Cooperative regulation and control system and method for hydrogen in oxygen of alkaline water electrolysis hydrogen production system

Abstract

The invention relates to the technical field of hydrogen energy application and water electrolysis hydrogen production, and discloses an oxygen-in-hydrogen coordinated regulation and control system and method for an alkaline water electrolysis hydrogen production system, and the oxygen-in-hydrogen coordinated regulation and control system comprises an alkaline electrolytic bath, a gas-liquid separator and a circulating pump which are communicated with one another to form a loop, the thermal management unit, the pressure regulation unit, the sensing monitoring unit and the multi-physical field coupling controller are arranged on the loop. The controller comprises a data acquisition module, a flux operation module, a viscosity mapping compensation module and a cooperative instruction generation module, the system calculates a dissolved hydrogen migration flux index based on monitoring data, generates a cooperative regulation and control instruction when the index exceeds a safety threshold value, and calculates an expected flow resistance variable quantity based on temperature viscosity characteristics to generate a feedforward compensation signal. Through superposition processing of the regulation and control instruction and the feedforward signal, the execution mechanism is driven to maintain the stability of the transmembrane pressure difference while inhibiting hydrogen transmembrane migration, the problem of pressure difference instability caused by excessive hydrogen concentration and temperature change in oxygen under the low-load working condition is solved, and the wide limit of system operation is widened.

Description

Technical Field

[0001] This invention relates to the fields of hydrogen energy application and water electrolysis hydrogen production technology, specifically to an oxygen-hydrogen synergistic regulation system and method for alkaline water electrolysis hydrogen production system. Background Technology

[0002] Alkaline water electrolysis for hydrogen production is currently the mainstream approach for producing green hydrogen using renewable energy sources. However, renewable energy sources such as wind power and photovoltaics are characterized by fluctuations and intermittency, which requires the electrolysis hydrogen production equipment to have the ability to operate stably over a wide power range.

[0003] In actual operation, when the electrolyzer is under low load, the electrolysis current density decreases, leading to a decline in the production rates of hydrogen and oxygen. However, the microscopic mass transfer process of hydrogen molecules permeating through the membrane to the oxygen side is mainly driven by temperature and system pressure, and does not decrease linearly and synchronously with the decrease in current density. This mismatch between the gas production rate and the permeation rate results in an increase in the proportion of hydrogen mixed in a unit volume of oxygen, which can easily exceed the safety threshold, forcing the system to frequently shut down or maintain a high-energy-consuming hot standby state, thus limiting the load regulation range of the hydrogen production system.

[0004] Existing control strategies typically treat temperature, pressure, and flow rate as independent control loops, using conventional PID feedback logic for individual regulation, lacking a collaborative control mechanism based on multi-physics coupling principles. For example, to suppress gas diffusion, the system needs to lower the operating temperature; however, the dynamic viscosity of the alkali solution increases with decreasing temperature, leading to increased fluid resistance within the electrolyzer's flow channels. Traditional pressure control loops struggle to detect and respond in real-time to these changes in flow resistance caused by temperature variations, often resulting in fluctuations in transmembrane pressure differential. This pressure imbalance not only exacerbates gas crosstalk but also causes mechanical stress damage to the diaphragm over the long term, shortening the electrolyzer's lifespan. Therefore, existing single-variable independent control modes are insufficient to meet the dual requirements of gas purity control and intrinsically safe operation in renewable energy hydrogen production scenarios. Summary of the Invention

[0005] To address the shortcomings of existing technologies, this invention provides a system and method for coordinated regulation of oxygen and hydrogen in an alkaline water electrolysis hydrogen production system. This solves the problems of excessive hydrogen concentration in oxygen caused by hydrogen transmembrane permeation in existing alkaline water electrolysis hydrogen production systems under wide power fluctuation and low load operating conditions, due to the lack of quantitative control methods based on microscopic mass transfer mechanisms. It also addresses the problems of transmembrane pressure differential instability caused by changes in fluid physical properties during regulation, which in turn leads to membrane mechanical damage and the risk of gas leakage.

[0006] To achieve the above objectives, the present invention provides the following technical solution:

[0007] The first aspect of this invention provides an oxygen-hydrogen synergistic regulation system for an alkaline water electrolysis hydrogen production system. The system includes an alkaline electrolyzer interconnected to form an alkaline solution circulation loop, an oxygen-side gas-liquid separator, a hydrogen-side gas-liquid separator, and an alkaline solution circulation pump; a thermal management unit, a pressure regulation unit, and a sensing and monitoring unit disposed on the alkaline solution circulation loop; and a multi-physics coupling controller electrically connected to the aforementioned units.

[0008] In this system, the multiphysics coupling controller is configured to execute coordinated control logic through an internal data acquisition module, flux calculation module, viscosity mapping compensation module, and coordinated instruction generation module. The data acquisition module reads the current density, alkali temperature, system pressure, and alkali flow rate data output by the sensing and monitoring unit. Based on the alkali temperature and system pressure, the flux calculation module calculates the dissolved hydrogen migration flux index, which characterizes the rate at which hydrogen passes through the porous membrane in the alkaline electrolyzer into the oxygen side.

[0009] The collaborative instruction generation module compares the dissolved hydrogen migration flux index with a preset safe flux threshold. When the dissolved hydrogen migration flux index exceeds the safe flux threshold, it generates collaborative control instructions that include commands to reduce system pressure, reduce alkali temperature, or adjust alkali circulation flow rate. The viscosity mapping compensation module stores temperature-viscosity characteristic data of the alkali and the electrolyzer flow channel resistance model. It is configured to calculate the expected dynamic viscosity of the alkali based on the target temperature and, combined with the alkali flow rate, calculate the expected change in flow resistance of the internal flow channels of the electrolyzer, generating a feedforward compensation signal to maintain a constant transmembrane pressure difference.

[0010] The collaborative instruction generation module superimposes the collaborative control instruction with the feedforward compensation signal generated by the viscosity mapping compensation module to drive the alkali circulation pump, thermal management unit and pressure regulation unit, thereby suppressing hydrogen transmembrane migration while maintaining stable transmembrane pressure difference.

[0011] In a preferred embodiment, the logic of the flux calculation module for calculating the dissolved hydrogen migration flux index includes: determining the electrolyzer structural characteristic factor determined by the porosity, tortuosity factor, and effective mass transfer area of ​​the membrane; calculating the temperature-dependent diffusion function characterizing the hydrogen diffusion capacity using a modified form of the Arrhenius equation, which increases with increasing alkaline solution temperature; calculating the pressure-dependent concentration gradient function using the gas-liquid equilibrium principle, which increases with increasing system pressure; and multiplying the electrolyzer structural characteristic factor, the temperature-dependent diffusion function, and the pressure-dependent concentration gradient function to obtain the dissolved hydrogen migration flux index.

