A liquid flow membraneless electrolysis water hydrogen production system

Abstract

The application relates to the technical field of hydrogen production systems, in particular to a liquid flow membrane-free water electrolysis hydrogen production system. The system comprises left and right end plates, left and right insulating plates, anode and cathode current collector plates, anode and cathode electrolysis chambers, anode gas-liquid outlets and one-way structural members. Electrolyte is input into the liquid flow membrane-free water electrolysis hydrogen production system from a liquid inlet, and the upper part is composed of a gas-liquid separation chamber and a hydrogen outlet. The gas-liquid enters the outlet of the gas-liquid separation chamber, is transferred from the gas-liquid separation chamber to the anode electrolysis chamber, and first passes through a one-way flow channel and is transferred to the inlet of the anode electrolysis chamber. In the hydrogen production process, the temperature feedback deviation and the flow rate feedback error at each moment are calculated, and the electrolyte temperature and flow rate are controlled respectively. The application improves the purity of the prepared hydrogen.

Description

Technical Field

[0001] This application relates to the field of hydrogen production system technology, specifically to a liquid flow membraneless water electrolysis hydrogen production system. Background Technology

[0002] Currently, the membrane (proton exchange membrane / anion exchange membrane) electrolysis method, widely used in the field of water electrolysis, faces numerous problems, mainly in the following three aspects: First, the high cost of membranes keeps their commercial application prohibitively expensive, hindering large-scale adoption. Second, the membrane's lifespan is limited, especially under high current density operating conditions, where rapid ion transfer can lead to the formation of fixed channels within the membrane, potentially causing cross-contamination between the two chambers and a possible hydrogen-oxygen mixture explosion, posing a serious safety hazard. Third, the active catalyst material coated on the membrane is prone to pulverization during electrolysis, resulting in rapid performance degradation. These problems severely restrict the large-scale application of water electrolysis for hydrogen production.

[0003] Given the current state of membrane electrode fusion (MEA) water electrolysis technology, large-scale commercialization in the short term faces significant challenges. Therefore, flow electrolysis for hydrogen production has gradually gained attention and application. However, when further applying flow electrolysis for hydrogen production, the stability of the liquid flow is difficult to guarantee due to its membrane-free electrolysis mode. Unstable liquid flow exacerbates gas turbulence, thus affecting hydrogen production efficiency. Furthermore, electrolyte temperature variations also significantly impact hydrogen production efficiency. In actual production, temperature fluctuations can lead to unstable reaction rates, further reducing hydrogen production efficiency. Moreover, gas cross-contamination can decrease hydrogen purity. The combined effect of these factors results in unsatisfactory efficiency and purity in current flow electrolysis for hydrogen production. Summary of the Invention

[0004] To address the aforementioned technical problems, the purpose of this application is to provide a liquid flow membrane-free water electrolysis hydrogen production system, the specific technical solution of which is as follows:

[0005] This application proposes a liquid flow membraneless water electrolysis hydrogen production system, the system comprising:

[0006] The liquid flow membraneless electrolysis water production hydrogen production data acquisition module acquires the temperature of each acquisition point of the input electrolyte during the hydrogen production process, and acquires the pressure and flow rate of each acquisition point during the electrolyte transportation process, and constructs the row vectors of the temperature matrix, pressure matrix, and flow rate matrix respectively;

[0007] The liquid flow membraneless electrolysis water hydrogen production temperature control module uses the sum of the temperatures at all sampling locations at each time point as each element of the temperature monitoring sequence. Through the linear relationship between the temperature monitoring sequence and each row vector in the temperature matrix, the variance expansion factor of each data point in the temperature matrix is ​​calculated to obtain the real-time monitoring weight of each data point in the temperature matrix. Based on the real-time monitoring weight of each row vector at the previous time point and the deviation between the temperature at each sampling location and the preset electrolyte temperature, the temperature feedback deviation at each time point is obtained. The electrolyte temperature in the liquid flow membraneless electrolysis water hydrogen production process is controlled by the negative feedback controller.

[0008] The flow rate control module for liquid flow membrane-free water electrolysis hydrogen production analyzes the differences in real-time monitoring weights between the flow rate matrix and the pressure and temperature matrices at the same positions, obtains the cumulative monitoring response value of each data point in the flow rate matrix, processes it to obtain the updated real-time monitoring weights of each data point in the flow rate matrix, calculates the flow rate feedback error at each time moment, and uses a negative feedback controller to regulate the electrolyte flow rate in the liquid flow membrane-free water electrolysis hydrogen production process.

