Mobile vanadium-based electric fuel energy storage and supply system

Abstract

The present application discloses a flow-type vanadium-based electric fuel energy storage and supply system, comprising: a stack reaction module, an electrolyte drive module, and a medium storage module. The stack reaction module comprises an oxygen evolution reaction flow unit, a vanadium electrolyte flow unit, and an oxygen reduction reaction flow unit, each of which is arranged adjacent to each other. The first flow field plate of the oxygen evolution reaction flow unit is provided with a bionic dendritic interdigitated first flow channel; the second flow field plate of the vanadium electrolyte flow unit is provided with a bidirectional spiral interdigitated second flow channel; the third flow field plate of the oxygen reduction reaction flow unit is provided with a multi-stage fractal interdigitated third flow channel; the medium storage module comprises a vanadium electrolyte storage tank and a reaction medium storage tank, which are arranged on opposite sides of the stack reaction module. The vanadium electrolyte storage tank is connected to the second flow field plate, and the reaction medium storage tank is connected to the first flow field plate and the third flow field plate, respectively. This system improves system integration while reducing costs.

Description

Technical Field

[0001] The present application relates to the field of electrochemical energy storage, and specifically to a flow-type vanadium-based electric fuel energy storage and supply system. Background Art

[0002] Existing vanadium-air batteries have the following advantages over all-vanadium flow batteries: the energy density is doubled, and higher instantaneous power can be provided at the same volume and mass, making it suitable for high-power output scenarios; one side of the battery is replaced with air, reducing the cost of battery active materials; the operating temperature range is wider, and it can work normally from room temperature to 60°C, and can adapt to more extreme working conditions.

[0003] However, existing vanadium-air batteries use two battery packs for separate charging and discharging processes, resulting in a relatively high overall system complexity and cost. They cannot be deployed and used on mobile energy storage devices such as electric vehicles, and their application range is relatively narrow.

[0004] Therefore, how to improve the integration of energy storage and power supply systems while reducing costs so that they can be applied in the field of mobile energy storage has become an urgent problem to be solved. Summary of the Invention

[0005] The present application provides a mobile vanadium-based electric fuel energy storage and supply system, which aims to improve the integration of the energy storage and supply system on the basis of reducing costs so that it can be applied to the field of mobile energy storage.

[0006] On the one hand, an embodiment of the present application provides a flow-type vanadium-based electric fuel energy storage and supply system, comprising: a stack reaction module, an electrolyte drive module and a medium storage module, wherein the electrolyte drive module is used to connect and drive the stack reaction module and the medium storage module to realize charging or discharging of the energy storage and supply system; the stack reaction module comprises an oxygen evolution reaction flow unit, a vanadium electrolyte flow unit and an oxygen reduction reaction flow unit arranged adjacent to each other; the oxygen evolution reaction flow unit comprises a first flow field plate, a first flow channel is provided on the first flow field plate, and the first flow channel is a bionic dendritic interdigitated type ; The vanadium electrolyte flow unit includes a second flow field plate, a second flow channel is provided on the second flow field plate, and the second flow channel is a bidirectional spiral interdigitated type; the oxygen reduction reaction flow unit includes a third flow field plate, a third flow channel is provided on the second flow field plate, and the third flow channel is a multi-stage fractal interdigitated type; the medium storage module includes a vanadium electrolyte storage tank and a reaction medium storage tank, the vanadium electrolyte storage tank and the reaction medium storage tank are arranged on opposite sides of the fuel cell reaction module, the vanadium electrolyte storage tank is connected to the second flow field plate, and the reaction medium storage tank is respectively connected to the first flow field plate and the third flow field plate.

[0007] Optionally, in some embodiments of the present application, the first flow field plate is a gradient pore structure made of titanium alloy material by laser three-dimensional printing, and the gradient porosity of the first flow field plate is between 50% and 85%.

[0008] Optionally, in some embodiments of the present application, a catalyst layer formed of iridium oxide is provided on the surface of the first flow field plate, and the loading value of the catalyst layer is between 1.5 mg / cm2 and 2.5 mg / cm2.

[0009] Optionally, in some embodiments of the present application, the value of the main channel width of the first flow channel is 2 mm, the value of the branch channel width is 0.8 mm, and the value of the flow channel depth is 1.5 mm.

[0010] Optionally, in some embodiments of the present application, the second flow field plate is made of graphite carbon felt, and the specific surface area of ​​the second flow field plate is 800 square meters per gram.

[0011] Optionally, in some embodiments of the present application, the pitch angle of the second flow channel is 15 degrees, and the cross-sectional area of ​​the second flow channel is 2.4 square millimeters.

[0012] Optionally, in some embodiments of the present application, a polyperfluorosulfonic acid-based composite membrane is provided on the surface of the second flow field plate, and the thickness of the polyperfluorosulfonic acid-based composite membrane is 183 microns.