[0012] In a preferred embodiment, the logic of the viscosity mapping compensation module in generating the feedforward compensation signal includes: when the cooperative instruction generation module generates a target instruction to reduce the alkaline solution temperature, retrieving the expected dynamic viscosity value corresponding to the alkaline solution temperature reaching the target temperature based on temperature-viscosity characteristic data; using the fluid dynamics friction loss formula, calculating the expected flow resistance pressure drop of the internal flow channel of the electrolyzer based on the expected dynamic viscosity value and the current alkaline solution flow rate; calculating the difference between the expected flow resistance pressure drop and the current actual flow resistance pressure drop to obtain the flow resistance increment; and generating the feedforward compensation signal based on the flow resistance increment.

[0013] Furthermore, the feedforward compensation signal includes a flow correction command or a back pressure bias command. The flow correction command is configured to drive the rotational speed of the alkali circulation pump to decrease proportionally during the temperature drop, keeping the product of the alkali dynamic viscosity and the alkali flow rate constant. The back pressure bias command is configured to drive the pressure regulating unit to reduce the set value of the back pressure valve, thereby reducing the back pressure at the system outlet and accommodating the increase in flow resistance.

[0014] In a preferred embodiment, the cooperative instruction generation module is configured to select a control mode based on the current density and its rate of change. When the current density is detected to be lower than a preset low load threshold and the rate of change is within the steady-state range, the diffusion suppression mode is activated; when the absolute value of the rate of change is detected to exceed a preset fluctuation threshold, the pulsation cleaning mode is activated.

[0015] In the diffusion suppression mode, the cooperative instruction generation module uses the safe flux threshold as a constraint to solve in reverse the maximum allowable alkaline temperature and the maximum allowable system pressure required to satisfy the dissolved hydrogen migration flux index being less than the safe flux threshold, and generates cooperative control instructions accordingly.

[0016] In the pulse cleaning mode, the collaborative command generation module generates collaborative control commands according to a specific timing sequence: In the first stage, a pressure-down pulse command is generated to control the pressure regulating unit to quickly reduce the system pressure and maintain it within a preset time window; in the second stage, at a preset lag time after the pressure-down pulse command is activated, a flow surge pulse command is generated to drive the alkali circulation pump to increase its speed and generate an impact flow rate; in the third stage, after the flow surge pulse command has been activated for a preset cleaning duration, the pressure-down pulse command and the flow surge pulse command are canceled, driving the system pressure and alkali flow rate to return to the steady-state set value corresponding to the current current density.

[0017] In addition, the pressure regulation unit includes an oxygen-side back pressure regulating valve installed on the gas outlet pipeline of the oxygen-side gas-liquid separator, and a hydrogen-side back pressure regulating valve installed on the gas outlet pipeline of the hydrogen-side gas-liquid separator; the thermal management unit includes a heat exchanger and a temperature regulating valve installed on the heat exchanger bypass or cooling medium pipeline. The sensing and monitoring unit includes a transmembrane differential pressure transmitter, with its high-pressure end connected to the gas outlet of the hydrogen-side gas-liquid separator and its low-pressure end connected to the gas outlet of the oxygen-side gas-liquid separator. The multiphysics coupling controller is internally configured with a PID closed-loop control loop. The real-time differential pressure signal output by the transmembrane differential pressure transmitter is input into the PID closed-loop control loop, and the feedforward compensation signal is superimposed as an bias quantity onto the output of the PID closed-loop control loop.

[0018] The second aspect of this invention provides a method for coordinated regulation of oxygen and hydrogen in an alkaline water electrolysis hydrogen production system. This method, based on a multi-physics field coupled controller, includes the following steps: a data acquisition module reads current density, alkaline solution temperature, system pressure, and alkaline solution flow rate data; a flux calculation module calculates the dissolved hydrogen migration flux index using alkaline solution temperature and system pressure based on the physical mechanisms of Fick's first law and Henry's law; a coordinated instruction generation module compares the dissolved hydrogen migration flux index with a preset safe flux threshold; when the dissolved hydrogen migration flux index exceeds the safe flux threshold, a coordinated regulation instruction is generated, including reducing system pressure, reducing alkaline solution temperature, or adjusting the alkaline solution circulation flow rate; a viscosity mapping compensation module calculates the expected dynamic viscosity of the alkaline solution based on the target temperature and calculates the expected change in flow resistance of the internal flow channels of the electrolyzer based on the alkaline solution flow rate, generating a feedforward compensation signal; after superimposing the coordinated regulation instruction and the feedforward compensation signal, the actuator of the alkaline water electrolysis hydrogen production system is driven, thereby maintaining a stable transmembrane pressure difference while suppressing hydrogen transmembrane migration.

[0019] This invention provides a system and method for synergistic regulation of oxygen and hydrogen in an alkaline water electrolysis hydrogen production system. It has the following beneficial effects:

[0020] 1. This invention constructs a dissolved hydrogen migration flux index model, transforming the microscopic mass transfer process, which cannot be directly measured, into a calculable index based on temperature and pressure. This overcomes the limitations of traditional control methods that rely solely on linear adjustment of current density. The system can quantitatively assess the risk of hydrogen transmembrane migration based on the physical mechanisms of Fick's first law and Henry's law. Furthermore, by inversely solving the temperature and pressure combination corresponding to the safe flux threshold, it achieves inherently safe control of the hydrogen content in oxygen, thus broadening the low-load operating tolerance of alkaline water electrolysis hydrogen production systems.

[0021] 2. This invention introduces a viscosity mapping compensation module and a feedforward control strategy, which effectively solves the problem of system pressure field imbalance caused by fluid property changes due to temperature regulation. By predicting the change in dynamic viscosity of alkaline solution and the increase in flow resistance caused by temperature changes, the system can automatically generate feedforward signals for flow correction or back pressure bias while performing temperature regulation, thereby decoupling pressure control from temperature changes and ensuring that the transmembrane pressure difference is always maintained near zero under large temperature variation conditions, thus preventing diaphragm mechanical damage caused by physical parameter coupling.

