Control method, device and equipment of alkaline water electrolysis hydrogen production system and medium

Abstract

The embodiment of the invention provides a control method, device and equipment for an alkaline water electrolysis hydrogen production system and a medium. The control method comprises the steps that system parameters and system instructions of the alkaline water electrolysis hydrogen production system are obtained; determining the current working condition of the alkaline water electrolysis hydrogen production system according to the system parameters and the system instructions; determining a corresponding control scheme according to the current working condition, and executing the control scheme under the current working condition; when the control scheme is executed, the Faraday efficiency of the alkaline water electrolysis hydrogen production system is determined according to the current density and the hydrogen production amount; if the Faraday efficiency is larger than or equal to the preset efficiency, whether the hydrogen content in oxygen, the system pressure, the system temperature and the system liquid level exceed preset safety parameter threshold values or not is judged; and if the hydrogen content in the oxygen, the system pressure, the system temperature and / or the system liquid level exceed the preset safety parameter threshold values, a preset safety scheme is triggered to be executed. According to the embodiment of the invention, a systematic technical support is provided for engineering application of the alkaline water electrolysis hydrogen production system in a fluctuating power supply scene.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of electrochemical hydrogen production and process control, in particular to a control method and device of an alkaline water electrolysis hydrogen production system, an electronic device and a storage medium. BACKGROUND

[0002] As a mature industrial hydrogen production process, alkaline water electrolysis hydrogen production technology has been widely used in traditional industries such as ammonia synthesis and oil refining for a long time. The alkaline electrolytic tank of a typical alkaline water electrolysis hydrogen production system operates at a temperature of 40-80℃, and the current density is about 0.25A / cm 2 , which has the advantages of high process maturity, long operation life and relatively low hydrogen production cost, so it has a good application basis in large-scale centralized hydrogen production projects. With the rapid expansion of the installed capacity of renewable energy such as wind power and photovoltaic power, water electrolysis driven by fluctuating power is gradually becoming one of the important technologies for building a new power system and hydrogen energy supply system, which can realize peak shaving and valley filling of power and local consumption.

[0003] However, when the alkaline water electrolysis hydrogen production system is directly coupled with fluctuating power sources such as wind power and photovoltaic power, its operating conditions change from the original relative stability to frequent load fluctuations or even rapid start-stop, which exposes a series of technical problems that are not significant under traditional stable power conditions, including that the gas cross safety risk has not been effectively solved, the control mode mainly based on single parameter adjustment is difficult to adapt to the safety and efficient operation requirements in a wide load range under fluctuating power sources, and the energy loss caused by bypass current lacks online evaluation and control means. SUMMARY

[0004] The embodiments of the present application provide a control method of an alkaline water electrolysis hydrogen production system to solve or at least partially solve the above problems.

[0005] Correspondingly, the embodiments of the present application also provide a control device of an alkaline water electrolysis hydrogen production system, an electronic device and a storage medium to ensure the implementation and application of the above method.

[0006] In order to solve the above problems, the embodiments of the present application disclose a control method of an alkaline water electrolysis hydrogen production system, the driving power source of the alkaline water electrolysis hydrogen production system includes a fluctuating power source, and the method comprises: obtaining system parameters and system instructions of the alkaline water electrolysis hydrogen production system, the system parameters at least including current density, system pressure, system temperature, system liquid level, hydrogen production amount, and hydrogen content in oxygen; determining the current operating condition of the alkaline water electrolysis hydrogen production system according to the system parameters and the system instructions; determine a corresponding control scheme according to the current working condition, and execute the control scheme under the current working condition to control the alkaline water electrolysis hydrogen production system; In the execution of the control scheme, a Faraday efficiency of the alkaline water electrolysis hydrogen production system is determined according to the current density and the hydrogen production amount; If the Faraday efficiency is greater than or equal to a preset efficiency, it is determined whether the hydrogen content in the oxygen, the system pressure, the system temperature and the system liquid level exceed preset safety parameter thresholds; If the hydrogen content in the oxygen, the system pressure, the system temperature and / or the system liquid level exceed the preset safety parameter thresholds, a preset safety scheme is triggered to be executed to control the alkaline water electrolysis hydrogen production system.

[0007] The embodiments of the present application also disclose a control device of an alkaline water electrolysis hydrogen production system, a driving power supply of the alkaline water electrolysis hydrogen production system comprising a fluctuating power supply, and the device comprising: A parameter acquisition module is configured to acquire system parameters and system instructions of the alkaline water electrolysis hydrogen production system, wherein the system parameters at least include a current density, a system pressure, a system temperature, a system liquid level, a hydrogen production amount and a hydrogen content in oxygen; A working condition determination module is configured to determine a current working condition of the alkaline water electrolysis hydrogen production system according to the system parameters and the system instructions; A system control module is configured to determine a corresponding control scheme according to the current working condition, and execute the control scheme under the current working condition to control the alkaline water electrolysis hydrogen production system; An efficiency determination module is configured to determine a Faraday efficiency of the alkaline water electrolysis hydrogen production system according to the current density and the hydrogen production amount in the execution of the control scheme; A safety confirmation module is configured to determine whether the hydrogen content in the oxygen, the system pressure, the system temperature and the caustic liquid level exceed preset safety parameter thresholds if the Faraday efficiency is greater than or equal to a preset efficiency; A safety control module is configured to trigger a preset safety scheme to be executed to control the alkaline water electrolysis hydrogen production system if the hydrogen content in the oxygen, the system pressure, the system temperature and / or the caustic liquid level exceed the preset safety parameter thresholds.

[0008] The embodiments of the present application also disclose an electronic device, comprising a processor and a memory having executable codes stored thereon, wherein the executable codes, when executed, cause the processor to perform the control method of the alkaline water electrolysis hydrogen production system according to one or more of the embodiments of the present application.

[0009] The application also discloses a machine readable medium having executable codes stored thereon, which, when executed, cause a processor to perform the control method of the alkaline water electrolysis hydrogen production system.

[0010] Compared with the prior art, the application has the following advantages: In the application, system parameters and system instructions of the alkaline water electrolysis hydrogen production system are acquired, the system parameters at least including current density, system pressure, system temperature, system liquid level, hydrogen production amount, and hydrogen content in oxygen; the current working condition of the alkaline water electrolysis hydrogen production system is determined according to the system parameters and the system instructions; a corresponding control scheme is determined according to the current working condition, and the control scheme is executed under the current working condition to control the alkaline water electrolysis hydrogen production system; when the control scheme is executed, the Faraday efficiency of the alkaline water electrolysis hydrogen production system is determined according to the current density and the hydrogen production amount; if the Faraday efficiency is greater than or equal to a preset efficiency, it is determined whether the hydrogen content in oxygen, the system pressure, the system temperature, and the system liquid level exceed a preset safety parameter threshold; if the hydrogen content in oxygen, the system pressure, the system temperature, and / or the system liquid level exceed the preset safety parameter threshold, a preset safety scheme is triggered to be executed to control the alkaline water electrolysis hydrogen production system.

