an electrode assembly arranged between the anode end plate 21 and the cathode end plate 22; gas diffusion layers 26 are arranged on both sides of the cathode end plate 22; a mesh anode current collecting layer 23 is arranged at one end of the anode end plate 21 facing the cathode end plate 22; the electrode assembly includes an integrated membrane electrode 25 and sealing gaskets 24 arranged on both sides of the integrated membrane electrode 25.

The two anode end plates 21 of the integrated condensing reactor module are connected in series.

The components of the integrated condensation reaction system are fastened together by means of holes and bolts arranged around the pole plates and the sealing gaskets.

The sealing gasket 24 is a hollow rectangular frame structure, the size of the hollow is larger than the size of the anode catalyst layer 251 and the cathode catalyst layer 253 , and smaller than the size of the anion exchange membrane 252 and the gas diffusion layer 26 .

In this embodiment, the thickness of the sealing pad 24 is 0.02 cm to 0.5 cm, and the material thereof is polytetrafluoroethylene, silica gel, fluororubber, polyetheretherketone or rubber.

As shown in Figs. 3 and 4, cathode reaction chambers 225 are formed at both ends of the cathode end plate 22, a gas connector 223 is formed at the upper end of the cathode reaction chamber 225, and a gas channel 222 is formed at the lower end; a plurality of parallel gas channels are formed at the bottom of the cathode reaction chamber 225, and the two ends of the gas channels are respectively connected to the gas connector 223 and the gas channel 222; the cathode reaction chambers 225 at both ends of the cathode end plate 22 are connected through the gas connector 223; the bottom of the gas channel 222 is inclined so that the hydrogen generated by the cathode can be discharged smoothly to reduce the pressure inside the reaction chamber; the side wall of the cathode end plate 22 forms a gas outlet 221, which is connected to the gas channel 222, and the gas outlet 221 is arranged at the lowest end of the bottom surface of the gas channel 222. The gas channel 222 and the gas connector 223 are both rectangular through grooves.

In this embodiment, a pole ear 224 is provided on the side of the cathode end plate 22, and the pole ear 224 is used to connect the cathode wire.

As shown in Figures 5 and 6, an anode reaction chamber 215 and a cooling chamber 216 are formed on both sides of the anode end plate respectively; an electrolyte feed port 211 and an electrolyte discharge port 212 connected to the anode reaction chamber 215, as well as a coolant inlet 213 and a coolant outlet 214 connected to the cooling chamber 216 are formed on the side walls of the anode end plate respectively; the electrolyte feed port 211 and the electrolyte discharge port 212 are diagonally distributed; the coolant inlet 213 and the coolant outlet 214 are diagonally distributed; a metal plate of the same size as the cooling chamber 216 is arranged outside the cooling chamber 216 and is welded to the outside of the cooling chamber to form a sealed cooling chamber 216; an interlaced columnar flow trough is arranged inside the anode reaction chamber 215, and the electrolyte is more evenly distributed in the reaction chamber under the action of the flow trough, thereby promoting mass transfer.

The structure of the columnar flow channel is that a plurality of rectangular parallelepipeds are arranged in an alternating manner in the anode reaction chamber 215, and the gaps between the rectangular parallelepipeds form the columnar flow channel.

A plurality of guide plates are staggeredly arranged in the cooling cavity 216 to ensure that the coolant is evenly distributed in the cooling cavity.

In this embodiment, the anode end plate 21 and the cathode end plate 22 are both made of metal materials such as nickel, iron or titanium.

In this embodiment, an anode wire hole groove 217 is provided on the side of the anode end plate 21 , and the anode wire hole groove 217 is used to connect the anode wire.

In this embodiment, a plurality of grooves are arranged around the anode reaction chamber to improve the sealing performance of the reaction device.

In this embodiment, the sizes of the mesh anode current collecting layer and the gas diffusion layer are respectively the same as the sizes of the bottoms of the anode reaction chamber and the cathode reaction chamber, and the areas are greater than 100 cm ² .

In this embodiment, the mesh anode current collecting layer 23 is directly embedded in the reaction cavity of the anode end plate 21 .

As shown in Figure 7, the integrated membrane electrode 25 includes an anion exchange membrane 252, an anode catalyst layer 251 arranged at the anode end of the anion exchange membrane 252, and a cathode catalyst layer 253 arranged at the cathode end of the anion exchange membrane 252. The anode catalyst layer 251 is in contact with the mesh anode current collecting layer 23; the cathode catalyst layer 253 is in contact with the gas diffusion layer 26.