[0022] 3. This invention achieves differentiated collaborative control based on operating condition identification. For the low-load steady-state range, a diffusion suppression strategy of cooling and depressurization is adopted, and for the transient range of variable load, a pulse cleaning strategy of pressure induction and flow shearing is adopted. This hierarchical control logic can not only block gas permeation channels through physical dimensionality reduction under steady state, but also effectively remove stagnant bubbles on the surface of the electrode plate under transient fluctuations. It solves the problems of gas leakage and local overheating caused by drastic load changes in renewable energy fluctuation scenarios, and improves the dynamic response capability and operational safety of the system. Attached Figure Description

[0023] Figure 1 This is a schematic diagram of the system hardware architecture connection of the present invention;

[0024] Figure 2 This is a flowchart illustrating the logic for calculating dissolved hydrogen migration flux in this invention.

[0025] Figure 3 This is the main flow chart of the system pressure, alkali circulation flow rate and alkali temperature coordinated control method of the present invention.

[0026] Figure 4 This is a block diagram of the viscosity mapping and pressure difference balance control logic of the present invention.

[0027] The components include: 10. Alkaline electrolyzer; 20. Oxygen-side gas-liquid separator; 30. Hydrogen-side gas-liquid separator; 40. Alkali circulation pump; 50. Thermal management unit; 51. Heat exchanger; 52. Temperature regulating valve; 60. Pressure regulating unit; 61. Oxygen-side back pressure regulating valve; 62. Hydrogen-side back pressure regulating valve; 70. Sensing and monitoring unit; 71. Current density sensor; 72. Temperature sensor group; 73. Pressure sensor group; 74. Flow sensor; 75. Hydrogen concentration analyzer in oxygen; 80. Multiphysics coupling controller; 81. Data acquisition module; 82. Flux calculation module; 83. Viscosity mapping compensation module; and 84. Cooperative instruction generation module. Detailed Implementation

[0028] The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0029] See attached document Figure 1 The present invention provides an oxygen-hydrogen synergistic regulation system for an alkaline water electrolysis hydrogen production system. The system includes an alkaline electrolyzer 10, an oxygen-side gas-liquid separator 20, a hydrogen-side gas-liquid separator 30, an alkaline circulating pump 40, a thermal management unit 50, a pressure regulating unit 60, a sensing and monitoring unit 70, and a multi-physics field coupling controller 80.

[0030] The alkaline electrolyzer 10 is internally equipped with an anode chamber, a cathode chamber, and a porous membrane located between the anode and cathode chambers. It is configured to decompose water to produce oxygen and hydrogen under the action of direct current. The oxygen outlet of the alkaline electrolyzer 10 is connected to the inlet of the oxygen-side gas-liquid separator 20 via a pipeline for separating oxygen and alkaline solution. The hydrogen outlet of the alkaline electrolyzer 10 is connected to the inlet of the hydrogen-side gas-liquid separator 30 via a pipeline for separating hydrogen and alkaline solution.

[0031] The liquid outlets of the oxygen-side gas-liquid separator 20 and the hydrogen-side gas-liquid separator 30 merge and are connected to the suction inlet of the alkali circulation pump 40. The alkali circulation pump 40 is a variable frequency speed control pump configured to drive the alkali solution to circulate within the system, and its outlet is connected to the thermal management unit 50 via a pipeline. The thermal management unit 50 is configured to regulate the temperature of the alkali solution flowing through it, and its outlet is connected to the alkali solution inlet of the alkaline electrolyzer 10. The thermal management unit 50 includes a heat exchanger 51 and a temperature regulating valve 52 located on the bypass or cooling medium pipeline of the heat exchanger 51. The heat exchange rate of the alkali solution is changed by adjusting the opening degree of the temperature regulating valve 52.

[0032] The pressure regulating unit 60 includes an oxygen-side back pressure regulating valve 61 installed on the gas outlet pipeline of the oxygen-side gas-liquid separator 20, and a hydrogen-side back pressure regulating valve 62 installed on the gas outlet pipeline of the hydrogen-side gas-liquid separator 30. Both the oxygen-side back pressure regulating valve 61 and the hydrogen-side back pressure regulating valve 62 are continuously adjustable electric or pneumatic regulating valves, configured to regulate the operating pressure of the oxygen side and hydrogen side of the system, respectively.

[0033] The sensing and monitoring unit 70 is configured to collect the operating status parameters of the system in real time, including: a current density sensor 71, used to collect the real-time current density supplied to the alkaline electrolyzer 10; a temperature sensor group 72, including an inlet temperature sensor at the inlet of the alkaline electrolyzer 10 and an outlet temperature sensor at the outlet, used to collect the alkaline solution temperature; a pressure sensor group 73, including an oxygen-side pressure sensor on the oxygen-side pipeline and a hydrogen-side pressure sensor on the hydrogen-side pipeline, used to collect the system operating pressure; and a transmembrane differential pressure transmitter, whose high-pressure end is connected to the gas outlet of the hydrogen-side gas-liquid separator 30 and its low-pressure end is connected to the gas outlet of the oxygen-side gas-liquid separator 20, configured to directly measure and output the real-time differential pressure signal between the hydrogen and oxygen sides as the final safety feedback signal of the system; a flow sensor 74, installed on the alkaline solution circulation pipeline, used to collect the alkaline solution circulation flow rate; and an oxygen hydrogen concentration analyzer 75, installed at the gas outlet of the oxygen-side gas-liquid separator 20, used to detect the hydrogen content in the oxygen.

[0034] The multiphysics coupling controller 80 is electrically connected to the alkali circulation pump 40, temperature regulating valve 52, oxygen-side back pressure regulating valve 61, hydrogen-side back pressure regulating valve 62, and each sensor in the sensing and monitoring unit 70. The multiphysics coupling controller 80 is configured to receive signals collected by the sensing and monitoring unit 70 and generate control commands based on internally preset control logic to drive the aforementioned actuators. The control commands are transmitted to each actuator via a 4-20mA analog signal, Modbus bus signal, or Profinet industrial Ethernet signal. The multiphysics coupling controller 80 also has an internal PID closed-loop control loop, with a feedforward compensation signal superimposed as a bias quantity at the output of the PID closed-loop control loop.

[0035] The multiphysics coupling controller 80 includes a data acquisition module 81, a flux calculation module 82, a viscosity mapping compensation module 83, and a cooperative instruction generation module 84.

[0036] The data acquisition module 81 is configured to read the current density, alkali temperature, system pressure, and alkali flow rate data output by the sensing and monitoring unit 70 at a preset sampling frequency, and to perform filtering processing on the data.