[0011] The application integrates the key parameters such as the current density, the system pressure, the system temperature, the system liquid level, the hydrogen production amount, and the hydrogen content in oxygen into a unified control framework, realizes safe, stable, and efficient operation of the alkaline water electrolysis hydrogen production system under fluctuating power sources such as wind power and photovoltaic power, and solves the problem that the traditional control mode mainly based on single-parameter adjustment cannot adapt to the safe and efficient operation demand in a wide load range under fluctuating power sources. The application also introduces online evaluation of the Faraday efficiency into the control system, so that the invalid energy consumption that is difficult to detect is quantified and visualized. The application also constructs a safety boundary control mechanism around the hydrogen content in oxygen, the system pressure, the system temperature, and the system liquid level, so that the hydrogen content in oxygen, the system pressure, the system temperature, and the system liquid level can be stably controlled below the preset safety parameter threshold in the whole working condition range, and the safety risk caused by the hydrogen content in oxygen, the system pressure, the system temperature, and the system liquid level exceeding the preset safety parameter threshold is avoided.

[0012] Overall, the application comprehensively considers multiple targets such as safety, energy efficiency, and service life on the basis of realizing the "monitoring-determining-adjusting" closed-loop control, adapts to complex operating conditions under fluctuating power sources, provides systematic technical support for engineering application of the alkaline water electrolysis hydrogen production system in fluctuating power source scenes such as wind power and photovoltaic power, and has good popularization value and application prospect. BRIEF DESCRIPTION OF DRAWINGS

[0013] Figure 1is a step flow chart of a control method embodiment of an alkaline water electrolysis hydrogen production system of the present application; Figure 2 is a structural schematic diagram of an alkaline water electrolysis hydrogen production system of a control method embodiment of an alkaline water electrolysis hydrogen production system of the present application; Figure 3 is a parameter change diagram of each part of the electrolytic cell in the starting process of a control method embodiment of an alkaline water electrolysis hydrogen production system of the present application; Figure 4 is a diagram of different parameters changing with system pressure of a control method embodiment of an alkaline water electrolysis hydrogen production system of the present application; Figure 5 is a characteristic region division schematic diagram of alkaline solution flow-rate-system load-oxygen hydrogen content of a control method embodiment of an alkaline water electrolysis hydrogen production system of the present application; Figure 6 is a control flow chart of a control method embodiment of an alkaline water electrolysis hydrogen production system of the present application; Figure 7 is a structural block diagram of a control device embodiment of an alkaline water electrolysis hydrogen production system of the present application; Figure 8 is a structural schematic diagram of the device provided in an embodiment of the present application. DETAILED DESCRIPTION

[0014] In order to make the above-mentioned purposes, features and advantages of the present application more obvious and easy to understand, the present application will be further described in detail below in combination with the drawings and specific embodiments.

[0015] As a mature industrial hydrogen production process, alkaline water electrolysis hydrogen production technology has been widely used in traditional industries such as synthetic ammonia and oil refining for a long time. A typical alkaline electrolytic cell operates at a temperature of 40-80℃, with a current density of about 0.25A / cm 2 , high process maturity, long operation life and relatively low hydrogen production cost, so it has a good application basis in large-scale centralized hydrogen production projects. With the rapid growth of installed capacity of renewable energy such as wind power and photovoltaic power, water electrolysis driven by fluctuating power to realize peak shaving and local consumption has gradually become one of the important technical routes for building a new power system and hydrogen energy supply system.

[0016] However, when directly coupled with fluctuating power sources such as wind power and photovoltaic power, the operation condition of the alkaline water electrolysis system changes from the original relatively stable condition to frequent load fluctuations or even rapid start-stop, exposing a series of technical problems that are not prominent under the condition of traditional stable power sources. First, during the low load and start-stop stage, the cross phenomenon of hydrogen and oxygen gas in the alkaline water electrolysis system is significantly intensified, and the hydrogen content in oxygen is close to the chain value of 2%, even approaching the risk of 4% explosion limit. In order to ensure safety, the alkaline electrolyzer load is generally controlled in the range of 20% to 100% of the rated power in engineering applications, resulting in the inability to effectively utilize part of the renewable power.

[0017] Secondly, due to the large volume and heat capacity of the alkaline electrolyzer, its cold start process mainly relies on the heat generated by the electrolysis reaction and the heating device. The traditional constant current method from room temperature to 80°C often takes nearly 1 hour. During this process, if the electrode catalyst layer is in a low-temperature high-potential state for a long time, irreversible deactivation may occur, causing a decrease in electrode performance and service life. Although the "room temperature to 95°C and 100% load" time can be shortened to about 60 minutes through the step-by-step current increase (step-by-step pressure increase) strategy, the current engineering site generally lacks a system control scheme that can program, standardize, and repeatedly execute this type of start-stop strategy.

[0018] Thirdly, the existing industrial devices mostly use single regulation modes such as constant current or constant voltage, supplemented by basic temperature, pressure, and liquid level control. This type of control method can meet the basic operation requirements under stable power conditions, but in the context of fluctuating power sources such as wind power and photovoltaic power, it is difficult to balance multiple objectives such as safety boundaries (e.g., hydrogen content control in oxygen), energy consumption levels (e.g., cell voltage and Faraday efficiency), and device life (electrode corrosion, fatigue, and damage caused by frequent start-stop) due to the regulation of only a single variable. Moreover, there is a lack of systematic and coordinated optimization strategies for the entire process of load fluctuations.

[0019] In addition, the hidden energy consumption problem caused by bypass current is particularly prominent in high-power systems. Test results show that in a 250 kW alkaline electrolysis system, the energy loss caused by bypass current accounts for about 3.1% of the total energy consumption of the system, corresponding to about 8.6 kW power. Although increasing the current density helps to improve the Faraday efficiency, the existing systems generally lack mechanisms for online calculation of Faraday efficiency, identification of bypass current, and feedback of bypass current to the operation control strategy, making it difficult to timely perceive and effectively suppress the bypass current, which is an energy consumption "black box".