[0009] Preferably, it also includes: a left end plate 1, a left insulating plate 2, an anode current collector 3, an anode electrolysis chamber 4, an anode gas-liquid outlet 5, and a unidirectional structural component 6; a right end plate 7, a right insulating plate 8, a cathode current collector 10, and a cathode electrolysis chamber 11; the electrolyte is input into the liquid flow membraneless electrolysis water hydrogen production system from the liquid inlet 12, and the upper part consists of a gas-liquid separation chamber 13 and a hydrogen outlet 14; the plates are fixed together with screws and nuts 9.

[0010] Preferably, the unidirectional structural component 6 and the gas-liquid separation chamber 13 are on the same main body. The gas and liquid enter the outlet 15 of the gas-liquid separation chamber 13 and transfer from the gas-liquid separation chamber 13 to the anode electrolysis chamber 4. They first pass through the unidirectional flow channel 16 and then transfer to the inlet 17 of the anode electrolysis chamber 4. Both the cathode current collector 10 and the anode current collector 3 contain electrodes 18. The gas-liquid mixture after the electrocatalytic hydrogen evolution reaction is completed is discharged to the inlet 19 of the cathode electrolysis chamber 11. 20 and 21 are positioning holes.

[0011] Preferably, the outlet 15 of the gas-liquid separation chamber 13 is higher than the inlet 17 of the electrolyte entering the anolyte chamber 4, and the outlet 15 of the gas-liquid separation chamber 13 is in the opposite direction to the inlet 17 of the electrolyte entering the anolyte chamber 4.

[0012] Preferably, the temperature, pressure, and flow rate at each acquisition location at all times are used as row vectors of the temperature matrix, pressure matrix, and flow rate matrix, respectively.

[0013] Preferably, the temperature feedback deviation at each time point is:

[0014] Where, δ i T represents the temperature feedback deviation at time i. i-1,xThe value represents the temperature at time i-1 in the x-th row vector of the temperature matrix, where T represents the preset electrolyte temperature, and ω represents the temperature at time i-1. i-1,x This represents the real-time monitoring weight of the data point corresponding to the x-th row vector at time i-1 in the temperature matrix, where n is the number of row vectors.

[0015] Preferably, the cumulative monitoring response value for each data point in the velocity matrix is:

[0016] l i,v =a i,v +b i,v , where l i,v a is the cumulative monitoring response value of the data point corresponding to the v-th position at the i-th time in the velocity matrix; i,v b represents the mean of all velocity-pressure monitoring differences obtained up to the i-th time point based on the v-th position of the velocity and pressure matrices. i,v This represents the average of all velocity-temperature monitoring differences obtained up to the i-th time point based on the v-th position of the velocity and temperature matrices.

[0017] Preferably, the difference between the real-time monitoring weights of the flow velocity matrix and the corresponding data points at the same location in the pressure matrix and temperature matrix is ​​calculated, and the difference is used as the flow velocity-pressure monitoring difference and flow velocity-temperature monitoring difference at the same location, respectively. The real-time monitoring weights of each data point in the pressure matrix and temperature matrix are obtained by using the method of obtaining the real-time monitoring weights of each data point in the temperature matrix.

[0018] Preferably, the updated real-time monitoring weights of each data point in the velocity matrix are the result of normalizing the cumulative monitoring response values ​​of each data point in the velocity matrix.

[0019] Preferably, the calculation process for the flow velocity feedback error at each time point is as follows:

[0020] Among them, LS i V represents the flow velocity feedback deviation at time i. i-1,x ω′ represents the flow velocity at time i-1 in the x-th row vector of the flow velocity matrix, V represents the preset electrolyte flow velocity, and ω′ represents the flow velocity at time i-1. i-1,x This represents the real-time monitoring weight of the data point corresponding to the x-th row vector at time i-1 in the velocity matrix after the update, where n is the number of row vectors.