[0037] The flux calculation module 82 is configured to calculate the dissolved hydrogen migration flux index, which characterizes the rate at which hydrogen gas passes through the porous membrane into the oxygen side, based on the physical mechanisms of Fick's first law and Henry's law and the alkaline temperature and system pressure obtained by the data acquisition module 81. The dissolved hydrogen migration flux index characterizes the physical quantity of hydrogen molecules passing through the membrane per unit time driven by the concentration gradient.

[0038] The dissolved hydrogen migration flux index is calculated based on the following logic: the diffusion coefficient of hydrogen in alkaline solution is positively correlated with the temperature of the alkaline solution, and the solubility of hydrogen in alkaline solution is positively correlated with the system pressure. The flux calculation module 82 calculates the dissolved hydrogen migration flux index using the following functional relationship:

[0039] ;

[0040] In the formula: Indicates the dissolved hydrogen migration flux index; These represent characteristic constants related to the porosity and geometry of porous membranes. This represents the temperature-dependent diffusion function, the value of which varies with the temperature of the alkali solution. The increase in the value represents the thermal motion and diffusion ability of hydrogen molecules in alkaline solution. This represents the pressure-dependent concentration gradient function, the value of which varies with system pressure. The increase in concentration represents the driving potential for hydrogen to migrate from a high-concentration liquid phase to a gas phase or a low-concentration side.

[0041] The viscosity mapping compensation module 83 is configured to store temperature-viscosity characteristic data of the alkali solution and the electrolyzer flow channel resistance model. Before the system performs temperature adjustment, the viscosity mapping compensation module 83 calculates the expected dynamic viscosity of the alkali solution based on the target temperature and, in conjunction with the current alkali solution circulation flow rate, calculates the expected change in flow resistance within the electrolyzer flow channel. The viscosity mapping compensation module 83 is further configured to generate a feedforward compensation signal to maintain a constant transmembrane pressure difference based on the expected change in flow resistance. The feedforward compensation signal includes a speed correction command for the alkali solution circulation pump 40 or an opening correction command for the oxygen-side back pressure regulating valve 61 and the hydrogen-side back pressure regulating valve 62.

[0042] The collaborative instruction generation module 84 is configured to select a control mode based on the comparison result of the dissolved hydrogen migration flux index and a preset threshold. When the dissolved hydrogen migration flux index exceeds the preset threshold, the collaborative instruction generation module 84 generates a collaborative control instruction. The collaborative control instructions include instructions to reduce system pressure, instructions to reduce alkali temperature, and instructions to adjust the alkali circulation flow rate. The collaborative instruction generation module 84 superimposes the collaborative control instructions with the feedforward compensation signal generated by the viscosity mapping compensation module 83, and finally outputs the result to the alkali circulation pump 40, temperature control valve 52, oxygen-side back pressure control valve 61, and hydrogen-side back pressure control valve 62, driving the system to maintain a stable transmembrane pressure difference while suppressing hydrogen migration.

[0043] See attached document Figure 2This embodiment details the calculation model and application logic used by the flux calculation module 82 inside the multiphysics coupling controller 80. The dissolved hydrogen migration flux index model is a digital mapping model based on the electrochemical and hydrodynamic mass transfer mechanism. Its core lies in transforming the microscopic mass transfer process, which cannot be directly measured in real time, into a quantitative index that can be calculated in real time from macroscopic operating parameters (temperature, pressure).

[0044] The flux calculation module 82 is pre-loaded with a diffusion rate sub-model based on Fick's first law and a solubility sub-model based on Henry's law. In the process of producing hydrogen through alkaline water electrolysis, the process of hydrogen gas passing through the ion exchange membrane or porous membrane from the high-concentration alkaline solution side to the oxygen side is mainly driven by two physical factors: the liquid phase diffusion coefficient and the transmembrane concentration gradient.

[0045] The diffusion rate sub-model is configured to quantify the effect of temperature on the mass transfer process. Increased temperature in the alkali solution leads to a decrease in the dynamic viscosity of the solution and an increase in the thermal kinetic energy of gas molecules, resulting in an exponential increase in the diffusion coefficient of hydrogen in the alkali solution. The flux calculation module 82 uses a modified form of the Arrhenius equation to characterize this physical process. The solubility sub-model is configured to quantify the effect of pressure on the mass transfer process. According to the gas-liquid equilibrium principle, the saturation concentration of dissolved hydrogen in the alkali solution is linearly positively correlated with the absolute pressure of the system; an increase in system pressure directly increases the source concentration potential energy driving hydrogen transmembrane migration.

[0046] Based on the aforementioned physical mechanism, the flux calculation module 82 inputs the collected real-time alkaline solution temperature and system pressure into the comprehensive calculation model to calculate the current dissolved hydrogen migration flux index. In specific implementation, the dissolved hydrogen migration flux index... The calculation is performed using the following mathematical formula:

[0047] ;

[0048] In the formula: The dissolved hydrogen migration flux index is expressed in moles per square meter per second (mol / (m²)). 2 ·s)) or a normalized dimensionless value, characterizing the physical intensity of hydrogen permeation flux; This represents the structural characteristic factor of the electrolyzer. This value is determined by the porosity, tortuosity factor, and effective mass transfer area of ​​the diaphragm. After the equipment is finalized, it is either a constant or a variable that is corrected for aging over time. In specific implementation, the characteristic constant... and structural characteristic factors Obtained through calibration tests: Under standard temperature and pressure, tracer gas is introduced into one side of the electrolytic cell, and the permeation rate on the other side is measured. The initial structural factor of the equipment is obtained by backfitting, or it can be preset based on the Darcy permeability parameters of porous media provided by the diaphragm manufacturer. This represents the limiting pre-diffusion factor of hydrogen under standard conditions; This represents the diffusion activation energy of hydrogen in an alkaline medium, expressed in joules per mole (J / mol). Represents the ideal gas constant; This indicates the real-time Kelvin temperature of the alkaline solution after being collected and filtered by temperature sensor group 72. Henry's constant represents hydrogen in working concentration alkaline solution, and is the conversion coefficient between pressure and dissolved concentration; This indicates the real-time absolute pressure of the system collected by pressure sensor group 73; This indicates the permissible hydrogen reference concentration in the oxygen-side alkaline solution or the low concentration boundary value maintained by gas-liquid separation and exhaust on the oxygen side.

[0049] The flux calculation module 82 performs the above calculations in each control cycle and displays the results calculated in real time. The data is transmitted to the collaborative instruction generation module 84. The collaborative instruction generation module 84 internally stores a preset safe throughput threshold. This safe throughput threshold It is the critical physical flux value derived by back-calculating based on the premise that the hydrogen concentration in oxygen does not exceed the safety standard (e.g., 1.5% or 2.0%).