[0020] In summary, under the application background of coupling fluctuating power sources such as wind power and photovoltaic power, the existing alkaline water electrolysis hydrogen production system still has problems such as gas cross safety risk at low load and start-stop stage, long cold start time and easy damage to the electrode. The existing control mode mainly based on single parameter adjustment cannot adapt to the safe and efficient operation requirements in a wide load range, and lacks online evaluation and control means for energy loss caused by bypass current. Therefore, it is urgent to propose a multi-parameter collaborative optimization operation control method for alkaline water electrolysis hydrogen production system, which comprehensively considers safety, energy efficiency and service life and other multiple objectives on the basis of realizing the "monitoring-judgment-adjustment" closed-loop control, to adapt to the complex operating conditions under the driving of fluctuating power sources.

[0021] Therefore, in order to solve the problems of large gas cross safety risk, slow cold start process and easy damage to the electrode, limited load adaptation range and high energy consumption level of the alkaline water electrolysis hydrogen production system under the driving of fluctuating power sources such as wind power and photovoltaic power, the embodiment of the present application proposes a multi-parameter collaborative optimization operation control method. Through comprehensive monitoring and linkage adjustment of current density, alkali flow, system pressure, system temperature, start-stop process, safety threshold (especially hydrogen content in oxygen) and bypass current, the overall optimization of system operation state is realized under multiple conditions and multiple target constraints.

[0022] In some embodiments, the embodiment of the present application controls the hydrogen content in oxygen through fine control in the full operating range, so that it is always lower than the preset safety threshold, for example, to ensure that the chain value is lower than about 2%, and to avoid approaching the lower limit of explosion of about 4%, thereby significantly reducing the safety risk caused by gas cross. In other embodiments, by optimizing the current rise and fall strategy and the collaborative control of system temperature, system pressure and alkali flow during the cold start and start-stop process, the start-up time from room temperature to stable operating state is shortened, and the duration of low-temperature high-potential operating state is reduced, thereby reducing the irreversible damage to the electrode catalyst layer and prolonging the service life of the electrode. In terms of energy efficiency, the embodiment of the present application dynamically couples the settings of alkali flow, system pressure and system temperature with current density, so that the electrolytic cell can maintain a lower cell voltage and a higher hydrogen production efficiency as much as possible in a wide load range of 20% to 100% of the rated power, thereby improving the adaptability of the system to external power fluctuations. At the same time, a method of comparing the predicted hydrogen production amount based on Faraday's law with the actual hydrogen production amount is introduced to evaluate the Faraday efficiency and the proportion of bypass current in real time, and to use it as an important feedback signal for operation optimization to identify and suppress the invalid energy loss caused by bypass current.

[0023] Through the above-mentioned multi-parameter cooperative optimization, the application finally forms a set of "monitoring-determining-regulating" closed-loop automatic operation control method, so that the alkaline water electrolysis hydrogen production system can still realize safe and controllable, rapid response, high energy efficiency and equipment life-friendly operation under fluctuating power conditions, and provides an engineering-promotable control technical solution for large-scale renewable energy hydrogen production.

[0024] Referring to Figure 1 is a step flow chart of an embodiment of a control method of an alkaline water electrolysis hydrogen production system of the application, comprising the following steps: Step 101, obtaining system parameters and system instructions of the alkaline water electrolysis hydrogen production system, wherein the system parameters at least include current density, system pressure, system temperature, system liquid level, hydrogen production amount, and hydrogen content in oxygen.

[0025] In an alternative embodiment, the control method of an alkaline water electrolysis hydrogen production system shown in the embodiment of the application is applicable to alkaline water electrolysis hydrogen production systems with a scale of two standard sides (about 2Nm 3 / h) and larger, and the driving power source of the alkaline water electrolysis hydrogen production system includes fluctuating power sources such as wind power and photovoltaic power. The alkaline water electrolysis hydrogen production system applicable to the control method of an alkaline water electrolysis hydrogen production system shown in the embodiment of the application uses alkaline aqueous solution as electrolyte, preferably KOH solution with a mass fraction of 25-35wt%, more preferably about 30wt% KOH solution, and the typical working temperature is 60-95℃, and the applicable current density range is 2000-5500A / m 2 .

[0026] Specifically, the structure of the alkaline water electrolysis hydrogen production system can refer to Figure 2 , Figure 2 is a structural schematic diagram of an alkaline water electrolysis hydrogen production system of an embodiment of a control method of an alkaline water electrolysis hydrogen production system of the application.

[0027] The alkaline water electrolysis hydrogen production system mainly comprises a power rectifier system, an alkaline electrolytic cell system, an alkali solution circulation and water replenishment system, a gas-liquid separation and gas treatment system, an inert gas purging system, and a control and monitoring system.

[0028] Among them, the alkaline electrolytic cell system comprises an electrolytic cell main body composed of an end plate, a bipolar plate, an electrode, a diaphragm and a plurality of small chambers, for completing the alkaline water electrolysis reaction and forming a plurality of small chamber units in series.

[0029] The alkali liquor circulation and water replenishment system comprises an alkali liquor circulation system and a water replenishment system, realizes circulation delivery and heat exchange of electrolyte, and ensures that the electrolyte flow and temperature in the electrolytic cell are in a suitable range. The alkali liquor circulation system is composed of an alkali liquor tank, an alkali liquor circulation pump, a filter, a plate heat exchanger (or an alkali liquor cooler) and the like, and is used for maintaining circulation flow and heat exchange of the electrolyte in the electrolytic cell and the external loop. The water replenishment system is provided with a pure water replenishment tank, a water replenishment pump and a sampling and concentration detection interface, and is used for replenishing water consumption in the electrolysis process and maintaining stable electrolyte concentration.

[0030] The gas-liquid separation and gas treatment system is provided with a hydrogen and oxygen gas-liquid separator, a drop catcher, a cooling dryer, a hydrogen purification device and a hydrogen storage tank, so as to separate the generated gas from the electrolyte, realize demisting and cooling and purification, and send the dried and purified hydrogen into the hydrogen storage tank or an external hydrogen supply interface, and the oxygen is discharged or recycled through a special pipeline.

[0031] The inert gas purging system is composed of a nitrogen cylinder set, a pressure reducing valve and a purging pipeline, and is used for filling nitrogen into the electrolytic cell and related pipelines through a special purging pipeline under start-up, shutdown and abnormal conditions, replacing the inert gas in the electrolytic cell and pipelines, reducing the risk of gas cross and explosion, and realizing air replacement before cold start and safe inertization under shutdown and abnormal conditions.

[0032] The power rectification system comprises a transformer and a rectification power supply, provides adjustable direct current and voltage for the electrolytic cell, and realizes accurate control of the current density and system load.