[0021] This application has the following beneficial effects:

[0022] This application's liquid flow membrane-free electrolysis water production system enables hydrogen production through water electrolysis in a low-energy, low-cost manner. Addressing the issue that the membrane-free electrolysis mode can lead to unstable liquid flow during hydrogen production, exacerbating gas turbulence and affecting efficiency, and that electrolyte temperature significantly impacts efficiency, this application employs precise and stable control of electrolyte temperature and flow rate to ensure the stability of the membrane-free electrolysis process. Furthermore, the anode and cathode chambers of this hydrogen production system are structurally separated, effectively preventing cross-contamination of gases and thus improving the purity of the produced hydrogen. Attached Figure Description

[0023] To more clearly illustrate the technical solutions and advantages in the embodiments of this application 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 application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0024] Figure 1 A block diagram of a liquid flow membraneless water electrolysis hydrogen production system provided in this application;

[0025] Figure 2 A schematic diagram of the liquid flow membraneless electrolysis water production hydrogen production system provided in this application;

[0026] Figure 3 A schematic diagram of the liquid flow membraneless water electrolysis hydrogen production system provided in this application;

[0027] Figure 4 A cross-sectional view of the unidirectional structural component 6 in the liquid flow membraneless electrolysis water hydrogen production system provided in this application;

[0028] Figure 5 A schematic diagram of voltage decay in the liquid flow membraneless electrolysis water production hydrogen production system provided in this application;

[0029] Figure 6 A schematic diagram illustrating the electrolysis efficiency of the liquid flow membraneless electrolysis water production hydrogen production system provided in this application. Detailed Implementation

[0030] To further illustrate the technical means and effects adopted by this application to achieve the intended purpose of the invention, the following, in conjunction with the accompanying drawings and preferred embodiments, details the specific implementation, structure, features, and effects of a liquid flow membraneless electrolysis water production system proposed in this application. In the following description, different "one embodiment" or "another embodiment" do not necessarily refer to the same embodiment. Furthermore, specific features, structures, or characteristics in one or more embodiments can be combined in any suitable form.

[0031] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application pertains.

[0032] The following description, in conjunction with the accompanying drawings, details a specific scheme for a liquid flow membraneless electrolysis water hydrogen production system provided in this application.

[0033] Please see Figure 1 The diagram illustrates a block diagram of a liquid flow membrane-free water electrolysis hydrogen production system according to an embodiment of this application. The system includes:

[0034] First, in this embodiment, the water electrolysis hydrogen production system is a cuboid-shaped device, specifically as follows: Figure 2 As shown in the figure. In this embodiment, a schematic diagram of the specific liquid flow membrane-free water electrolysis hydrogen production system is shown below. Figure 3 As shown, Figure 3 The anode side includes: a left end plate 1, a left insulating plate 2, an anode current collector 3, an anode electrolysis chamber 4, an anode gas-liquid outlet 5, and a unidirectional structural component 6; the cathode side includes: a right end plate 7, a right insulating plate 8, a cathode current collector 10, and a cathode electrolysis chamber 11; the electrolyte is input from the liquid inlet 12 to the liquid flow membraneless water electrolysis hydrogen production system, and the upper part of the system consists of a gas-liquid separation chamber 13 and a hydrogen outlet 14; the plates are fixed together with eight pairs of screws and nuts 9.

[0035] A cross-sectional view of unidirectional structural component 6 in a liquid flow membrane-free water electrolysis hydrogen production system is shown below. Figure 4 As shown, Figure 4 In this configuration, the unidirectional structural component 6 and the gas-liquid separation chamber 13 are on the same main body. Gas and liquid enter through the outlet 15 of the gas-liquid separation chamber 13 and transfer from the gas-liquid separation chamber 13 to the anode electrolysis chamber 4, first passing through the unidirectional flow channel 16 and then through the inlet 17 of the anode electrolysis chamber 4. Both the cathode current collector 10 and the anode current collector 3 contain electrodes 18 for applying voltage to the electrolysis system. The gas-liquid mixture after the HER reaction is completed exits through the inlet 19 of the cathode electrolysis chamber 11. It should be noted that the inlet 19 of the cathode electrolysis chamber 11 is located closer to the cathode current collector 10, while the inlet 17 of the anode electrolysis chamber 4 is located closer to the anode current collector 3. Holes 20 and 21 are positioning holes used to accurately fix the positions of the plates.

[0036] In the liquid flow membrane-free water electrolysis hydrogen production system, from left to right, a left insulating plate 2, an anode current collector 3, a unidirectional structural layer, a cathode current collector 10, and a right insulating plate 8 are arranged between the right end plate 7 and the left end plate 1. A first sealing ring is arranged between the left insulating plate 2 and the left end plate 1, and a second sealing ring is arranged between the left insulating plate 2 and the anode current collector 3. Both the first and second sealing rings are used to ensure a seal when the electrolyte and oxygen are discharged from the anode electrolysis chamber 4. A third sealing ring is arranged between the anode current collector and the unidirectional structural component 6, forming the anode electrolysis chamber 4. A fourth sealing ring is arranged between the unidirectional structural component 6 and the cathode current collector, forming the cathode electrolysis chamber 11. A fifth sealing ring is provided between the cathode current collector 10 and the right insulating plate 8, and a sixth sealing ring is provided between the right end plate 7 and the right insulating plate 8. Both the fifth and sixth sealing rings are used to ensure that the electrolyte enters the cathode electrolysis chamber 11 and achieves a seal.