[0050] When calculated Less than the safe flux threshold When the system determines that the current operating condition is within the intrinsically safe range, it maintains the conventional control strategy, that is, maintaining the rated operating temperature and operating pressure to maintain electrolysis efficiency.

[0051] When calculated Greater than or equal to the safe flux threshold At this point, the system determines that there is a physical trend of excessive hydrogen in the oxygen level under the current operating conditions. The coordinated instruction generation module 84 then generates targeted control instructions based on the physical correlation of the above formula:

[0052] On the one hand, by lowering the target temperature Using the exponential term The attenuation characteristics significantly reduce the diffusion coefficient; on the other hand, by reducing the target pressure Using linear terms The reduction of [something] decreases the driving force of the concentration gradient. Through the inverse solution of the mathematical model, the controller can accurately calculate the [something] in order to [something]. Press back to The following combination of target setpoints for temperature and pressure is required to achieve mechanism-based quantitative and precise control.

[0053] See attached document Figure 3This embodiment details how the multiphysics coupling controller 80 performs decoupled and coordinated regulation of system pressure, alkali circulation flow rate, and alkali temperature under different operating conditions based on real-time operating status. This method breaks through the limitations of traditional single-parameter linear adjustment following current and establishes an active defense logic based on physical mass transfer mechanisms.

[0054] The coordinated control method first performs a condition identification step. The multiphysics coupling controller 80 monitors the operating current density of the alkaline electrolyzer 10 in real time through the data acquisition module 81. and its rate of change Based on these two parameters, the controller divides the current system operating state into a low-load steady-state range and a variable-load transient range. Simultaneously, it combines the dissolved hydrogen migration flux index calculated in the aforementioned embodiments. The controller executes specific control strategies based on the following logic branches.

[0055] When the operating current density is monitored Below a preset low load threshold (e.g., 30% of rated current), and the rate of change of current. When the system is within the steady-state range, the controller determines that it has entered the low-load steady-state region. At this time, due to the significant decrease in gas production rate, the flow velocity of the gas-liquid mixture inside the electrolyzer decreases, resulting in a weakened bubble desorption capacity on the electrode surface, and gas transmembrane permeation becomes the main risk. Under this condition, the cooperative instruction generation module 84 activates the diffusion suppression mode.

[0056] In diffusion suppression mode, the controller performs simultaneous dimensionality-reduced regulation of temperature and pressure. First, the controller performs inverse optimization calculations based on a dissolved hydrogen migration flux exponential model. Specifically, the controller sets a safe flux threshold... As a constraint, the reverse solution satisfies... Required maximum permissible alkali temperature and maximum permissible system pressure Subsequently, the controller generates a target temperature setting command, driving the temperature regulating valve 52 in the thermal management unit 50 to increase the proportion of alkaline solution flowing through the heat exchanger 51 or increase the flow rate of the cooling medium, actively lowering the alkaline solution temperature from the rated operating temperature (typically 80-90℃) to the calculated target low temperature value (e.g., 60-65℃). By lowering the temperature, the physical increase in electrolyte viscosity and the slowing down of gas molecule thermal motion reduce the diffusion coefficient of hydrogen in the electrolyte and the equivalent pore size of the membrane micropores, thereby physically blocking the gas migration channels.

[0057] Simultaneously, in diffusion suppression mode, the controller generates a target pressure setting command, driving the oxygen-side back pressure regulating valve 61 and the hydrogen-side back pressure regulating valve 62 in the pressure regulating unit 60 to synchronously reduce their openings, lowering the system operating pressure to the critical pressure value. The critical pressure value is set to be higher than the sum of the saturated vapor pressure of the electrolyte and the pump's net positive suction head (NPSH) pressure, to prevent boiling of the liquid surface in the gas-liquid separator or cavitation at the pump inlet. By reducing the total pressure, Henry's Law is used to reduce the absolute solubility of hydrogen in the liquid phase, thereby reducing the total amount of solute available for diffusion.

[0058] When the rate of change of operating current density is monitored When the absolute value of the current exceeds the preset fluctuation threshold (e.g., a change exceeding 5% of the rated current per second), especially during rapid load reduction, the controller determines that the system has entered a variable load transient range. At this time, the main risk inside the electrolytic cell is the hysteresis effect between the decreased bubble generation rate caused by the sudden drop in current and the failure of existing attached bubbles to detach in time, which easily leads to the formation of a gas film on the electrode surface. Under this condition, the collaborative instruction generation module 84 activates the pulse cleaning mode.

[0059] In the pulsed cleaning mode, the controller employs a time-decoupled control strategy for pressure and flow, meaning that instead of maintaining constant or linear pressure and flow, a specific phase difference is introduced for dynamic adjustment. The specific implementation steps are as follows:

[0060] The first stage involves executing a pressure-induced nucleation process. The controller generates a short-duration pressure-down pulse command, controlling the back pressure regulating valve to rapidly reduce the system pressure and maintain it for a short time window. This sudden pressure drop aims to disrupt the gas-liquid equilibrium of dissolved gases in the electrolyte, artificially creating supersaturation, and inducing deeply dissolved hydrogen molecules to rapidly nucleate and precipitate into microbubbles on the electrode surface or at the pore openings of the diaphragm.

[0061] The second stage involves executing a flow shearing and stripping action. This is done after a preset lag time following the initiation of the pressure probe action. At a time interval of 50ms to 500ms (e.g.), the controller generates a flow surge pulse command, driving the alkali circulation pump 40 to rapidly increase its speed, generating an impact flow rate higher than the current density matching value. This flow surge action aims to utilize the strong fluid shear force generated by the high flow rate, and using the fluid dynamics boundary layer theory, to thin the laminar sublayer thickness on the electrode surface, forcibly peeling off and carrying away the microbubbles induced in the first stage and originally attached to them out of the electrolysis chamber.

[0062] The third stage is the execution of the state recovery action. After the flow surge action continues for a preset cleaning duration (e.g., 10 to 30 seconds), the controller cancels the pressure reduction command and the flow surge command, and drives the system pressure and alkali circulation flow rate to smoothly recover to the steady-state set value corresponding to the current current density according to the preset slope, completing one complete pulse cleaning cycle.