The anode catalyst layer 251 and the cathode catalyst layer 253 on both sides of the anion exchange membrane 252 are both formed by using a coating membrane technology.

The size of the anode catalyst layer 251 and the cathode catalyst layer 253 is the same as that of the anode reaction chamber and the cathode reaction chamber, and the area is greater than 100 cm ² ; the size of the anion exchange membrane 252 is slightly larger than the reaction chamber;

The catalyst coating membrane technology refers to adding conductive carbon black and anion ionomer to powdered anode catalyst and cathode catalyst in a certain proportion to prepare catalyst ink, which is evenly sprayed on both sides of the anion exchange membrane using an ultrasonic sprayer, with a catalyst loading of 0.5-4 mg/cm ² ; the sprayed anion exchange membrane is hot-pressed using a hot press, the temperature of the hot press is set to 40-100°C, the pressure is set to 30-80 bar/cm ² , and the hot pressing time is 2-10 minutes.

Example 2

As shown in Figure 8, based on Example 1, this embodiment is assembled in parallel with multiple reactor modules. In this embodiment, a total of 4 integrated condensation reactor modules connected in parallel are arranged, and the 4 reactor modules are assembled separately. The electrolyte at the outlet of the static mixer is divided into 4 parts, which are respectively introduced into the electrolyte feed ports of the 4 integrated condensation reactor modules. The electrolyte passes through the two anode reaction chambers of each reactor module in turn, and finally flows out from the electrolyte outlet of another anode end plate. The electrolyte of the four reactor modules is merged into the same product storage tank in a parallel manner. The cathode gas outlets of the 4 reactor modules are collected in parallel to the main hydrogen pipeline for centralized storage. The coolant is passed into each reactor module in a parallel manner, and is discharged from the coolant outlet and then returned to the low-temperature constant temperature circulation device. The four reactor modules are individually controlled by four DC power supplies. Gate valves are set at the gas outlet, electrolyte outlet and coolant outlet of each reactor module. The appropriate number of reactor modules is selected according to the reaction requirements, and the gate valve is opened when the reactor module is in operation.

Example 3

As shown in Figure 9, based on Example 1, this embodiment is assembled in parallel with multiple reactor modules. In this embodiment, 10 integrated condensation reactor modules connected in parallel are arranged, and 10 reactor modules are assembled separately. The electrolyte at the outlet of the static mixer is divided into 10 parts, which are respectively introduced into the electrolyte feed ports of 10 integrated condensation reactor modules. The electrolyte passes through the two anode reaction chambers of each reactor module in turn, and finally flows out from the electrolyte outlet of another anode end plate. The electrolyte of the four reactor modules is merged into the same product storage tank in parallel. The cathode gas outlets of the 10 reactor modules are collected in parallel to the main hydrogen pipeline for centralized storage. The coolant is introduced into each reactor module in parallel, and is discharged from the coolant outlet and then returned to the low-temperature constant temperature circulation device. The 10 reactor modules are individually controlled by 10 DC power supplies. Gate valves are set at the gas outlet, electrolyte outlet and coolant outlet of each reactor module. The appropriate number of reactor modules is selected according to the reaction requirements, and the gate valve is opened when the reactor module is in operation.

The use of the utility model:

During use, the alkaline electrolyte and the aqueous solution containing biomass-derived molecules are stored in the corresponding electrolyte storage tank and substrate storage tank, respectively, and are pumped in by the electrolyte feed pump and the substrate feed pump, respectively. The electrolyte and the substrate are introduced into the inlet of the static mixer, where the electrolyte and the substrate are quickly and evenly mixed, and then introduced into the integrated condensation reactor module through the electrolyte feed port to enter the anode reaction chamber. After the electrolyte passes through the first anode end plate reaction chamber, it flows out from the electrolyte outlet of the first anode end plate and then immediately enters the electrolyte inlet of the second anode end plate, and finally flows out from the electrolyte outlet of the second anode end plate. Under the action of the staggered columnar flow trough and the large-area anode catalyst, the substrate is quickly oxidized to the target product and hydrogen is precipitated at the cathode. At the same time, the low-temperature constant temperature circulation device sets a certain temperature according to the reaction requirements, and the coolant enters the cooling chamber of the first anode end plate from the coolant feed port of the first anode end plate, and then passes through the cooling chambers of the two anode end plates in sequence, and finally flows out from the coolant outlet of the cooling chamber of the second anode end plate and returns to the low-temperature constant temperature circulation device. The coolant takes away the Joule heat generated during the reaction. The integrated condensing reactor module is based on the principle of solid polymer electrolyte membrane. No reaction liquid is introduced into the cathode. The high-purity hydrogen generated by the cathode during the reaction is directly discharged and collected from the cathode gas outlet without gas-liquid separation and purification. During the reaction, the reactor modules in this embodiment can be connected in series, in parallel, or in series and in parallel. The number and combination of the reactor modules are determined according to the concentration of the biomass-derived molecules.