[0033] The control and monitoring system takes a PLC (Programmable Logic Controller) or a DCS (Distributed Control System) as the core, collects key signals such as system pressure, system temperature, alkali liquor and gas flow, system liquid level (including gas-liquid separator and cell liquid level), gas composition (including hydrogen content in oxygen and oxygen content in hydrogen) and electrical parameters in real time through field arranged pressure transmitters, temperature sensors, flowmeters, liquid level meters / differential pressure transmitters, online gas analyzers and voltage / current detection modules, and uploads the data to an upper computer or a monitoring and energy consumption analysis system for recording and visualization. The PLC sends control signals to the alkali liquor circulation pump, the pressure regulating valve, the exhaust valve, the cooling water regulating valve and the rectification power supply and the like according to the monitoring data and operating conditions, completes the coordinated adjustment of parameters such as current density, alkali liquor flow, system pressure and system temperature, and realizes safe, stable and efficient operation of the alkaline water electrolysis hydrogen production system under different operating conditions.

[0034] Specifically, the control and monitoring system can cooperate with the industrial computer, various sensors and actuators to form a complete automatic control unit. The system liquid level control measures the liquid level and pressure difference in real time through the differential pressure transmitter installed on the gas-liquid separator, and drives the water supply valve and exhaust valve to act, so as to maintain the liquid level of the separator within the set range and keep the liquid level balance on both sides; the system pressure control detects the system pressure through the pressure transmitter on the hydrogen branch, and links the hydrogen side pressure regulating valve and the exhaust valve to realize the closed-loop regulation of the system pressure; the system temperature control obtains temperature information through the temperature sensor arranged on the electrolytic cell and the alkali pipeline, and comprehensively adjusts the opening degree of the cooling water regulating valve of the heat tracing device and the alkali cooler, so as to keep the temperature of the electrolytic cell and the alkali within the target interval; the water supply control triggers the start and stop of the water supply pump by the liquid level signal, so as to ensure the relative stability of the electrolyte liquid level and concentration; the current and voltage control unit executes the constant current, constant voltage or segmented variable current operation mode according to the upper computer or external power instruction, and forms the current density curve matched with the load instruction; the gas composition monitoring unit measures the hydrogen content in oxygen and the oxygen content in hydrogen in real time through the online gas analyzer, and provides key feedback signals for gas cross, safety interlocking and multi-parameter collaborative optimization.

[0035] By Figure 2 According to the structural configuration shown in the figure, the alkaline water electrolysis hydrogen production system in the embodiment of the application realizes the integrated configuration of the electrolysis reaction unit, the fluid transportation unit, the gas separation and treatment unit, the power supply unit and the control unit at the hardware level, so that the current density, the alkali flow, the system pressure, the system temperature, the start-stop program and the bypass current and other key operating parameters can be measured and adjusted, which lays a system foundation for the implementation of the subsequent multi-parameter collaborative optimization operation control method.

[0036] In step 101 of the embodiment of the application, by monitoring the alkaline water electrolysis hydrogen production system, the system parameters and system instructions of the alkaline water electrolysis hydrogen production system are obtained, the system parameters at least including the current density, the system pressure, the system temperature, the system liquid level, the hydrogen production amount, the hydrogen content in oxygen, and the system instructions can include external power instructions, start-stop instructions and other instructions.

[0037] In one embodiment, based on Figure 2 As shown in the alkaline water electrolysis hydrogen production system, a set of operating parameter monitoring system can be established around the electrolytic cell body and its supporting BOP (Balance Of Plant, balance system) equipment. The operating parameter monitoring system covers not only the electrical quantity and thermal parameter related to the reaction itself, but also the gas composition, flow and liquid level parameters affecting the safety boundary and energy efficiency level, and on this basis, several evaluation indexes obtained by calculation are introduced, to provide continuous and reliable data support for multi-parameter collaborative optimization control.

[0038] For the operation parameter monitoring system, first, on the electrical side, the operation parameter monitoring system can focus on monitoring the electrolytic cell working current and electrolytic voltage, and converting them into normalized indicators such as current density and cell voltage. The current density is usually controlled in the range of about 1500-5500 A / m 2 , which is converted by the output current of the rectifier power supply and the effective electrode area, and combined with the number of cells to obtain the working state of the single cell and the whole tank. The electrolytic voltage is reflected by the tank voltage and the sampled cell voltage, which is used to evaluate the polarization degree and energy consumption level. The above electrical parameters are collected at a high sampling frequency, and are recorded together with the load instruction, system working condition identifier, to provide a basis for subsequent load tracking, start-stop strategy execution and bypass current diagnosis.

[0039] In terms of fluid and thermal parameters, the operation parameter monitoring system can continuously monitor the electrolytic tank temperature in the alkali solution flow, system pressure and system temperature. The alkali solution flow is obtained by installing a flow meter on the circulating loop, and the typical operating interval is 150-250 L / h, which directly affects the mass transfer conditions, cell voltage and gas cross. The system pressure is measured by a pressure transmitter on the hydrogen side or the common header, and is preferably controlled at about 0.4 MPa, and when it fluctuates within a certain range, the electrolytic efficiency, gas-liquid separation effect and equipment mechanical strength can be considered. The electrolytic tank temperature is set at multiple temperature sensing points in the middle and inlet and outlet pipelines of the electrolytic tank, forming a comprehensive representation of the temperature distribution of the electrolytic cavity, and the working range is generally 30-95℃, and normal operation is more focused on maintaining in the high-efficiency interval of 80-95℃. Through the joint monitoring of flow, pressure and temperature, the reaction heat balance, mass transfer condition and cooling capacity can be reflected in real time, and a basis is provided for the coordinated regulation between "temperature-pressure-flow-load" in the control strategy.

[0040] Gas quality and safety-related parameters are another focus of the operation parameter monitoring system of the present application. The operation parameter monitoring system is arranged with an online gas analyzer in the hydrogen branch (the hydrogen branch usually includes a hydrogen cooler, a hydrogen scrubber and a hydrogen separator) and the oxygen branch (the oxygen branch usually includes an oxygen cooler, an oxygen scrubber and an oxygen separator), which detects the hydrogen content in oxygen and the oxygen content in hydrogen in real time, and pays special attention to the change of the hydrogen volume fraction in oxygen. The hydrogen content in oxygen is not only used to judge the gas cross situation in the diaphragm and pipeline, but also directly related to the explosion risk and safety interlock threshold. Some embodiments of the present application continuously collect gas composition data and perform correlation analysis with parameters such as current density, alkali solution flow and system pressure to dynamically depict the gas cross behavior under different working conditions, and provide a basis for safety control in low-load operation, load rising and falling process and start-stop process.