[0063] Lag time The settings are determined based on the nucleation kinetic time constant of bubbles, ensuring that when the fluid shock wave arrives, the bubbles have completed nucleation and are at a critical size that is easy to peel off. Through the timing coordination of the above-mentioned pressure induction and flow shear, the system can effectively remove trapped bubbles on the surface of the plates and diaphragm during periods of severe load fluctuations, preventing the risk of gas leakage caused by local overheating or bubble bridging.

[0064] Before being sent to the specific actuator, the temperature regulation command, pressure regulation command, and flow regulation command generated above must be transmitted to the subsequent viscosity mapping compensation module 83 for flow resistance verification and feedforward compensation calculation to ensure that the transmembrane pressure difference inside the electrolyzer is always maintained within a safe range when performing large parameter adjustments.

[0065] See attached document Figure 4 This embodiment details the viscosity mapping compensation module 83 within the multiphysics coupling controller 80 and its linkage mechanism with the actuator. This mechanism is configured to address the technical problem of system pressure field imbalance caused by changes in fluid physical properties due to temperature regulation, and achieves zero-drift anchoring of transmembrane pressure difference through a feedforward control strategy.

[0066] The viscosity mapping compensation module 83 integrates a fluid property database and a flow channel hydraulic resistance calculation unit. The fluid property database stores temperature-dynamic viscosity characteristic curves for potassium hydroxide or sodium hydroxide alkaline solutions of specific concentrations (e.g., 30% by mass). These characteristic curves indicate the dynamic viscosity of the alkaline solution. With temperature The decrease in viscosity exhibits a non-linear upward trend. Fluid property databases are constructed using polynomial fitting formulas or lookup tables. For example, the mapping relationship between temperature and viscosity is stored using the Vogel-Fulcher-Tammann equation, and the controller is based on real-time temperature... Substitute the values ​​into the equation to solve for the dynamic viscosity. The flow channel hydraulic resistance calculation unit stores the flow resistance coefficients that characterize the geometric features of the flow channels inside the electrolyzer. This coefficient is determined by the channel length, hydraulic diameter, and channel roughness.

[0067] When the cooperative instruction generation module 84 generates a target instruction to lower the alkaline solution temperature in order to suppress hydrogen diffusion (denoted as...), When the temperature actually drops, the viscosity mapping compensation module 83 does not wait for the temperature to actually decrease, but immediately starts the feedforward calculation process. First, the viscosity mapping compensation module 83, based on the fluid property database, retrieves or interpolates the value of the solution when the temperature reaches a certain level. The expected dynamic viscosity value corresponding to the time Subsequently, combined with the current real-time alkali circulation flow rate... The expected flow resistance pressure drop in the internal flow channels of the electrolyzer is calculated using the friction loss formula from fluid mechanics. .

[0068] The calculation of the expected flow resistance pressure drop follows the following physical relationship:

[0069] ;

[0070] In the formula: This represents the predicted friction loss of fluid flowing through the electrolysis chamber; The preset flow resistance geometric coefficient; The expected dynamic viscosity is calculated based on the target temperature; This represents the current actual volumetric flow rate.

[0071] Viscosity mapping compensation module 83 further calculates the flow resistance increment. This value is the difference between the expected flow resistance pressure drop and the current actual flow resistance pressure drop. If A positive value indicates that cooling will increase the fluid resistance inside the electrolyzer, leading to a passive increase in the pressure at the inlet. If the system only controls the outlet back pressure to remain constant, the average pressure distributed along the flow path inside the electrolyzer will increase. Furthermore, due to slight differences in the flow channel structure or gas-liquid ratio between the hydrogen and oxygen sides, this overall increase in pressure field can easily cause the local transmembrane pressure difference to exceed the safety threshold.

[0072] Based on the calculated flow resistance increment The viscosity mapping compensation module 83 generates a reverse feedforward compensation command and performs dynamic balance control using one of the following two paths or a combination thereof:

[0073] The first compensation path is the flow correction path. The system automatically generates the corrected flow setpoint based on the principle of equal shear force or equal pressure drop. The calculation logic aims to offset the increased resistance caused by higher viscosity by reducing the flow rate, thus making the product... Maintaining a relatively constant flow rate. The controller sends the corrected flow rate setpoint to the alkali circulation pump 40, driving the pump speed to decrease proportionally as the temperature drops, thereby ensuring that the fluid dynamic field inside the electrolyzer does not fluctuate drastically due to temperature changes.

[0074] The second compensation path is the back pressure bias path. When the process requires maintaining a high flow rate for flushing and the flow rate cannot be reduced, the system calculates the flow resistance increment. The controller determines the specific impact value on the transmembrane pressure difference and generates pre-adjustment commands for the opening of the oxygen-side back pressure regulating valve 61 or the hydrogen-side back pressure regulating valve 62. Specifically, while the temperature actuator operates, the controller actively reduces the set value of the back pressure valve to lower the back pressure at the system outlet, thereby creating pressure space to accommodate the increased internal flow resistance pressure drop due to increased viscosity, thus maintaining the balance of the average pressure inside the electrolyzer relative to the diaphragm.

[0075] The viscosity mapping compensation module 83 superimposes the calculated flow correction command or back pressure bias command as a feedforward signal into the system's PID control loop. Through this mechanism, the system achieves synchronous decoupling of pressure control and temperature change during large-scale temperature variations, ensuring that the transmembrane pressure difference between the hydrogen and oxygen sides remains anchored near a preset zero point (e.g., within ±2 kPa) throughout the entire dynamic process of the alkali solution thickening due to temperature decrease. This prevents the risk of diaphragm mechanical damage caused by physical parameter coupling. It is worth noting that the feedforward signal output by the viscosity mapping compensation module 83 is used for coarse adjustment to quickly offset the main pressure fluctuation trend; simultaneously, the system uses the real-time differential pressure value collected by the transmembrane pressure transmitter for PID feedback fine adjustment, eliminating the residual between model calculation errors and the actual physical environment (such as pipeline scaling and valve hysteresis), ensuring closed-loop convergence of control accuracy.

[0076] This embodiment illustrates in detail the entire process of the system switching from rated high load to low load standby through a specific operating scenario, demonstrating how the multi-physics coupling controller 80 coordinates control actions in four dimensions: pressure induction, flow shearing, temperature regulation, and viscosity compensation.