[0037] Furthermore, to facilitate the energization of the electrolytic hydrogen production system, an anode lug with a "+" symbol is provided extending outward from the side wall of the anode current collector 3, and a cathode lug with a "-" symbol is provided extending outward from the side wall of the cathode current collector 10.

[0038] In this embodiment, the outlet for hydrogen and electrolyte in the unidirectional structural component 6 is located at the upper end of the electrolytic active material and connected to the gas-liquid separation chamber 13. To prevent hydrogen from entering the anode electrolysis chamber 4 due to the flow of electrolyte, the outlet 15 of the hydrogen and electrolyte in the gas-liquid separation chamber 13 is higher than the inlet of the electrolyte into the anode electrolysis chamber 4, thus achieving a liquid seal in the gas-liquid separation chamber 13. Furthermore, to prevent hydrogen from entering the inlet 17 of the anode electrolysis chamber 4 under the adhesive force of water, the outlet 15 of the hydrogen and electrolyte in the gas-liquid separation chamber 13 is in the opposite direction to the inlet 17 of the electrolyte into the anode electrolysis chamber 4, ensuring that the amount of hydrogen mixed in the electrolyte is minimized.

[0039] In the water electrolysis hydrogen production system of this embodiment, the electrolyte temperature and flow rate are stabilized during the hydrogen production process by controlling the electrolyte temperature and flow rate, thus avoiding poor gas stability and large temperature deviations during the hydrogen production process. The unidirectional structural component 6 is mainly derived from the Tesla valve structure. In the water electrolysis hydrogen production system, the unidirectional structural component 6 has two main functions: firstly, it connects the anode and cathode electrolysis chambers 4, allowing ion transfer; secondly, it prevents oxygen generated by anodic electrolysis from entering the cathode reaction chamber, thus preventing a decrease in hydrogen purity. After the electrolyte undergoes the HER (electrocatalytic hydrogen evolution reaction), the generated OH... – It will be transferred to the anode reaction chamber along with the flow of electrolyte, and then the OER (oxygen evolution reaction) reaction will occur. Therefore, the system is called a liquid flow membraneless electrolysis water production hydrogen production system.

[0040] Specifically, the cathode catalyst platinum is electroplated onto the reaction zone of the cathode current collector 10, and the anode catalyst iridium oxide is fixed to the reaction zone of the anode current collector 3 by electroplating and sintering. In this embodiment, a 1 mol / L sodium hydroxide solution is used as the electrolyte at a temperature of 80°C. Before the electrolyte is fed into the water electrolysis hydrogen production system, it needs to be heated and cooled to maintain the electrolyte temperature at 80°C. This can be achieved through a heating device and a cooling device, where the heating device is an electric heater and the cooling device is a cooling pipe. During the process of supplying the electrolyte to the liquid flow membraneless water electrolysis hydrogen production system, the electrolyte temperature is collected in real time and controlled in real time to maintain the electrolyte temperature at 80°C. It should be noted that in this embodiment, the temperature and flow rate of the electrolyte are controlled to avoid low reaction stability during the liquid flow membraneless water electrolysis hydrogen production process, which could lead to a decrease in the stability of the hydrogen production system and affect the hydrogen production yield.

[0041] In this embodiment, the liquid flow membraneless water electrolysis hydrogen production system mainly includes the following modules, specifically:

[0042] The liquid flow membraneless electrolysis water production hydrogen production data acquisition module acquires the temperature of each acquisition point of the input electrolyte during the hydrogen production process, and acquires the pressure and flow rate of each acquisition point during the electrolyte transportation process, and constructs the row vectors of the temperature matrix, pressure matrix, and flow rate matrix respectively.

[0043] Firstly, in this embodiment, a temperature control module is used to precisely regulate the temperature of the electrolyte. Specifically, a temperature sensor is used to collect the temperature of the electrolyte input during the hydrogen production process in real time. Since the membrane-free water electrolysis hydrogen production process is susceptible to environmental interference, the actual delivered electrolyte temperature may vary to varying degrees. Therefore, in this embodiment, temperature sensors are evenly distributed along the path from the electrolyte storage device to the inlet of the water electrolysis hydrogen production system.