[0041] In addition, in order to accurately grasp the material balance, a flowmeter can be arranged at the hydrogen outlet to measure the hydrogen production (i.e., hydrogen production) online, and if necessary, a flow measuring device can also be arranged on the oxygen side. The gas-liquid separator and the liquid tank are provided with liquid level or differential pressure transmitters for monitoring the change of the system liquid level, judging whether the electrolyte is at a reasonable working height, and providing signals for water replenishment control and abnormal leakage diagnosis. By combining the flow and liquid level parameters, conditions such as gas path blockage, liquid level imbalance or abnormal discharge can be found in time.

[0042] On this basis, some embodiments of the embodiments of the present application also introduce several comprehensive evaluation parameters obtained by online calculation. The control alkaline water electrolysis hydrogen production system calculates the theoretical hydrogen production according to Faraday's law according to the real-time current, electrode area and cell number, and compares it with the actual hydrogen production measured by the hydrogen flowmeter to obtain the key indicator of Faraday efficiency. The change of Faraday efficiency not only reflects the degree of current utilization, but also can be used to identify hidden problems such as bypass current and micro-leakage. When the Faraday efficiency is monitored for a long time to be low or deviate from the normal characteristic curve, it can be determined that there is a large bypass current or the operating point is not reasonably selected, thereby triggering the corresponding energy efficiency optimization and operation adjustment.

[0043] All the above monitoring data are accessed to PLC or DCS through field bus or industrial Ethernet, and then unified collected, stored and visualized by upper computer or energy consumption monitoring platform. The alkaline water electrolysis hydrogen production system can segmentally mark and statistically analyze the data according to time, working condition or load instruction, and establish characteristic data sets for cold start process, steady state running stage and load reduction and shutdown stage. Through this running parameter monitoring system, the key running parameters of the alkaline water electrolysis hydrogen production system are comprehensively perceived, which provides reliable data basis and judgment basis for subsequent working condition identification, multi-parameter collaborative optimization control and safety interlocking.

[0044] Optionally, the step 101 specifically comprises: obtaining initial system parameters of the alkaline water electrolysis hydrogen production system; performing filtering processing and denoising processing on the initial system parameters to obtain intermediate system parameters; determining to-be-processed parameters in the intermediate system parameters, the to-be-processed parameters including intermediate system parameters exceeding a preset boundary threshold and intermediate system parameters with missing signals; performing marking processing and / or fault-tolerant processing on the to-be-processed parameters in the intermediate system parameters to obtain system parameters of the alkaline water electrolysis hydrogen production system.

[0045] After obtaining the initial system parameters of the alkaline water electrolysis hydrogen production system, the embodiments of the present application need to perform a series of pretreatments to obtain the system parameters of the alkaline water electrolysis hydrogen production system.

[0046] Specifically, the alkaline water electrolysis hydrogen production system can continuously collect current, voltage, current density, cell voltage, alkali flow, system pressure, system temperature, system liquid level (such as gas-liquid separator liquid level), hydrogen and oxygen flow, hydrogen production, and gas composition parameters such as hydrogen in oxygen and oxygen in hydrogen as initial system parameters of the alkaline water electrolysis hydrogen production system, and write them into a time series database with a unified timestamp.

[0047] The initial system parameters of the alkaline water electrolysis hydrogen production system are reasonably filtered and denoised to obtain intermediate system parameters, and intermediate system parameters exceeding the preset boundary threshold (i.e., obviously exceeding the limit) and signal missing intermediate system parameters are determined, so that the intermediate system parameters exceeding the preset boundary threshold and the signal missing intermediate system parameters are marked and / or fault-tolerant processed to obtain the system parameters of the alkaline water electrolysis hydrogen production system.

[0048] The embodiments of the present application obtain the system parameters of the alkaline water electrolysis hydrogen production system by preprocessing the initial system parameters, reduce the interference of measurement noise on the control algorithm under the premise of ensuring data authenticity, and thus obtain a set of continuous and reliable operation state description to provide a basis for subsequent working condition identification and control decision.

[0049] Step 102, determining the current working condition of the alkaline water electrolysis hydrogen production system according to the system parameters and the system instructions.

[0050] In step 102 of the embodiments of the present application, in the working condition determination link, the current working condition of the alkaline water electrolysis hydrogen production system can be determined according to the system parameters and the system instructions. Specifically, the current working condition of the alkaline water electrolysis hydrogen production system can be divided into several categories such as cold start working condition, steady state running working condition, load increasing working condition, load decreasing working condition, shutdown working condition, and inert gas purging and safety disposal working condition, by comprehensively analyzing the current density change trend, electrolytic cell temperature, system pressure, external power instruction and the state of start-stop instruction. The working condition determination not only depends on the instantaneous value, but also pays attention to the change trend of the parameter with time, and combines the preset threshold and hysteresis interval to avoid frequent switching between different working conditions, so that the switching of the control strategy is smoother and more predictable.

[0051] Step 103, determining a corresponding control scheme according to the current working condition, and executing the control scheme under the current working condition to control the alkaline water electrolysis hydrogen production system.

[0052] In step 103 of the embodiments of the present application, according to the determined current working condition of the alkaline water electrolysis hydrogen production system, the control scheme corresponding to the current working condition is obtained, and the control scheme is executed under the current working condition to control the alkaline water electrolysis hydrogen production system.

[0053] Step 104, when executing the control scheme, determining the Faraday efficiency of the alkaline water electrolysis hydrogen production system according to the current density and the hydrogen production amount.

[0054] In the alkaline water electrolysis hydrogen production system, the bypass current is a kind of invalid current which does not directly participate in the effective electrolysis reaction but continuously consumes electric energy, and its existence will reduce the Faraday efficiency and increase the unit hydrogen production energy consumption. Test analysis shows that in a 250 kW level alkaline electrolysis system, the energy loss caused by the bypass current accounts for about 3% of the total power consumption of the system, corresponding to about 8-9 kW. This part of the loss is often difficult to be detected in time under the traditional operation mode, and can only be indirectly reflected by the long-term high energy consumption. Therefore, the online evaluation of the bypass current is organically embedded in the control system of the operation optimization in the embodiments of the present application, so that it is changed from "invisible loss" to "observable and controllable" operation parameters.

[0055] In step 104 of the embodiments of the present application, the bypass current is quantitatively characterized by the calculation of the Faraday efficiency, and when the control scheme is executed, the Faraday efficiency of the alkaline water electrolysis hydrogen production system is determined according to the current density and the hydrogen production amount (i.e. the actual hydrogen production amount measured by the hydrogen flow meter).