[0013] Optionally, in some embodiments of the present application, the third flow field plate is a titanium mesh, and the pore size of the titanium mesh is 10 microns.

[0014] Optionally, in some embodiments of the present application, a catalyst layer formed of platinum is provided on the surface of the third flow field plate, and a loading value of the catalyst layer includes 0.5 mg per square centimeter.

[0015] Optionally, in some embodiments of the present application, the third flow channel includes a primary flow channel and a secondary flow channel, the width of the primary flow channel is 1.5 mm, and the width of the secondary flow channel is 0.5 mm.

[0016] Optionally, in some embodiments of the present application, the volume of the vanadium electrolyte storage tank is 5 cubic meters, and the material used for the lining of the vanadium electrolyte storage tank includes fluororubber and / or silicon carbide.

[0017] Optionally, in some embodiments of the present application, the medium storage module further includes a tank status monitoring unit, which includes an ultrasonic concentration sensor, an online redox potential monitoring probe, and a tank status sensor; wherein the ultrasonic concentration sensor and the online redox potential monitoring probe are provided in the vanadium electrolyte storage tank, and the tank status sensor is provided in the reaction medium storage tank, and the tank status sensor is used to monitor the pressure, temperature and pH value inside the reaction medium storage tank.

[0018] Optionally, in some embodiments of the present application, the reaction medium storage tank stores acidic energy storage fluid medium and high-pressure air medium in stages, and the pH value of the acidic energy storage fluid medium includes 0.5.

[0019] Optionally, in some embodiments of the present application, an isolation plate is further provided in the reaction medium storage tank. The isolation plate is made of nanomaterials and is used to separate the gaseous medium and the liquid medium in the reaction medium storage tank.

[0020] Optionally, in some embodiments of the present application, the stack reaction module further includes: an ion exchange unit, a current collector unit and a fixing unit, the ion exchange unit including a first ion exchange membrane and a second ion exchange membrane, the first ion exchange membrane is arranged between the oxygen evolution reaction flow unit and the vanadium electrolyte flow unit, and the second ion exchange membrane is arranged between the vanadium electrolyte flow unit and the oxygen reduction reaction flow unit; the current collector unit includes a first copper plate current collector and a second copper plate current collector, the first copper plate current collector is arranged on the side of the oxygen evolution reaction flow unit away from the first ion exchange membrane, and the second copper plate current collector is arranged on the side of the oxygen reduction reaction flow unit away from the second ion exchange membrane; the fixing unit includes a first end plate and a second end plate, the first end plate is arranged on the side of the first copper plate current collector away from the oxygen evolution reaction flow unit, and the second end plate is arranged at The second copper plate current collector is away from one side of the oxygen reduction reaction flow unit; the oxygen evolution reaction flow unit also includes a first sealing gasket, which is arranged between the first flow field plate and the first ion exchange membrane; the vanadium electrolyte flow unit also includes a second sealing gasket and a third sealing gasket, the second sealing gasket is arranged between the first ion exchange membrane and the second flow field plate, and the third sealing gasket is arranged between the second flow field plate and the second ion exchange membrane; the oxygen reduction reaction flow unit also includes a fourth sealing gasket, which is arranged between the second ion exchange membrane and the third flow field plate; the electrolyte drive module includes a battery, a first pipeline and a second pipeline, the first pipeline is used to connect the battery and the stack reaction module, and the second pipeline is used to connect the stack reaction module and the medium storage module to charge or discharge the battery.

[0021] Compared to existing technologies, the mobile vanadium-based electric fuel energy storage and supply system provided in this application integrates the two independent battery packs required for traditional vanadium-air batteries into a single functional module by adopting an integrated charge-discharge stack reaction module, reducing the number of system components by 40% and the volume by 35%. Furthermore, through the multiphase fluid coordinated control technology of interdigitated flow field plates, efficient coupling of oxygen evolution (OER) and oxygen reduction (ORR) reactions is achieved, increasing the power density to 1.8 times that of traditional structures while reducing manufacturing costs by 50%. This achieves a higher level of integration of the energy storage and supply system while reducing costs, making it suitable for application in the field of mobile energy storage. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] Figure 1 It is a schematic diagram of the mobile vanadium-based electric fuel energy storage and supply system provided by this application;

[0023] Figure 2 It is a schematic diagram of the reaction medium storage tank provided by the present application;

[0024] Figure 3 This is the constant voltage charging curve of the battery of the mobile vanadium-based electric fuel energy storage and supply system provided by the present application under constant voltage charging;

[0025] Figure 4 This is the discharge performance curve corresponding to constant current discharge at different current densities of the mobile vanadium-based electric fuel energy storage and supply system provided in this application;

[0026] Figure 5 This is the battery discharge performance curve of the mobile vanadium-based electric fuel energy storage and supply system provided by this application at different gas flow rates;

[0027] Figure 6 This is the battery discharge performance curve of the mobile vanadium-based electric fuel energy storage and supply system provided by the present application at different vanadium electrolyte flow rates;

[0028] Figure 7 This is the battery discharge performance curve at different operating temperatures of the mobile vanadium-based electric fuel energy storage and supply system provided in this application. DETAILED DESCRIPTION

[0029] The technical solutions in the embodiments of the present application will be described below in conjunction with the drawings in the embodiments of the present application. The described technical solutions are only used to explain and illustrate the ideas of the present application and should not be regarded as limiting the scope of protection of the present application.