[0044] A temperature matrix is ​​constructed using the temperatures collected by all temperature sensors. In this embodiment, the temperatures from each temperature sensor at all times are arranged in ascending order to form row vectors. The row vectors corresponding to all temperature sensors constitute the temperature matrix. Each column of the temperature matrix corresponds to the real-time temperature collected by all temperature sensors at each time point between the electrolyte storage device and the inlet of the water electrolysis hydrogen production system. The purpose of constructing the temperature matrix in this embodiment is to comprehensively consider the temperature changes caused by various environmental disturbances during electrolyte transport in the hydrogen production process, thereby accurately analyzing the deviations generated during control and providing a basis for subsequent precise temperature control.

[0045] In this embodiment, a flow rate control module is used to control the flow rate of the electrolyte. Therefore, the pressure and flow rate during the electrolyte delivery process are collected, and the pressure and flow rate during the electrolyte delivery process are collected in real time through pressure sensors and flow rate sensors.

[0046] Specifically, in order to further analyze the correlation between the interference at different locations and the parameter changes during the actual delivery of the electrolyte, in this embodiment, the acquisition locations of the pressure sensor, flow rate sensor and temperature sensor were uniformly set, that is, the number of pressure sensor, flow rate sensor and temperature sensor is the same and they are all evenly distributed along the path between the electrolyte storage device and the inlet of the water electrolysis hydrogen production system.

[0047] It should be noted that, for the pressure and flow rate collected in real time at each sampling location during the electrolyte delivery process, the pressure matrix and flow rate matrix are obtained accordingly, based on the construction method of the temperature matrix described above. All three matrices have the same dimensions.

[0048] The liquid flow membraneless electrolysis water production hydrogen production temperature control module uses the sum of the temperatures at all sampling locations at each time point as the elements of the temperature monitoring sequence. Through the linear relationship between the temperature monitoring sequence and each row vector in the temperature matrix, the variance amplification factor of each data point in the temperature matrix is ​​calculated to obtain the real-time monitoring weight of each data point in the temperature matrix. Based on the real-time monitoring weight of each row vector at the previous time point and the deviation between the temperature at each sampling location and the preset electrolyte temperature, the temperature feedback deviation at each time point is obtained. The electrolyte temperature is then controlled by a negative feedback controller.

[0049] Specifically, this embodiment performs feedback control deviation analysis on the electrolyte temperature based on the temperature matrix during the electrolyte delivery process. The temperature matrix is ​​used as input data and mapped in the vertical direction to obtain a vertically mapped temperature monitoring sequence. Each element in the temperature monitoring sequence corresponds to the sum of the temperatures collected by all temperature sensors at each time point.

[0050] Under normal circumstances, the temperature of the electrolyte at different locations during transportation should remain consistent, and the temperature change trend at all monitoring locations should be synchronized with the overall temperature change trend of the electrolyte. Based on this, a linear regression equation is constructed using the mapping relationship between the vertically mapped temperature monitoring sequence and each row vector in the temperature matrix, and then the variance magnification factor for each data point in the temperature matrix is ​​calculated. It should be noted that each data point in the temperature matrix corresponds to a temperature. For ease of understanding and description, this embodiment describes the elements in the matrix by data points. Specifically, each data point in the temperature matrix corresponds to a temperature, each data point in the pressure matrix corresponds to a pressure, and each data point in the flow rate matrix corresponds to a flow rate. The larger the variance magnification factor, the more pronounced the collinearity of temperature changes at different locations as they follow changes in electrolyte temperature. It should be noted that constructing the linear regression equation and calculating the variance magnification factor based on the mapping relationship between the temperature monitoring sequence and the temperature data within different row vectors in the temperature matrix is ​​a well-known technical process and will not be elaborated upon here.

[0051] Furthermore, the variance magnification factor calculated for each data point within the temperature matrix is ​​used as input, and normalization is performed using the Softmax function. The result of the normalization is then used as the real-time monitoring weight ω corresponding to each data point within the temperature matrix. Therefore, weighted feedback is achieved through linear comparison of temperatures at different locations during the electrolyte delivery process, thereby realizing precise control of the electrolyte temperature. The specific formula for calculating the temperature feedback deviation is as follows:

[0052] Where, δ i T represents the temperature feedback deviation at time i. i-1,x This represents the temperature at the (i-1)th time in the x-th row vector of the temperature matrix, where T represents the preset electrolyte temperature, which is set to 80℃ in this embodiment; ω i-1,x This represents the real-time monitoring weight of the data point corresponding to the x-th row vector at time i-1 in the temperature matrix, where n is the number of row vectors.