[0056] Specifically, according to the real-time collected current density, electrode effective area and electrolysis cell number, the theoretical hydrogen production amount is calculated by using the Faraday law, and then compared with the actual hydrogen production amount measured by the hydrogen flow meter to obtain the Faraday efficiency at the current time. The calculation process of the Faraday efficiency and the bypass current is as follows formula (1) and formula (2): (1) (2) Wherein, is the theoretical hydrogen production amount, is the average hydrogen production amount measured by the hydrogen flow meter, is the real-time calculated Faraday efficiency, I is the current density (A / m 2 ), S is the single cell electrode area (m 2 ), n is the number of cells, and F is the Faraday constant.

[0057] Wherein, the closer the Faraday efficiency is to 100%, the more current is used for effective water decomposition reaction; otherwise, it means that there is a certain proportion of bypass current or other invalid consumption. By continuously recording and trend analysis of this index, the typical efficiency characteristic curve of the system under different load levels and different working conditions can be identified, and whether the current operating point is in a reasonable interval can be judged accordingly. On this basis, the Faraday efficiency is no longer used only for post-evaluation, but is directly used as a feedback quantity for operation optimization.

[0058] In some embodiments, the online evaluation of bypass current not only serves real-time control, but also provides data support for optimization of device structure and maintenance strategy. The control system stores and statistically analyzes the current, voltage, hydrogen production and Faraday efficiency under different pipeline arrangements, grounding methods or maintenance states through the energy consumption monitoring platform, which can analyze the change law of bypass current under different pipeline arrangements, grounding methods or maintenance states, and provide quantitative basis for subsequent hardware measures such as adding manifold resistance, optimizing electrical connection and reforming local structure. At the same time, by associating these historical data with fault records and maintenance records, the relationship between some efficiency anomalies and diaphragm aging, electrode pollution or leakage hidden danger can be identified, and maintenance warning can be given in advance.

[0059] Step 105, if the Faraday efficiency is greater than or equal to the preset efficiency, whether the hydrogen content in the oxygen, the system pressure, the system temperature and the system liquid level exceed the preset safety parameter threshold value is judged.

[0060] Step 106, if the hydrogen content in the oxygen, the system pressure, the system temperature and / or the system liquid level exceeds the preset safety parameter threshold value, a preset safety scheme is triggered to perform safety control on the alkaline water electrolysis hydrogen production system.

[0061] In steps 105 and 106 of the embodiments of the present application, while the control scheme is being executed, it is also necessary to judge whether various system parameters exceed the preset safety parameter threshold value, so that the safety interlocking logic runs through the entire control process and has a higher priority than economic optimization. Specifically, in the control process, if the Faraday efficiency is greater than or equal to the preset efficiency, whether the hydrogen content in the oxygen, the system pressure, the system temperature and the system liquid level exceed the preset safety parameter threshold value is judged, and if the hydrogen content in the oxygen, the system pressure, the system temperature and / or the system liquid level exceeds the preset safety parameter threshold value, for example, when the hydrogen content in the oxygen approaches or exceeds the safety threshold value, or the key parameters such as system pressure, system temperature and system liquid level reach the interlocking setting value, a preset safety scheme is triggered to perform safety control on the alkaline water electrolysis hydrogen production system.

[0062] In one embodiment, if the hydrogen content in the oxygen, the system pressure, the system temperature and / or the system liquid level exceeds the preset safety parameter threshold value, the control system will immediately inhibit the system load from rising, and if necessary, will forcibly execute measures such as rapid load reduction, opening of inert gas purge, closing of external output valve and implementation of emergency shutdown. During the safety interlocking triggering period, all optimization adjustments related to energy efficiency give way to safety handling, and only after the gas composition and working condition parameters return to the safety interval, the system is allowed to gradually recover to the normal operating state according to the predetermined logic.

[0063] The embodiments of the present application realize safe, stable and efficient operation of the alkaline water electrolysis hydrogen production system under fluctuating power sources such as wind power and photovoltaic power by including key parameters such as current density, system pressure, system temperature, system liquid level, hydrogen production amount and hydrogen content in oxygen into a unified control framework, solving the problem that the traditional control mode mainly based on single parameter adjustment cannot adapt to the safe and efficient operation demand in a wide load range under fluctuating power sources. The embodiments of the present application also introduce online evaluation of Faraday efficiency into the control system, so that the invalid energy consumption that is difficult to detect is quantified and visualized. The embodiments of the present application also construct a safety boundary control mechanism around the hydrogen content in oxygen, system pressure, system temperature and system liquid level, so that the hydrogen content in oxygen, system pressure, system temperature and system liquid level can be stably controlled below the preset safety parameter threshold in the whole working condition range, avoiding the safety risk caused by the hydrogen content in oxygen, system pressure, system temperature and system liquid level exceeding the preset safety parameter threshold.

[0064] Overall, on the basis of realizing the "monitoring-judgment-regulation" closed-loop control, the embodiments of the present application comprehensively consider multiple targets such as safety, energy efficiency and service life to adapt to complex operating conditions under fluctuating power sources, and provide systematic technical support for the engineering application of the alkaline water electrolysis hydrogen production system under fluctuating power sources such as wind power and photovoltaic power, which has good popularization value and application prospect.

[0065] Optionally, the system temperature includes an alkali temperature of alkali in the alkaline water electrolysis hydrogen production system, and the system liquid level includes an alkali liquid level of the alkali, and the determining a corresponding control scheme according to the current working condition and executing the control scheme under the current working condition comprises: if the current working condition is a cold start working condition, a cold start control scheme is acquired; according to the cold start control scheme, a nitrogen purging operation is performed on the alkaline water electrolysis hydrogen production system, and the system liquid level is adjusted to a preset initial liquid level range; the alkali is heated; when the alkali temperature reaches a first start temperature, the current density is raised to a first start density, and the current density is maintained at the first start density within a first time range; when the alkali temperature reaches a second start temperature, the current density is raised from the first start density to a second start density in stages; when the alkali temperature reaches a third start temperature, the current density is raised from the second start density to a third start density according to a preset start slope, and the heating of the alkali is stopped.

[0066] In the embodiments of the present application, the cold start and start-stop processes are considered as the most sensitive operating stages to safety and device life. Traditional alkaline electrolyzers usually adopt constant current mode for cold start, and it takes a long time to raise the temperature from room temperature to the stable operating temperature, and the electrolyzer is in a low-temperature high-potential state for a considerable period of time, which not only has a low start efficiency, but also easily accelerates the irreversible deactivation of the electrode catalyst layer. In the embodiments of the present application, the cold start and start-stop processes are included in the unified process control logic by the coordinated design of nitrogen purging, liquid injection conditions, current density step-up strategy, and load reduction and shutdown process, so as to achieve the comprehensive goals of controlled safety boundary, shortened start time, and reduced electrode damage.