Application Example 1

Example 1 is applied to the electrocatalytic oxidation of biomass derivatives to prepare 2,5-furandicarboxylic acid. In this application example, the concentration of the 5-hydroxymethylfurfural aqueous solution is 0.6 mol/L, the alkaline electrolyte is 3 mol/L potassium hydroxide, and the 5-hydroxymethylfurfural and potassium hydroxide solutions are introduced into the static mixer at the same flow rate.

In this application example, the area of a single anode and cathode is 100 ^cm2 (i.e., the area of the anode and cathode electrodes in each reactor module is 200 ^cm2 ), the anode is sprayed with 8.0 cm×12.5 cm nickel cobalt molybdate ( _NiCoMoO4 ) catalyst, the catalyst loading is 2.0±0.05 mg cm ^-2 , the cathode is sprayed with 8.0 cm×12.5 cm commercial ruthenium oxide (RuO2) catalyst, the catalyst loading is 1±0.05 mg cm ^-2 , and the anion exchange membrane uses FAA-3-50 produced by Fumar, Germany. The temperature of the hot press is set to 60°C, and the pressure is set to 50 bar cm ^-2 . The temperature of the low temperature constant temperature circulation device is set to 5°C.

As shown in Figure 10, at currents of 20 A (current density 100 mA cm ^-2 ) and 120 A (current density 600 mA cm ^-2 ), the operating voltages are 1.9 V and 2.7 V respectively, the operating power of a single reactor module can exceed 300 W, and the Faradaic efficiency of 2,5-furandicarboxylic acid at 100 mA cm ^-2 exceeds 95%.

The utility model provides a modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation. The electrolyte and substrate are simultaneously introduced into a static mixer, in which the substrate and electrolyte are mixed more evenly, avoiding the lack of alkali supply during the reaction due to uneven mixing of the alkaline electrolyte and the substrate, thereby affecting the selectivity and Faraday efficiency of the target product; the integrated membrane electrode is prepared by catalyst coating membrane technology, and the cathode and anode catalysts are closely combined with the anion exchange membrane, which greatly reduces the distance between the electrodes, thereby reducing the internal resistance of the reaction and improving energy efficiency; the integrated condensing anode end plate is designed, and the electrolyte temperature is reduced through the built-in cooling chamber of the reactor, reducing the rate of non-electrochemical reactions of unstable biomass-derived platform molecules, and increasing the proportion of electrochemical reactions; multiple reactor modules are integrated to expand the reaction scale, realize continuous production of high-concentration commercial chemicals on a larger scale, and simultaneously produce high-purity hydrogen at the cathode, which provides the possibility for the industrial production of electrocatalytic oxidation of biomass molecules.

It should be noted that, in the absence of conflict, the embodiments of the present invention and the features in the embodiments can be combined with each other.

In the description of the present utility model, it should be understood that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside" and the like indicate positions or positional relationships based on the positions or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present utility model and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the present utility model. In addition, the terms "first", "second", etc. are only used for descriptive purposes, and cannot be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Therefore, features defined as "first", "second", etc. may explicitly or implicitly include one or more of the features. In the description of the present utility model, unless otherwise specified, "multiple" means two or more.

In the description of the present invention, it should be noted that, unless otherwise clearly specified and limited, the terms "installation", "connection" and "connection" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be an indirect connection through an intermediate medium, or it can be the internal communication of two components. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood by specific circumstances.

The applicant declares that the above is only a specific implementation method of the present utility model, but the protection scope of the present utility model is not limited thereto. Technical personnel in the relevant technical field should understand that any changes or substitutions that can be easily thought of by technical personnel in the relevant technical field within the technical scope disclosed in the present utility model fall within the protection scope and disclosure scope of the present utility model.