[0077] In the initial stage ( At any given time, the system is operating at its rated full load, and the operating current density is maintained at the nominal value (e.g., 4000 A / m). 2 (Above). At this time, the multiphysics coupling controller 80 controls the thermal management unit 50 to maintain the alkali solution temperature at the standard operating temperature (e.g., 85°C), controls the pressure regulating unit 60 to maintain the system pressure at the standard operating pressure (e.g., 1.6 MPa), and controls the alkali solution circulation pump 40 to operate at the rated flow rate. In this state, the flux calculation module 82 calculates the dissolved hydrogen migration flux index in real time. Below the preset safe throughput threshold The system is in a conventional closed-loop control mode, with the main objective being to maintain the thermal balance of the electrolyzer.

[0078] exist At that moment, the data acquisition module 81 detected a step drop in the operating current density (for example, due to fluctuations in renewable energy power, the command current drops from 100% to 20% within 5 seconds), and simultaneously the current change rate... The system exceeds the preset fluctuation threshold. The collaborative instruction generation module 84 immediately determines that the system has entered the transient range of variable load and activates the pulsed cleaning control logic. The controller first generates a pressure drop instruction, driving the oxygen-side back pressure regulating valve 61 and the hydrogen-side back pressure regulating valve 62 to operate synchronously, causing the system pressure to drop rapidly to the induced pressure value within a short period of time (e.g., within 200ms). This sudden pressure drop disrupts the dissolution equilibrium at the gas-liquid interface, causing the electrolyte to be in a supersaturated state, which promotes the rapid nucleation and precipitation of hydrogen molecules dissolved in the boundary layer of the electrode surface.

[0079] Following closely behind, At a certain moment (e.g., with a lag of 300 ms), the controller generates a flow surge command. In response to this command, the alkali circulation pump 40 instantaneously increases its speed to 110% of its maximum rated speed or maintains the current high flow rate without immediately decreasing as the current drops. At this time, a high-speed fluid shock wave is generated in the flow channels inside the electrolyzer. Since the bubbles have already nucleated and grown under the pressure induction of the previous stage, the strong shear force generated by the fluid shock wave can effectively overcome the adhesion of the bubbles to the electrode surface, forcibly peeling off the stagnant microbubbles and carrying them out of the electrolysis chamber. This pulsating cleaning process continues for a preset time window (e.g., 10–30 seconds) and is then automatically terminated by the controller.

[0080] exist At this point, the current density stabilizes at a low load level (e.g., 20%), and the pulsating cleaning process is complete. At this time, the flux calculation module 82 performs predictive calculations based on the current low current density, standard temperature, and standard pressure conditions. It finds that if the current operating parameters of 85℃ and 1.6MPa are maintained, the dissolved hydrogen migration flux index... Will exceed the safe throughput threshold There is a risk of excessive hydrogen in the oxygen content. The collaborative instruction generation module 84 then switches to diffusion suppression mode and determines new target operating parameters—target temperature—through a reverse calculation model. Set to 60℃, target pressure Set to 0.5 MPa.

[0081] exist to During the parameter adjustment transition, the viscosity mapping compensation module 83 intervenes in the control. As the thermal management unit 50 begins to increase the cooling power, the alkali solution temperature gradually decreases from 85℃ to 60℃. The viscosity mapping compensation module 83 calculates the dynamic viscosity of the alkali solution in real time based on the temperature change rate by querying the fluid property database. It is gradually increasing. Based on the flow channel resistance model. It is predicted that if the flow rate remains constant, the increase in viscosity will lead to an increase in the flow resistance pressure drop inside the electrolyzer, thereby raising the inlet pressure and disrupting the transmembrane pressure differential balance.

[0082] To counteract this physical effect, the viscosity mapping compensation module 83 generates a continuous flow correction feedforward signal. During the temperature decrease, the controller drives the alkali circulation pump 40 to decrease its speed at a specific slope. This rate of flow decrease is precisely matched to the rate of viscosity increase through a model, such that the product... Maintaining relative constancy. Through this feedforward compensation, although the alkali solution becomes more viscous, the pressure loss flowing through the electrolyzer is reduced. This ensures that the pressure distribution on the hydrogen and oxygen sides remains unchanged, thus maintaining a dynamic balance during the cooling process, and the transmembrane pressure difference reading remains stable within the range of 0±1 kPa.

[0083] Finally in At that moment, the system reached a new steady state: operating at 20% current density, 60°C alkali solution temperature, 0.5MPa system pressure, and a low circulation flow rate after viscosity correction. Under this state, although the gas production was low, the low temperature significantly reduced the diffusion coefficient, and the low pressure reduced the solubility concentration gradient, allowing for real-time calculations... Falling back to The following results show that the device operates with inherent safety under low load conditions without any mechanical damage to the diaphragm caused by significant parameter adjustments.

Claims

1. A system for coordinated regulation of oxygen and hydrogen in an alkaline water electrolysis hydrogen production system, characterized in that, include: An alkaline electrolytic cell, an oxygen-side gas-liquid separator, a hydrogen-side gas-liquid separator, and an alkaline circulation pump are interconnected to form an alkaline solution circulation loop. A thermal management unit, a pressure regulation unit, and a sensing and monitoring unit are installed on the alkaline solution circulation loop; And a multi-physics coupling controller, which is electrically connected to the alkali circulation pump, the thermal management unit, the pressure regulating unit and the sensing and monitoring unit respectively; The multiphysics coupling controller includes a data acquisition module, a flux calculation module, a viscosity mapping compensation module, and a cooperative instruction generation module. The data acquisition module is configured to read the current density, alkali temperature, system pressure, and alkali flow rate data output by the sensing and monitoring unit. The flux calculation module is configured to calculate the dissolved hydrogen migration flux index, which characterizes the rate at which hydrogen passes through the porous membrane in the alkaline electrolyzer into the oxygen side, based on the alkaline solution temperature and system pressure. The viscosity mapping compensation module is configured to store the temperature viscosity characteristics data of the alkali solution and the flow channel resistance model of the electrolyzer, calculate the expected dynamic viscosity of the alkali solution based on the target temperature, calculate the expected flow resistance change of the flow channel inside the electrolyzer in combination with the alkali solution flow rate, and generate a feedforward compensation signal to maintain a constant transmembrane pressure difference. The collaborative instruction generation module is configured to compare the dissolved hydrogen migration flux index with a preset safe flux threshold. When the dissolved hydrogen migration flux index exceeds the safe flux threshold, a coordinated control command is generated, which includes a command to reduce system pressure, a command to reduce alkali temperature, or a command to adjust alkali circulation flow rate. The collaborative instruction generation module superimposes the collaborative control instruction with the feedforward compensation signal generated by the viscosity mapping compensation module to drive the alkali circulation pump, the thermal management unit, and the pressure regulation unit, thereby maintaining a stable transmembrane pressure difference while suppressing hydrogen transmembrane migration.