[0030] The various embodiments provided in this application are similar, and features in different embodiments may be combined with each other.

[0031] like Figure 1 As shown, an embodiment of the present application provides a flow-type vanadium-based electric fuel energy storage and supply system, including: a fuel cell reaction module 1, an electrolyte drive module 2 and a medium storage module 3. The electrolyte drive module 2 is used to connect and drive the fuel cell reaction module 1 and the medium storage module 3 to realize charging or discharging of the energy storage and supply system.

[0032] In the embodiment of the present application, the stack reaction module 1 includes an oxygen evolution reaction flow unit 10, a vanadium electrolyte flow unit 20, and an oxygen reduction reaction flow unit 30, which are arranged adjacent to each other. Preferably, the vanadium electrolyte flow unit 20 is arranged between the oxygen evolution reaction flow unit 10 and the oxygen reduction reaction flow unit 30.

[0033] Specifically, the oxygen evolution reaction (OER) flow unit 10 includes a first flow field plate 11 , on which a first flow channel is provided. The first flow channel is a bionic dendritic interdigitated type.

[0034] Specifically, the vanadium electrolyte flow unit 20 includes a second flow field plate 21 , on which a second flow channel is provided. The second flow channel is a bidirectional spiral interdigital type.

[0035] Specifically, the oxygen reduction reaction (ORR) flow unit 30 includes a third flow field plate 31 . The second flow field plate 21 is provided with a third flow channel, and the third flow channel is a multi-stage fractal interdigitated type.

[0036] Specifically, the medium storage module 3 includes a vanadium electrolyte storage tank 40 and a reaction medium storage tank 50. The vanadium electrolyte storage tank 40 and the reaction medium storage tank 50 are arranged on opposite sides of the fuel cell reaction module 1. The vanadium electrolyte storage tank 40 is connected to the second flow field plate 21, and the reaction medium storage tank 50 is connected to the first flow field plate 11 and the third flow field plate 31 respectively.

[0037] The mobile vanadium-based electric fuel energy storage and supply system provided in this application utilizes an integrated charge-discharge stack reaction module 1, integrating the two independent battery groups 24 required for a traditional vanadium-air battery 24 into a single functional module. This reduces the number of system components by 40% and the volume by 35%. Furthermore, through the multiphase fluid coordinated control technology of interdigitated flow field plates, the system achieves efficient coupling of the oxygen evolution (OER) and oxygen reduction (ORR) reactions, increasing the power density to 1.8 times that of traditional structures while reducing manufacturing costs by 50%. This achieves a higher level of integration of the energy storage and supply system while reducing costs, making it suitable for application in the field of mobile energy storage.

[0038] In the embodiment of the present application, the first flow field plate 11 is a gradient pore structure made of titanium alloy material by laser 3D printing, and the gradient porosity of the first flow field plate 11 is between 50% and 85%. The pores on the first flow field plate 11 are distributed in a gradient manner.

[0039] In an embodiment of the present application, a catalyst layer formed of iridium oxide (IrO2) is provided on the surface of the first flow field plate 11. The catalyst layer has a loading value between 1.5 mg / cm2 and 2.5 mg / cm2. The loading values ​​of the catalyst layer include 1.5 mg / cm2, 1.6 mg / cm2, 1.7 mg / cm2, 1.8 mg / cm2, 1.9 mg / cm2, 2 mg / cm2, 2.1 mg / cm2, 2.2 mg / cm2, 2.3 mg / cm2, 2.4 mg / cm2, and 2.5 mg / cm2. Preferably, the catalyst layer has a loading value of 2 mg / cm2.

[0040] In an embodiment of the present application, the value of the main channel width of the first flow channel includes 2 mm, the value of the branch channel width includes 0.8 mm, and the value of the flow channel depth includes 1.5 mm. Specifically, the value of the main channel width of the first flow channel includes 1.8 mm, 1.9 mm, 2 mm, 2.1 mm, and 2.2 mm, the value of the branch channel width includes 0.6 mm, 0.7 mm, 0.8 mm, 0.9 mm, and 1 mm, and the value of the flow channel depth includes 1.3 mm, 1.4 mm, 1.5 mm, 1.6 mm, and 1.7 mm. Among them, the values ​​of the main channel width, the branch channel width, and the flow channel depth of the above-mentioned first flow channel can be arbitrarily combined. Preferably, the main channel width of the first flow channel is 2 mm, the branch channel width is 0.8 mm, and the flow channel depth is 1.5 mm (mm).