[0053] As described above, the calculated temperature feedback deviation at each moment is input into the negative feedback controller to control the electrolyte temperature. The control process includes: the negative feedback controller stabilizing the temperature based on the temperature feedback deviation, thereby precisely maintaining the electrolyte temperature at 80°C. It should be noted that, specifically, the negative feedback controller in this embodiment is a proportional-integral controller, and its initial control parameters are obtained using the decay curve method. The specific control process is a well-known existing technology and will not be elaborated upon in this embodiment.

[0054] The flow rate control module for liquid flow membrane-free water electrolysis hydrogen production analyzes the differences in real-time monitoring weights between the flow rate matrix and the pressure and temperature matrices at the same positions, obtains the cumulative monitoring response value of each data point in the flow rate matrix, processes it to obtain the updated real-time monitoring weights of each data point in the flow rate matrix, calculates the flow rate feedback error at each time moment, and uses a negative feedback controller to regulate the electrolyte flow rate in the liquid flow membrane-free water electrolysis hydrogen production process.

[0055] Furthermore, the temperature-controlled electrolyte is transported to a water electrolysis hydrogen production system for hydrogen production, specifically as follows: Figure 2 As shown, the electrolyte is fed into the water electrolysis hydrogen production system through inlet 12. In the ideal membrane-free mode, the liquid flows smoothly, avoiding turbulence. However, in the membrane-free electrolysis device, since there is no diaphragm between the positive and negative electrodes, the turbulent liquid flow will aggravate the instability of gas generation during the reaction process. Therefore, in this embodiment, the flow rate is stably controlled by a flow rate control module.

[0056] Based on the above process, correspondingly, for the pressure matrix and the flow velocity matrix, the real-time monitoring weights of each data point in the pressure matrix and the flow velocity matrix are calculated according to the method of obtaining the real-time monitoring weights of each data point in the temperature matrix.

[0057] Furthermore, the stability of electrolyte flow rate is affected by the cumulative changes of factors at different locations. Therefore, it is necessary to comprehensively consider the changes in parameters at different locations, conduct a consistency comparison analysis of the impact of flow rate changes at different locations, update the real-time monitoring weights, and then more accurately analyze the changing patterns and interrelationships of various parameters during electrolyte delivery.

[0058] Specifically, the differences in real-time monitoring weights between the velocity matrix and the pressure and temperature matrices are calculated. The calculation method is as follows: calculate the difference between the real-time monitoring weights of the velocity matrix and the pressure and temperature matrices for corresponding data points at the same location, and use these differences as the velocity-pressure monitoring difference 'a' and the velocity-temperature monitoring difference 'b' at the same location, respectively. Based on the above calculations, the cumulative monitoring response values ​​at different locations during the velocity monitoring process are obtained. The specific calculation formula is: l i,v =a i,v +b i,v , where l i,v a is the cumulative monitoring response value of the data point corresponding to the v-th position at the i-th time in the velocity matrix; i,v b represents the mean of all velocity-pressure monitoring differences obtained up to the i-th time point based on the v-th position of the velocity and pressure matrices. i,vThis represents the average of all flow rate-temperature monitoring differences obtained up to the i-th time based on the v-th position of the flow rate matrix and temperature matrix. The larger the calculated cumulative monitoring response value, the greater the consistency variation between different parameter data at the same position during the overall electrolyte delivery process, and the greater the confidence level of its cumulative flow rate deviation.

[0059] Therefore, further, the Softmax function is used to obtain the normalized result of each monitoring cumulative response value, and the normalized result is used as the updated real-time monitoring weight of each data point in the velocity matrix; then, based on the updated real-time monitoring weight, the velocity feedback error at each moment during electrolyte delivery is calculated. Specifically, according to the updated real-time monitoring weight of each data point in the velocity matrix, the calculation method for temperature feedback deviation at each moment is adopted, and correspondingly, the velocity feedback error at each moment is calculated. For ease of understanding, preferably, the corresponding calculation formula is given in this embodiment:

[0060] Among them, LS i V represents the flow velocity feedback deviation at time i. i-1,x ω′ represents the flow rate at the (i-1)th time in the x-th row vector of the flow rate matrix, and V represents the preset electrolyte flow rate, which is set to 1.3 L / min in this embodiment; i-1,x This represents the real-time monitoring weight of the data point corresponding to the x-th row vector at time i-1 in the velocity matrix after the update, where n is the number of row vectors.