2. The oxygen-hydrogen synergistic regulation system for alkaline water electrolysis hydrogen production according to claim 1, characterized in that, The logic for calculating the dissolved hydrogen migration flux index by the flux calculation module includes: The structural characteristic factors of the electrolyzer are determined, which are determined by the porosity, tortuosity factor and effective mass transfer area of ​​the diaphragm. The temperature-dependent diffusion function characterizing the hydrogen diffusion capacity is calculated using a modified form of the Arrhenius equation, wherein the temperature-dependent diffusion function characterizing the hydrogen diffusion capacity increases with increasing alkaline solution temperature. The pressure-related concentration gradient function is calculated using the principle of gas-liquid equilibrium, and the pressure-related concentration gradient function increases with the increase of the system pressure. The dissolved hydrogen migration flux index is obtained by multiplying the electrolyzer structural characteristic factor, the temperature-related diffusion function, and the pressure-related concentration gradient function.

3. The oxygen-hydrogen synergistic regulation system for alkaline water electrolysis hydrogen production according to claim 1, characterized in that, The logic for generating the feedforward compensation signal by the viscosity mapping compensation module includes: When the collaborative instruction generation module generates a target instruction to reduce the temperature of the alkali solution, it retrieves the expected dynamic viscosity value corresponding to the alkali solution temperature reaching the target temperature based on the temperature-viscosity characteristic data. Using the fluid dynamics friction loss formula, the expected flow resistance pressure drop of the internal flow channel of the electrolyzer is calculated based on the expected dynamic viscosity value and the current alkali flow rate. The difference between the expected flow resistance pressure drop and the current actual flow resistance pressure drop is calculated to obtain the flow resistance increment; The feedforward compensation signal is generated based on the flow resistance increment.

4. The oxygen-hydrogen synergistic regulation system for alkaline water electrolysis hydrogen production according to claim 3, characterized in that, The feedforward compensation signal includes a flow correction command or a back pressure bias command. The flow correction command is configured to drive the rotational speed of the alkali circulation pump to decrease proportionally during the temperature drop, so that the product of the alkali dynamic viscosity and the alkali flow rate remains constant. The back pressure bias command is configured to drive the pressure regulating unit to reduce the set value of the back pressure valve, thereby reducing the back pressure at the system outlet and accommodating the flow resistance increment.

5. The oxygen-hydrogen synergistic regulation system for alkaline water electrolysis hydrogen production according to claim 1, characterized in that, The collaborative instruction generation module is configured to select a control mode based on the current density and its rate of change. When the current density is detected to be lower than the preset low load threshold and the rate of change is within the steady state range, the diffusion suppression mode is activated. When the absolute value of the rate of change exceeds the preset fluctuation threshold, the pulsating cleaning mode is activated.

6. The oxygen-hydrogen synergistic regulation system for the alkaline water electrolysis hydrogen production system according to claim 5, characterized in that, In the diffusion suppression mode, the cooperative instruction generation module uses the safety flux threshold as a constraint to solve in reverse the maximum allowable alkaline temperature and maximum allowable system pressure required to satisfy the requirement that the dissolved hydrogen migration flux index is less than the safety flux threshold, and generates the cooperative control instruction accordingly.

7. The oxygen-hydrogen synergistic regulation system for alkaline water electrolysis hydrogen production according to claim 5, characterized in that, In the pulsed cleaning mode, the collaborative instruction generation module generates the collaborative control instructions according to the following timing sequence: In the first stage, a pressure-down pulse command is generated to control the pressure regulating unit to quickly reduce the system pressure and maintain it for a preset time window. In the second stage, at a preset lag time after the pressure probe pulse command is initiated, a flow surge pulse command is generated to drive the alkaline circulating pump to increase its speed and generate an impact flow velocity. In the third stage, after the flow surge pulse command has been continuously used for a preset cleaning time, the pressure drop pulse command and the flow surge pulse command are canceled, and the system pressure and alkali flow rate are driven to return to the steady-state set value corresponding to the current current density.

8. The oxygen-hydrogen synergistic regulation system for alkaline water electrolysis hydrogen production according to claim 1, characterized in that, The pressure regulating unit includes an oxygen-side back pressure regulating valve installed on the gas outlet pipeline of the oxygen-side gas-liquid separator, and a hydrogen-side back pressure regulating valve installed on the gas outlet pipeline of the hydrogen-side gas-liquid separator; the thermal management unit includes a heat exchanger and a temperature regulating valve installed on the bypass or cooling medium pipeline of the heat exchanger.

9. The oxygen-hydrogen synergistic regulation system for alkaline water electrolysis hydrogen production according to claim 1, characterized in that, The sensing and monitoring unit includes a transmembrane differential pressure transmitter. The high-pressure end of the transmembrane differential pressure transmitter is connected to the gas outlet of the hydrogen-side gas-liquid separator, and the low-pressure end is connected to the gas outlet of the oxygen-side gas-liquid separator. The multiphysics coupling controller is internally configured with a PID closed-loop control loop. The real-time differential pressure signal output by the transmembrane differential pressure transmitter is connected to the PID closed-loop control loop, and the feedforward compensation signal is superimposed on the output of the PID closed-loop control loop as an offset.

10. A method for synergistic regulation of oxygen and hydrogen in an alkaline water electrolysis hydrogen production system, characterized in that, The method is based on a multiphysics coupling controller and includes the following steps: The data acquisition module reads current density, alkali temperature, system pressure, and alkali flow rate data. Based on the physical mechanisms of Fick's first law and Henry's law, the flux calculation module calculates the dissolved hydrogen migration flux index using the alkaline solution temperature and the system pressure. The dissolved hydrogen migration flux index is compared with a preset safe flux threshold by the collaborative instruction generation module; When the dissolved hydrogen migration flux index exceeds the safe flux threshold, a coordinated control command is generated, which includes reducing system pressure, reducing alkali temperature, or adjusting alkali circulation flow rate. The viscosity mapping compensation module calculates the expected dynamic viscosity of the alkaline solution based on the target temperature, and calculates the expected change in flow resistance of the internal flow channel of the electrolyzer in combination with the alkaline solution flow rate, thereby generating a feedforward compensation signal. After superimposing the coordinated control command and the feedforward compensation signal, the actuator of the alkaline water electrolysis hydrogen production system is driven, thereby suppressing hydrogen transmembrane migration while maintaining stable transmembrane pressure difference.

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