[0041] In an embodiment of the present application, a first flow field plate 11 with gradient pores based on titanium is produced by laser 3D printing, an iridium oxide catalyst is loaded on the surface, and the first flow channel is a bionic dendritic finger structure. The main channel width of the first flow channel is 2.0 mm, the branch channel width is 0.8 mm, and the depth is 1.5 mm, so that the voltage drop through the first flow channel is reduced by 52% compared with the traditional flow channel.

[0042] In the embodiment of the present application, the second flow field plate 21 is made of graphite carbon felt, and the specific surface area of ​​the second flow field plate 21 is 800 square meters per gram (m² / g). The specific process includes a high-temperature graphitization treatment at 2800°C.

[0043] In an embodiment of the present application, the value of the pitch angle of the second flow channel includes 15 degrees, and the value of the cross-sectional area of ​​the second flow channel includes 2.4 square millimeters. Specifically, the value of the pitch angle of the second flow channel includes 12 degrees, 13 degrees, 14 degrees, 15 degrees, 16 degrees, 17 degrees, and 18 degrees. The value of the cross-sectional area of ​​the second flow channel includes 2.1 square millimeters, 2.2 square millimeters, 2.3 square millimeters, 2.4 square millimeters, 2.5 square millimeters, 2.6 square millimeters, and 2.7 square millimeters. Among them, the value of the pitch angle of the second flow channel and the value of the cross-sectional area of ​​the second flow channel can be arbitrarily combined. Preferably, the pitch angle value of the second flow channel is 15 degrees, and the cross-sectional area value of the second flow channel is 2.4 square millimeters (mm²).

[0044] In the embodiment of the present application, a polyperfluorosulfonic acid-based composite membrane is provided on the surface of the second flow field plate 21. The thickness of the polyperfluorosulfonic acid-based composite membrane ranges from 183 microns. Specifically, the thickness of the polyperfluorosulfonic acid-based composite membrane ranges from 180 microns, 181 microns, 182 microns, 183 microns, 184 microns, 185 microns, and 186 microns. Preferably, the thickness of the polyperfluorosulfonic acid-based composite membrane is 183 microns (μm).

[0045] In the embodiment of the present application, the third flow field plate 31 is a titanium mesh, and the pore size of the titanium mesh includes 10 microns. Specifically, the pore size of the titanium mesh includes 8 microns, 9 microns, 10 microns, 11 microns, and 12 microns. Preferably, the pore size of the titanium mesh is 10 microns.

[0046] In the embodiment of the present application, a catalyst layer composed of platinum (Pt) is provided on the surface of the third flow field plate 31. The catalyst layer has a loading value of 0.5 mg / cm². The catalyst layer loading values ​​include 0.3 mg / cm², 0.4 mg / cm², 0.5 mg / cm², 0.6 mg / cm², and 0.7 mg / cm². Preferably, the catalyst layer loading value is 0.5 mg / cm².

[0047] In an embodiment of the present application, the third flow channel includes a primary flow channel and a secondary flow channel, and the value of the width of the primary flow channel includes 1.5 mm, and the value of the width of the secondary flow channel includes 0.5 mm. Specifically, the value of the width of the primary flow channel includes 1.3 mm, 1.4 mm, 1.5 mm, 1.6 mm, and 1.7 mm. The value of the width of the secondary flow channel includes 0.3 mm, 0.4 mm, 0.5 mm, 0.6 mm, and 0.7 mm. Among them, the values ​​of the width of the above-mentioned primary flow channel and the values ​​of the width of the secondary flow channel can be arbitrarily combined. Preferably, the value of the width of the primary flow channel is 1.5 mm, and the value of the width of the secondary flow channel is 0.5 mm.

[0048] In an embodiment of the present application, the third flow field plate 31 adopts an ultra-thin microporous titanium mesh with a pore size of 10 microns. A platinum catalyst layer is provided on the surface of the titanium mesh, and the platinum loading is 0.5 mg per square centimeter. The third flow channel is a multi-stage fractal interdigitated type, with a first-level flow channel width of 1.5 mm and a second-level flow channel width of 0.5 mm, so that the oxygen mass transfer efficiency of the third flow field plate 31 is increased to 3.8 times that of the traditional carbon paper electrode.

[0049] In the embodiment of the present application, the volume of the vanadium electrolyte storage tank 40 is 5 cubic meters (m³), and the material used for the lining of the vanadium electrolyte storage tank 40 includes fluororubber and / or silicon carbide.