[0061] The flow rate is controlled by feedback based on the error to maintain a stable flow rate during electrolyte delivery. The feedback control process involves the negative feedback controller adjusting the flow rate in real time based on the received flow rate feedback error. It should be noted that the negative feedback controller used in this embodiment is a proportional-integral controller, and the initial control parameters are obtained using the decay curve method. The specific control process is a well-known existing technology and will not be described further in this embodiment.

[0062] Furthermore, after the electrolyte is delivered to the water electrolysis hydrogen production system, a hydrogen evolution reaction occurs at the cathode, with the following equation: 2H₂O + 2e⁻ = H₂ + 2OH⁻ – The hydroxide ions and hydrogen generated in the reaction are transported along with the electrolyte into the gas-liquid separation chamber 13. In the gas-liquid separation chamber 13, after gas-liquid separation, the liquid enters a one-way flow channel, and the hydrogen exits the gas-liquid separation chamber 13 from the hydrogen outlet 14. This ensures the continuity of the electrolyte in the electrolysis system. The hydroxide ions and electrolyte that have passed through the gas-liquid separation chamber 13 flow out of the one-way flow channel and enter the anode electrolysis chamber 4. The presence of the one-way flow channel ensures that the reactants and products in the anode electrolysis chamber 4 do not enter the gas-liquid separation chamber 13, thus preventing a decrease in hydrogen purity. The hydroxide ions entering the anode electrolysis chamber 4 undergo an oxygen evolution reaction, with the reaction formula: 4OH⁻. ––4e = O2 + 2H2O, and the generated oxygen flows out of the electrolysis system from the anode gas-liquid outlet 5 along with the electrolyte. Based on the above two electrolysis reaction equations, it can be seen that the electrolysis process occurs in two independent reaction chambers, and hydroxide ions are transferred along with the liquid flow.

[0063] It should be noted that the specific processes of the hydrogen evolution reaction and oxygen evolution reaction described above are existing well-known technologies, and this embodiment does not impose any special restrictions on them, nor will it be described in detail.

[0064] A schematic diagram of voltage decay in a liquid flow membrane-free water electrolysis hydrogen production system is shown below. Figure 5 As shown, the horizontal axis represents time (in hours), and the vertical axis represents voltage (in voltages, in volts), illustrating the electrolysis efficiency of a liquid flow membrane-free water electrolysis hydrogen production system. Figure 6 As shown, the horizontal axis represents time in hours (h), and the vertical axis represents efficiency. Figure 5 and Figure 6 It can be seen that the total water splitting reaction is at 1 A / cm 2 At this current density, only a 1.42V operating voltage is required, achieving an electrolysis efficiency of 87.6%. Compared to the 1.8V–2.0V required for most existing water splitting systems, this significantly reduces energy consumption. Furthermore, after more than 250 hours of testing, the water electrolysis system showed no significant performance degradation, demonstrating its excellent stability.

[0065] It should be noted that the order of the embodiments described above is merely for descriptive purposes and does not represent the superiority or inferiority of the embodiments. The processes depicted in the accompanying drawings do not necessarily require a specific or sequential order to achieve the desired result. In some embodiments, multitasking and parallel processing are also possible or may be advantageous.

[0066] The various embodiments in this specification are described in a progressive manner. The same or similar parts between the various embodiments can be referred to each other. Each embodiment focuses on describing the differences from other embodiments.

[0067] The above description is only a preferred embodiment of this application and is not intended to limit this application. Any modifications, equivalent substitutions, improvements, etc., made within the principles of this application should be included within the protection scope of this application.