[0067] Specifically, in the cold start stage of the alkaline water electrolysis hydrogen production system, i.e., when the alkaline water electrolysis hydrogen production system is in a cold start working condition, the step-up current and temperature climbing strategy are executed according to the cold start control scheme, and the current density increase rate, target temperature and alkali flow are gradually advanced in a predetermined order.

[0068] Before the cold start, first, the nitrogen purging operation is performed on the alkaline water electrolysis hydrogen production system, and the system liquid level is adjusted to a preset initial liquid level range to create a safe and controllable initial environment for the system. Before starting, the electrolyzer and related pipelines are subjected to multiple rounds of nitrogen circulation purging, usually 2-3 times of pressure circulation, so that the system pressure is repeatedly changed between 0.1-0.2 MPa, to expel the original air and replace the internal space with inert gas and electrolyte, reducing the possibility of explosive atmosphere formed by the mixing of combustible gas and air. At the same time, through liquid level measurement and differential pressure monitoring, it is confirmed that the liquid levels of the hydrogen and oxygen side gas-liquid separators are in the set range, ensuring that the electrolyzer interior and the circulation loop are filled with electrolyte, laying a stable fluid and material foundation for the subsequent power-up and temperature rise and gas production processes.

[0069] The alkali is heated to start the cold start process, which adopts the strategy of step-by-step pressure increase and step-up current, rather than a single constant current mode. Specifically, when the alkali temperature reaches a first start temperature (e.g., above about 30°C) and the alkali liquid level is normal, the current density is quickly increased to a first start density (e.g., about 1000 A / m 2 ), and the current density is maintained at the first start density within a first time range (e.g., 10-15 min), so that the system completes the initial temperature rise and electrode "activation" under relatively mild conditions. Subsequently, under the premise that the cell voltage and voltage do not exceed the limit, the electrolysis reaction heat and heating means are used to raise the alkali temperature to a second start temperature (e.g., about 60-70°C), and the current density is increased from the first start density to a second start density (e.g., about 2000-2500 A / m 2), and during the stepwise promotion, the current density at each stage needs to be stabilized for 10 minutes, and the parameters such as voltage and hydrogen concentration in oxygen are observed to be normal and not to exceed the upper limit, and then the current density is promoted to the next stage. When the temperature of the alkali solution reaches the third starting temperature (for example, about 70°C or higher), the current density is promoted from the second starting density to the third starting density, i.e., the target load (for example, about 5000A / m 2 ) according to a preset starting slope (for example, about 500A / m 2 per 10 min), and the heat tracing device is gradually turned off, and the heating of the alkali solution is stopped, and the temperature is mainly maintained by relying on the spontaneous heat generated by the electrolysis reaction.

[0070] The above cold start control scheme of the embodiment of the present application is not a simple time program in control implementation, but is closely coupled with monitoring quantities such as temperature, pressure and liquid level. The PLC or DCS judges the stage switching condition according to the real-time temperature and liquid level state, and only when the temperature and liquid level of the previous stage reach the preset threshold and no abnormality such as pressure and gas composition occurs, the current promotion process of the next stage is allowed, thereby avoiding the safety hazard caused by blindly increasing the current when the temperature has not caught up. Through this "condition triggered" stage control mode, the cold start process has high repeatability and safety redundancy while maintaining flexibility.

[0071] Compared with the cold start mode in the prior art with a constant current density of 3500A / m 2 , the above segmented current increase mode of the embodiment of the present application can shorten the overall cold start time to about 60 minutes, significantly reduce the duration of the low-temperature high-potential working condition, and reduce the risk of irreversible damage to the electrode material due to excessively high overpotential.

[0072] In an example, the cold start control scheme of the embodiment of the present application is verified by experiment, the current density is increased in stages according to the predetermined strategy, a certain time is maintained at each stage of current density platform, and the cell voltage corresponding to different cells is determined. It can be found that the cell voltage instantaneously rises when the current density jumps, and then gradually falls as the temperature rises, indicating that the gradual pressure increase mode of the embodiment of the present application can complete the cold start current increase process under the premise of controlling the voltage level; the temperature of the electrolytic cell at typical positions (left and right end pressure plates and middle electrode plate) during the cold start process is obtained, and it can be found that under the control of gradual pressure increase and segmented current increase, the overall temperature of the electrolytic cell smoothly rises from room temperature to about 80-95°C, and the temperature change trend of each part is basically consistent, indicating that the cold start gradual pressure increase scheme of the embodiment of the present application can accelerate the cold start temperature rise and create conditions for subsequent full load operation under the premise of ensuring uniform temperature distribution and structural safety.

[0073] In an example, the cold start control scheme of the embodiment of the present application is verified by experiment, and the following results can be obtained: Figure 3The electrolytic cell parameter change diagram in the start-up process of the control method embodiment of the alkaline water electrolysis hydrogen production system of the application is shown.

[0074] Specifically, Figure 3 (a) is the relationship between current density and electrolytic cell temperature with time in the cold start stage, the horizontal coordinate is time, the left vertical coordinate is current density, and the right vertical coordinate is electrolytic cell temperature. It can be seen that the current density (dark line) gradually increases in the form of a predetermined segmented ladder, while the temperature (light line) smoothly rises on each current platform and eventually approaches 90-100℃, indicating that the gradual current increase strategy can control the current climbing pace while continuously increasing the electrolytic cell temperature.

[0075] Figure 3 (b) shows the changes of cell voltage and hydrogen volume fraction in oxygen (H2 / O2) in the same start-up process, the horizontal coordinate is time, the left vertical coordinate is cell voltage, and the right vertical coordinate is hydrogen volume fraction in oxygen. The cell voltage (dark line) shows a short upward surge at each current density jump, and then gradually falls with the increase of temperature; the hydrogen content in oxygen (light line) rapidly rises to a high level at the beginning of the start-up, and then shows a downward trend under the control strategy and tends to be stable, indicating that the start-up control method of the embodiment of the application can gradually reduce the hydrogen content in oxygen from the initial high value to the safe range under the premise of controllable voltage fluctuation, realizing the safety and energy efficiency optimization of the electrolytic cell during the start-up stage.