[0050] In the embodiment of the present application, the medium storage module 3 further includes a tank status monitoring unit 33, which includes an ultrasonic concentration sensor, an online redox potential monitoring probe, and a tank status sensor. The ultrasonic concentration sensor and the online redox potential monitoring probe are installed in the vanadium electrolyte storage tank 40, and the tank status sensor is installed in the reaction medium storage tank 50. The tank status sensor is used to monitor the pressure, temperature, and pH value within the reaction medium storage tank 50.

[0051] In the embodiment of the present application, the stack reaction module 1 further includes: an ion exchange unit 60 , a current collector unit 70 and a fixing unit 80 .

[0052] In an embodiment of the present application, the ion exchange unit 60 includes a first ion exchange membrane 61 and a second ion exchange membrane 62. The first ion exchange membrane 61 is arranged between the oxygen evolution reaction flow unit 10 and the vanadium electrolyte flow unit 20, and the second ion exchange membrane 62 is arranged between the vanadium electrolyte flow unit 20 and the oxygen reduction reaction flow unit 30.

[0053] In the embodiment of the present application, the oxygen evolution reaction flow unit 10 further includes a first sealing gasket 12, which is disposed between the first flow field plate 11 and the first ion exchange membrane 61. The vanadium electrolyte flow unit 20 further includes a second sealing gasket 22 and a third sealing gasket 23, wherein the second sealing gasket 22 is disposed between the first ion exchange membrane 61 and the second flow field plate 21, and the third sealing gasket 23 is disposed between the second flow field plate 21 and the second ion exchange membrane 62. The oxygen reduction reaction flow unit 30 further includes a fourth sealing gasket 32, which is disposed between the second ion exchange membrane 62 and the third flow field plate 31.

[0054] In an embodiment of the present application, the current collector unit 70 includes a first copper plate current collector 71 and a second copper plate current collector 72. The first copper plate current collector 71 is arranged on the side of the oxygen evolution reaction flow unit 10 away from the first ion exchange membrane 61, and the second copper plate current collector 72 is arranged on the side of the oxygen reduction reaction flow unit 30 away from the second ion exchange membrane 62.

[0055] In an embodiment of the present application, the fixing unit 80 includes a first end plate 81 and a second end plate 82. The first end plate 81 is arranged on a side of the first copper plate current collector 71 away from the oxygen evolution reaction flow unit 10, and the second end plate 82 is arranged on a side of the second copper plate current collector 72 away from the oxygen reduction reaction flow unit 30.

[0056] In an embodiment of the present application, the electrolyte drive module 2 includes a battery 24, a first pipeline 25 and a second pipeline 26. The first pipeline 25 is used to connect the battery 24 to the stack reaction module 1, and the second pipeline 26 is used to connect the stack reaction module 1 to the medium storage module 3 to charge or discharge the battery 24. Among them, the material used for the second pipeline 26 includes polytetrafluoroethylene. The battery 24 is connected to the first copper plate current collector 71 and the second copper plate current collector 72 through the first pipeline 25. The vanadium electrolyte storage tank 40 is connected to the second flow field plate 21 through the second pipeline 26, and the reaction medium storage tank 50 is connected to the first flow field plate 11 and the third flow field plate 31 respectively through the second pipeline 26.

[0057] In an embodiment of the present application, the fuel cell reaction module 1 is connected to the medium storage module 3 through a polytetrafluoroethylene reinforced pipe, and a magnetic levitation brushless electric pump is used to achieve low-energy directional transportation of the fluid. The entire system is integrated into a portable container, and the interior of the container is equipped with anti-seismic brackets and temperature-controlled interlayers to meet the needs of outdoor mobile deployment.

[0058] like Figure 2 As shown, the reaction medium storage tank 50 stores acidic energy storage fluid medium and high-pressure air medium in stages, and the pH value of the acidic energy storage fluid medium includes 0.5.

[0059] In the embodiment of the present application, an isolation plate 51 is further provided in the reaction medium storage tank 50 . The isolation plate 51 is made of nanomaterials and is used to separate the gaseous medium and the liquid medium in the reaction medium storage tank 50 .

[0060] The mobile vanadium-based electric fuel energy storage and supply system provided in this application has a current density of 80 mA / cm² and a temperature of 25°C. During the charging process, the vanadium electrolyte (1M V 3+ / V 4+ The stack voltage is adjusted from 1.8 V to 2.0 V to achieve a coordinated vanadium ion reduction and oxygen evolution reaction. During discharge, the ORR medium (80% O2 + 20% N2) reacts with the reduced vanadium electrolyte within the stack, achieving a system energy conversion efficiency of 91.2%.

[0061] The following non-limiting embodiments may enable a person skilled in the art to more fully understand the present application, but do not limit the present application in any way.