Claims

1. A liquid flow membraneless electrolysis water hydrogen system, characterized in that, The system comprises: The liquid flow membraneless water electrolysis hydrogen production data acquisition module acquires the temperature of each collection position of the input electrolyte in the hydrogen production process, and acquires the pressure and flow rate of each collection position in the electrolyte conveying process, and constructs the row vectors of the temperature matrix, the pressure matrix and the flow rate matrix respectively; The liquid flow membraneless water electrolysis hydrogen production temperature control module takes the accumulation of the temperature of all collection positions at each time as each element of the temperature monitoring sequence, calculates the variance expansion factor of each data point in the temperature matrix through the linear relationship between the temperature monitoring sequence and the row vectors in the temperature matrix, to obtain the real-time monitoring weight of each data point in the temperature matrix, obtains the temperature feedback deviation at each time according to the real-time monitoring weight of each row vector at the previous time and the deviation of the temperature of each collection position from the preset electrolyte temperature, inputs the calculated temperature feedback deviation at each time into the negative feedback controller, and controls the electrolyte temperature of the liquid flow membraneless water electrolysis hydrogen production process through the negative feedback controller; The liquid flow membraneless water electrolysis hydrogen production flow rate control module analyzes the differences of the flow rate matrix with respect to the real-time monitoring weight in the same position in the pressure matrix and the temperature matrix respectively, obtains the monitoring cumulative response value of each data point in the flow rate matrix, processes to obtain the updated real-time monitoring weight of each data point in the flow rate matrix, calculates the flow rate feedback error at each time, and performs feedback control on the flow rate based on the error to keep the flow rate stable in the electrolyte conveying process; and the negative feedback controller is adopted to regulate and control the electrolyte flow rate of the liquid flow membraneless water electrolysis hydrogen production process. The temperature feedback deviation at each time is: ; wherein, represents the temperature feedback deviation at the th moment, represents the temperature at the th moment in the xth row vector in the temperature matrix, represents the preset electrolyte temperature, represents the preset electrolyte temperature, represents the real-time monitoring weight of the data point corresponding to the xth row vector at the th moment in the temperature matrix, and n is the number of row vectors. The calculation process of the flow rate feedback error at each time is: ; wherein, represents the flow rate feedback deviation at the th moment, represents the flow rate at the th moment in the xth row vector in the flow rate matrix, represents the preset electrolyte flow rate, represents the xth row vector in the flow rate matrix, th moment after updating the real-time monitoring weight of the data point corresponding to the xth row vector, and n is the number of row vectors.

2. The liquid flow membraneless electrolytic water splitting system of claim 1, wherein, Further comprising: The left end plate (1), the left insulating plate (2), the anode current collector plate (3), the anode electrolysis chamber (4), the anode gas-liquid outlet (5) and the one-way structure (6); the right end plate (7), the right insulating plate (8), the cathode current collector plate (10), the cathode electrolysis chamber (11); the electrolyte is input into the liquid flow membraneless water electrolysis hydrogen production system from the liquid inlet (12), and the upper part is composed of a gas-liquid separation chamber (13) and a hydrogen outlet (14); the plates are fixed by screws and nuts (9).

3. The liquid flow membraneless electrolytic water splitting system of claim 2, wherein, The one-way structure (6) and the gas-liquid separation chamber (13) are on the same main body, the gas-liquid enters the outlet (15) of the gas-liquid separation chamber (13), is transferred from the gas-liquid separation chamber (13) to the anode electrolysis chamber (4), first passes through the one-way flow channel (16) and is transferred to the inlet (17) of the anode electrolysis chamber (4), the cathode current collector plate (10) and the anode current collector plate (3) both contain electrodes (18), and the gas-liquid mixed fluid after the electrocatalytic hydrogen evolution reaction is discharged to the inlet (19) of the cathode electrolysis chamber (11).

4. The liquid flow membraneless electrolytic water splitting system of claim 3, wherein, The outlet (15) of the gas-liquid separation chamber (13) is higher than the inlet (17) of the electrolyte into the anode electrolysis chamber (4), and the outlet (15) of the gas-liquid separation chamber (13) is opposite to the direction of the inlet (17) of the electrolyte into the anode electrolysis chamber (4).

5. The liquid flow membraneless electrolytic water splitting system of claim 1, wherein, The temperature, pressure and flow rate of each collection position at all times are taken as the row vectors of the temperature matrix, the pressure matrix and the flow rate matrix respectively.

6. The liquid flow membraneless electrolytic water splitting system of claim 1, wherein, The monitoring cumulative response value of each data point in the flow rate matrix is: wherein is the monitoring cumulative response value of the data point corresponding to the flow rate matrix at the th time instant and the th position; represents the mean of all flow rate-pressure monitoring differences obtained from the flow rate matrix and the pressure matrix up to the th time instant and the th position, represents the mean of all flow rate-temperature monitoring differences obtained from the flow rate matrix and the temperature matrix up to the th time instant and the th position.

7. The liquid flow membraneless electrolytic water splitting system of claim 6, wherein, The difference between the flow rate matrix and the pressure matrix and the temperature matrix is calculated respectively, and the difference is used as the flow rate-pressure monitoring difference and the flow rate-temperature monitoring difference at the same position.

8. The liquid flow membraneless electrolytic water splitting system of claim 1, wherein, The updated real-time monitoring weight of each data point in the flow rate matrix is the result of the normalized processing of the monitoring cumulative response value of each data point in the flow rate matrix. The updated real-time monitoring weight of each data point in the flow rate matrix is the result of the normalized processing of the monitoring cumulative response value of each data point in the flow rate matrix.

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