Claims (10)

1. A modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation, comprising a raw material system (1), an integrated condensation reaction system (2) and a coolant supply system (3) which are interconnected; the integrated condensation reaction system comprises at least one integrated condensation reactor module, characterized in that: the integrated condensation reactor module comprises two anode end plates (21), a cathode end plate (22) arranged between the two anode end plates (21), and an electrode assembly arranged between the anode end plate (21) and the cathode end plate (22); gas diffusion layers (26) are arranged on both sides of the cathode end plate (22); a mesh anode current collecting layer (23) is arranged at one end of the anode end plate (21) facing the cathode end plate (22); and the electrode assembly comprises an integrated membrane electrode (25) and sealing gaskets (24) arranged on both sides of the integrated membrane electrode (25). 2. The modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation according to claim 1 is characterized in that: the raw material system comprises an electrolyte supply system, a substrate supply system and a static mixer (15); the electrolyte supply system comprises an electrolyte storage tank (11) and an electrolyte supply pump (13) connected by a pipeline, and the electrolyte supply pump (13) is connected to the inlet of the static mixer (15) through a pipeline; the substrate supply mechanism comprises a substrate storage tank (12) and a substrate supply pump (14) connected by a pipeline, and the substrate supply pump (14) is connected to the inlet of the static mixer (15) through a pipeline; the outlet of the static mixer (15) is connected to the electrolyte feed port of the integrated condensation reaction system (2). 3. The modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation according to claim 1 is characterized in that: when the integrated condensation reaction system includes multiple integrated condensation reactor modules, the multiple integrated condensation reactor modules are connected in parallel and/or in series. 4. The modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation according to claim 1, characterized in that the modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation also includes a direct current power supply. 5. The modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation according to claim 1, characterized in that: cathode reaction chambers (225) are formed at both ends of the cathode end plate (22), a gas connector (223) is formed at the upper end of the cathode reaction chamber (225), and a gas channel (222) is formed at the lower end; a plurality of parallel gas channels are formed at the bottom of the cathode reaction chamber (225), and the two ends of the gas channels are respectively connected to the gas connector (223) and the gas channel (222); the cathode reaction chambers (225) at both ends of the cathode end plate (22) are connected through the gas connector (223); the bottom of the gas channel (222) is inclined so that the hydrogen generated by the cathode can be discharged smoothly to reduce the pressure inside the reaction chamber; a gas outlet (221) is formed on the side wall of the cathode end plate (22), the gas outlet (221) is connected to the gas channel (222), and the gas outlet (221) is arranged at the lowest end of the bottom surface of the gas channel (222). 6. The modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation according to claim 1, characterized in that: a pole ear (224) is provided on the side of the cathode end plate (22), and the pole ear (224) is used to connect the cathode wire. 7. The modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation according to claim 1 is characterized in that: an anode reaction chamber (215) and a cooling chamber (216) are formed on both sides of the anode end plate; an electrolyte feed port (211) and an electrolyte discharge port (212) connected to the anode reaction chamber (215), as well as a coolant inlet (213) and a coolant outlet (214) connected to the cooling chamber (216) are formed on the side walls of the anode end plate; the electrolyte feed port (211) and the electrolyte discharge port (212) are distributed diagonally; the coolant inlet (213) and the coolant outlet (214) are distributed diagonally; and a staggered columnar flow trough is arranged inside the anode reaction chamber (215). 8. The modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation according to claim 7, characterized in that the mesh anode current collecting layer (23) and the gas diffusion layer (26) are respectively the same size as the bottom of the anode reaction chamber (215) and the cathode reaction chamber (225), and the mesh anode current collecting layer (23) is embedded in the anode reaction chamber (215) of the anode end plate (21). 9. The modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation according to claim 1, characterized in that: the integrated membrane electrode (25) comprises an anion exchange membrane (252), an anode catalyst layer (251) arranged at the anode end of the anion exchange membrane (252), and a cathode catalyst layer (253) arranged at the cathode end of the anion exchange membrane (252), wherein the anode catalyst layer (251) is in contact with the mesh anode current collecting layer 23; and the cathode catalyst layer (253) is in contact with the gas diffusion layer (26). 10. The modular flow reactor for electrocatalytic hydrogen production coupled with biomass molecular oxidation according to claim 9, characterized in that: the size of the anode catalyst layer (251) and the cathode catalyst layer (253) are the same as the size of the anode reaction chamber and the cathode reaction chamber; the size of the anion exchange membrane (252) is larger than the anode reaction chamber.