[0062] Example 1: Constant voltage charging of a new mobile vanadium-based electric fuel energy storage system

[0063] This example conducts a constant voltage charging performance test under standard test conditions (25°C, normal pressure). The configuration parameters are as follows:

[0064] Vanadium electrolyte: 1.0 MV 3+ / V 4+ 3.0 M H2SO4 solution at a flow rate of 40 mL / min;

[0065] OER medium: 1.0 H2SO4 solution, flow rate 40 mL / min;

[0066] OER medium flow unit: laser 3D printed gradient pore titanium-based flow field plate (porosity 50-85%, gradient distribution), surface-loaded IrO2 catalyst (loading 2 mg / cm²), flow channel with biomimetic dendritic interdigitated structure (main channel width 2.0 mm, branch channel width 0.8 mm, depth 1.5 mm);

[0067] Vanadium electrolyte flow cell: graphitized carbon felt electrodes (surface area 800 m² / g, graphitized at 2800°C), bidirectional helical interdigitated flow channel design (pitch angle 15°, flow channel cross-sectional area 2.4 mm²), paired with a polyperfluorosulfonic acid composite membrane (thickness 183 μm);

[0068] Current collector unit: 140mm*140mm*1mm copper plate;

[0069] Fixing unit: 140mm*140mm*1mm bakelite;

[0070] Charging voltage: 2.0V, constant voltage charging;

[0071] Electrolyte tank temperature maintenance system: ±0.5℃ accuracy.

[0072] The constant voltage charging curve of the battery is as follows Figure 3 As shown, the maximum charge current density is 120 mA / cm 2 After seven cycles, the charging current density remained at 50 mA / cm 2 .

[0073] Example 2: Constant current discharge of a new mobile vanadium-based electric fuel energy storage system under different current density conditions.

[0074] This example conducts a constant current discharge performance test under standard test conditions (25°C, normal pressure). The configuration parameters are as follows:

[0075] Vanadium electrolyte: 1.0 MV 2+ 3.0 M H2SO4 solution at a flow rate of 60 mL / min;

[0076] ORR medium: high-pressure air (80% O2+20% N2), flow rate 100 sccm;

[0077] ORR medium flow unit: Pt catalyst layer (Pt loading 0.5 mg / cm²) supported by ultra-thin microporous titanium mesh (pore size 10 μm), with a multi-level fractal interdigitated structure (primary channel width 1.5 mm, secondary channel width 0.5 mm);

[0078] Vanadium electrolyte flow cell: graphitized carbon felt electrodes (surface area 800 m² / g, graphitized at 2800°C), bidirectional helical interdigitated flow channel design (pitch angle 15°, flow channel cross-sectional area 2.4 mm²), paired with a polyperfluorosulfonic acid composite membrane (thickness 183 μm);

[0079] Current collector unit: 140mm*140mm*1mm copper plate;

[0080] Fixing unit: 140mm*140mm*1mm bakelite;

[0081] Discharge current: discharge current density 10, 20, 30, 40, 50 mA / cm 2 , constant current discharge;

[0082] Tank pressure maintenance system: ±0.1kPa accuracy.

[0083] Discharge performance curve is as follows Figure 4 As shown, the maximum discharge capacity is 24 Ah L -1 .

[0084] Example 3: Discharge of the new flow-type vanadium-based electric fuel energy storage system battery 24 at different gas flow rates.

[0085] This example tests the polarization performance of an electric fuel energy storage system under standard test conditions (25°C, atmospheric pressure) at different gas flow rates. The configuration parameters are as follows:

[0086] Vanadium electrolyte: 1.0 MV 2+ 3.0 M H2SO4 solution at a flow rate of 40 mL / min;

[0087] ORR medium: high-pressure air (80% O2+20% N2), flow rates of 50, 100, 150, 200, 250, and 300 sccm;

[0088] ORR medium flow unit: Pt catalyst layer (Pt loading 0.5 mg / cm²) supported by ultra-thin microporous titanium mesh (pore size 10 μm), with a multi-level fractal interdigitated structure (primary channel width 1.5 mm, secondary channel width 0.5 mm);

[0089] Vanadium electrolyte flow cell: graphitized carbon felt electrodes (surface area 800 m² / g, graphitized at 2800°C), bidirectional helical interdigitated flow channel design (pitch angle 15°, flow channel cross-sectional area 2.4 mm²), paired with a polyperfluorosulfonic acid composite membrane (thickness 183 μm);

[0090] Current collector unit: 140mm*140mm*1mm copper plate;

[0091] Fixing unit: 140mm*140mm*1mm bakelite;

[0092] Discharge current: 50, 100, 150, 200, 250, 300 mA / cm 2 , gradient discharge;

[0093] Tank pressure maintenance system: ±0.1kPa accuracy.

[0094] Discharge performance curve is as follows Figure 5 As shown, under the flow rate of 50 sccm, the embodiment shows a peak power density of 68 mW / cm -2 .

[0095] Example 4: Discharge of a new flowable vanadium-based electric fuel energy storage system at different vanadium electrolyte flow rates.

[0096] This example tests the polarization performance of an electric fuel energy storage system under standard test conditions (25°C, atmospheric pressure) at different gas flow rates. The configuration parameters are as follows:

[0097] Vanadium electrolyte: 1.0 MV 2+ 3.0 M H2SO4 solution at flow rates of 5, 10, 20, 40, 60, and 80 mL / min;

[0098] ORR medium: high-pressure air (80% O2+20% N2), flow rates of 50, 100, 150, 200, 250, and 300 sccm;

[0099] ORR medium flow unit: Pt catalyst layer (Pt loading 0.5 mg / cm²) supported by ultra-thin microporous titanium mesh (pore size 10 μm), with a multi-level fractal interdigitated structure (primary channel width 1.5 mm, secondary channel width 0.5 mm);

[0100] Vanadium electrolyte flow cell: graphitized carbon felt electrodes (surface area 800 m² / g, graphitized at 2800°C), bidirectional helical interdigitated flow channel design (pitch angle 15°, flow channel cross-sectional area 2.4 mm²), paired with a polyperfluorosulfonic acid composite membrane (thickness 183 μm);

[0101] Current collector unit: 140mm*140mm*1mm copper plate;

[0102] Fixing unit: 140mm*140mm*1mm bakelite;

[0103] Discharge current: 50, 100, 150, 200, 250, 300 mA / cm 2 , gradient discharge;

[0104] Tank pressure maintenance system: ±0.1kPa accuracy.

[0105] Discharge performance curve is as follows Figure 6 As shown, 40 mL / min -1 Under the flow rate conditions, the peak power density of the embodiment is 110.5mW / cm -2 .

[0106] Example 5: Discharge of a new flowable vanadium-based electric fuel energy storage system at different operating temperatures.

[0107] This example tests the polarization performance of an electric fuel energy storage system under standard test conditions (normal pressure) at different gas flow rates. The configuration parameters are as follows:

[0108] Vanadium electrolyte: 1.0 MV 2+ 3.0 M H2SO4 solution at a flow rate of 40 mL / min;

[0109] ORR medium: high-pressure air (80% O2+20% N2), flow rate 100 sccm;

[0110] ORR medium flow unit: Pt catalyst layer (Pt loading 0.5 mg / cm²) supported by ultra-thin microporous titanium mesh (pore size 10 μm), with a multi-level fractal interdigitated structure (primary channel width 1.5 mm, secondary channel width 0.5 mm);

[0111] Vanadium electrolyte flow cell: graphitized carbon felt electrodes (surface area 800 m² / g, graphitized at 2800°C), bidirectional helical interdigitated flow channel design (pitch angle 15°, flow channel cross-sectional area 2.4 mm²), paired with a polyperfluorosulfonic acid composite membrane (thickness 183 μm);

[0112] Current collector unit: 140mm*140mm*1mm copper plate;

[0113] Fixing unit: 140mm*140mm*1mm bakelite;

[0114] Discharge current: 50, 100, 150, 200, 250, 300 mA / cm 2 , gradient discharge;

[0115] Tank pressure maintenance system: ±0.1kPa accuracy.

[0116] Working temperature: 23℃ (room temperature), 40℃, 50℃, 60℃.

[0117] Discharge performance curve is as follows Figure 7 As shown, under 40°C, the peak power density of the embodiment is 80 mW / cm-2 .

[0118] Compared with the existing technology, the mobile vanadium-based electric fuel energy storage and supply system provided by this application has the following beneficial effects:

[0119] 1. Integrated design breaks through the limitations of traditional architecture:

[0120] By adopting an integrated charge-discharge stack reaction module, the two independent battery packs required for traditional vanadium-air batteries are integrated into a single functional module, reducing the number of system components by 40% and the volume by 35%. Furthermore, through the multiphase fluid coordinated control technology of interdigitated flow field plates, efficient coupling of oxygen evolution (OER) and oxygen reduction (ORR) reactions is achieved, increasing the power density to 1.8 times that of traditional structures while reducing manufacturing costs by 50%. This achieves a higher level of integration of the energy storage and power supply system while reducing costs, making it suitable for application in the field of mobile energy storage.

[0121] 2. Wide range of working conditions adaptability and application scalability:

[0122] The system maintains stable operation over a wide temperature range from room temperature to 60°C (capacity fluctuation <5%) and supports dynamic adjustment of 80-120% of rated power (response time <200 ms). It is particularly suitable for:

[0123] • Mobile energy storage: integrated portable container (40 feet in size) to support vehicle-mounted deployment and rapid replacement.

[0124] • Grid-level frequency regulation: with millisecond-level power response capability and a frequency regulation accuracy of 99.3%.

[0125] • Off-grid power supply system: By connecting multiple tanks in parallel, the energy storage capacity can be expanded to 200 MWh.

[0126] 3. Intrinsic safety and environmental protection characteristics:

[0127] The system utilizes a fully acidic aqueous electrolyte system (pH = 0.5), eliminating the risk of organic solvent explosion. Based on the vanadium ion valence state conversion mechanism, the system generates no byproducts during the cycle, achieving an electrolyte recovery rate exceeding 99.5%. A supporting intelligent thermal runaway warning system initiates an emergency shutdown within 0.5 seconds in the event of abnormal temperatures (>65°C) or sudden pressure changes (>10 kPa / s), achieving a threefold increase in safety compared to traditional systems.

[0128] 4. Significant economic benefits:

[0129] By reducing the number of storage tanks and optimizing material costs, the system's unit energy storage cost is 50% lower than that of traditional vanadium-air batteries. Furthermore, the system supports online electrolyte regeneration. In a 100 MW / 400 MWh energy storage plant scenario, the lifetime cost per kilowatt-hour can be controlled at $0.045 / kWh, shortening the payback period to 5.2 years.

[0130] The above is a detailed introduction to a flow-type vanadium-based electric fuel energy storage and supply system input in the embodiment of this application. The description of the above embodiment is only used to help understand the core idea of ​​this application, and the above description should not be understood as limiting the scope of protection of this application.

Claims

1. A mobile vanadium-based electric fuel energy storage and supply system, characterized in that: include: A stack reaction module, an electrolyte driving module and a medium storage module, wherein the electrolyte driving module is used to connect and drive the stack reaction module and the medium storage module to realize charging or discharging of the energy storage and supply system; The stack reaction module includes an oxygen evolution reaction flow unit, a vanadium electrolyte flow unit and an oxygen reduction reaction flow unit arranged adjacent to each other; The oxygen evolution reaction flow unit comprises a first flow field plate, on which a first flow channel is provided, and the first flow channel is a bionic dendritic interdigitated type; The vanadium electrolyte flow unit includes a second flow field plate, the second flow field plate is provided with a second flow channel, and the second flow channel is a bidirectional spiral interdigital type; The oxygen reduction reaction flow unit includes a third flow field plate, a third flow channel is provided on the second flow field plate, and the third flow channel is a multi-stage fractal interdigitated type; The medium storage module includes a vanadium electrolyte storage tank and a reaction medium storage tank, which are arranged on opposite sides of the stack reaction module. The vanadium electrolyte storage tank is connected to the second flow field plate, and the reaction medium storage tank is connected to the first flow field plate and the third flow field plate respectively.

2. The mobile vanadium-based electric fuel energy storage and supply system according to claim 1 is characterized in that: The first flow field plate is a gradient pore structure made of titanium alloy material by laser three-dimensional printing, and the gradient porosity of the first flow field plate is between 50% and 85%.

3. The mobile vanadium-based electric fuel energy storage and supply system according to claim 1 or 2, characterized in that: A catalyst layer formed of iridium oxide is provided on the surface of the first flow field plate, and the loading of the catalyst layer is between 1.5 mg / cm2 and 2.5 mg / cm2.

4. The mobile vanadium-based electric fuel energy storage and supply system according to claim 3 is characterized in that: The main channel width of the first flow channel may be 2 mm, the branch channel width may be 0.8 mm, and the flow channel depth may be 1.5 mm.

5. The mobile vanadium-based electric fuel energy storage and supply system according to claim 1, characterized in that: The second flow field plate is made of graphite carbon felt, and the specific surface area of ​​the second flow field plate is 800 square meters per gram.

6. The mobile vanadium-based electric fuel energy storage and supply system according to claim 1 or 5, characterized in that: The pitch angle of the second flow channel is 15 degrees, and the cross-sectional area of ​​the second flow channel is 2.4 square millimeters.

7. The mobile vanadium-based electric fuel energy storage and supply system according to claim 6, characterized in that: A polyperfluorosulfonic acid-based composite membrane is provided on the surface of the second flow field plate, and the thickness of the polyperfluorosulfonic acid-based composite membrane ranges from 183 microns.

8. The mobile vanadium-based electric fuel energy storage and supply system according to claim 1, characterized in that: The third flow field plate is a titanium mesh, and the pore size of the titanium mesh is within the range of 10 microns.

9. The mobile vanadium-based electric fuel energy storage and supply system according to claim 1 or 8, characterized in that: A catalyst layer formed of platinum is provided on the surface of the third flow field plate, and a loading value of the catalyst layer includes 0.5 mg / cm2.

10. The mobile vanadium-based electric fuel energy storage and supply system according to claim 9, characterized in that: The third flow channel includes a primary flow channel and a secondary flow channel. The width of the primary flow channel is 1.5 mm, and the width of the secondary flow channel is 0.5 mm.

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