[0076] In one example, the statistical results of the time required for the electrolytic cell system to rise from 0 load to 100% load at different initial temperatures are obtained by experiment, as shown in Table 1 below. The temperature in the table is the initial temperature of the electrolytic cell and electrolyte before start-up, and the corresponding start-up time is the time required for the electrolytic cell load to rise from 0 to 100% at the initial temperature, where 100% refers to the highest current density that the system can reach under the condition of a cell voltage of 2.0V at that temperature. As can be seen from the data in the table, as the initial temperature increases from 30℃ to 70℃, the start-up time of the system is shortened from about 25min to about 5min, indicating that appropriately increasing the initial start-up temperature can significantly speed up the current rise and grid connection process of the electrolytic cell, which is beneficial to shorten the cold start time and improve the response speed of the system to external power commands.

[0077] Table 1 Time required for the electrolytic cell system to rise from 0 load to 100% load at different initial temperatures

[0078] In an example, the time required for cold start of the electrolyzer system at different caustic flow rates is determined by experiment, as shown in Table 2 below. The caustic flow rate in the table is the set flow rate of the circulation loop during the cold start process, and the corresponding start time is the time required for the electrolyzer load to increase from 0 to 100% under room temperature conditions. As can be seen from the data in the table, when the caustic flow rate is 150 L / min, the cold start time is about 58 min; when the flow rate is increased to 200 L / min and 250 L / min, the start time is increased to about 62 min and 68 min, respectively. The results show that the greater the caustic flow rate, the greater the ability to cool and remove heat, resulting in a relatively slower heating rate of the electrolyzer, thereby prolonging the time required for cold start. This provides a basis for selecting an appropriate caustic flow rate during the cold start phase of the embodiments of the present application, balancing start efficiency and heat transfer safety.

[0079] Table 2 Time required for cold start of electrolyzer system at different caustic flow rates

[0080] The embodiments of the present application systematically and procedurally optimize the cold start process. By implementing multiple rounds of nitrogen purging and liquid level pre-adjustment before starting, and using a cold start strategy of segmented flow increase and gradual pressure increase, the current increase process is coordinated with state variables such as temperature and pressure. This not only shortens the start time from room temperature to stable operating state, but also significantly reduces the running time under low temperature and high voltage conditions, and reduces the irreversible damage to the electrode catalyst layer. In the wind-solar coupling scenario with frequent start and stop, this coordinated control method helps to prolong the service life of the electrode and key components, and improves the reliability of long-term operation of the system.

[0081] Optionally, the system parameters further include caustic flow rate and exhaust volume, and the determining a corresponding control scheme according to the current working condition and executing the control scheme under the current working condition comprises: if the current working condition is a load reduction condition or a shutdown condition, obtaining a load reduction and shutdown control scheme; according to the load reduction and shutdown control scheme, reducing the current density at a first shutdown slope, and monitoring the hydrogen content in the oxygen; when the hydrogen content in the oxygen is greater than or equal to a preset safety content threshold, performing the nitrogen purging operation and reducing the current density at a second shutdown slope, the second shutdown slope being greater than the first shutdown slope; or when the hydrogen content in the oxygen is greater than or equal to a preset safety content threshold, maintaining the current density above a preset density threshold and increasing the caustic flow rate and the exhaust volume to a preset risk handling threshold; when the hydrogen content in the oxygen is reduced to less than the preset safety content threshold, performing a shutdown operation on the alkaline water electrolysis hydrogen production system.

[0082] The embodiments of the present application organically link the load change slope, inert gas purging and alkali liquor circulation processes in the load reduction and shutdown stages of the alkaline water electrolysis hydrogen production system, i.e., the load reduction condition and the shutdown condition of the alkaline water electrolysis hydrogen production system, and unify them into a control strategy to balance safety and equipment protection. The system load refers to the ratio of the real-time power to the rated power, which can be represented by the current density in a one-to-one correspondence.

[0083] Specifically, when the external power instruction decreases or the system needs to be planned to be shut down, it is judged that the current condition of the alkaline water electrolysis hydrogen production system is a load reduction condition or a shutdown condition, and a load reduction and shutdown control scheme is obtained. According to the load reduction and shutdown control scheme, the current density is gradually reduced according to a first shutdown slope, and the hydrogen content in oxygen is continuously monitored.

[0084] Experiments show that when the current density decreases to about 0.15 A / cm 2 , the hydrogen volume fraction in oxygen may approach about 3.43%, which has approached the lower limit of explosion. The embodiments of the present application introduce the concept of "gas cross risk area" accordingly, when the H2 / O2 volume fraction detected by the online gas analyzer reaches or exceeds about 1.8%, the system is considered to enter the risk area, and the simple linear load reduction is no longer allowed, but a more rigorous safety control strategy is forced to be executed. In the gas cross risk area, the control system can select one or a combination of the two disposal paths according to the field demand and equipment configuration.

[0085] The first disposal path is to immediately start inert gas (usually nitrogen) purging when the hydrogen content in oxygen is greater than or equal to a preset safety content threshold (for example, about 1.8%), to fill inert gas into the related pipeline and separator as soon as possible under the condition of maintaining a certain system pressure, and to reduce the current density to zero according to a faster second shutdown slope, so that the combustible gas concentration is rapidly reduced to less than the preset safety content threshold before entering the complete shutdown state, wherein the second shutdown slope is greater than the first shutdown slope.

[0086] The second disposal path is to not reduce the current density to zero in a short time when the hydrogen content in oxygen is greater than or equal to the preset safety content threshold (for example, about 1.8%), but to maintain a current density that is not lower than the safety lower limit, i.e., to maintain a current density that is higher than the preset density threshold, and to moderately increase the alkali liquor flow and the exhaust volume to a preset risk treatment threshold to accelerate the discharge and replacement of the mixed gas, and to complete the final shutdown when the hydrogen content in oxygen obviously falls and is lower than the preset safety content threshold.

[0087] In one embodiment, regardless of the treatment path adopted, the system maintains continuous alkaline circulation for a period of time after shutdown, for example, no less than about 3 hours, so that the electrolyzer and circulation loop gradually cool down and remove residual gas in the liquid flow state, avoiding the risk of subsequent gas precipitation and local accumulation caused by local stagnation or stagnant liquid.

[0088] This application embodiment, through the aforementioned holistic design of the cold start and start-stop processes, establishes a coordinated control relationship among multiple variables such as current density, temperature, pressure, alkaline solution flow rate, and gas composition. This enables the entire system, from "inert gas purging and liquid injection before startup," "segmented current-increasing cold start," to "load reduction and safe shutdown," to operate under a unified control logic. Under fluctuating power supply conditions such as wind power and photovoltaic power, this application embodiment ensures both the efficiency and repeatability of the cold start process while effectively reducing the risk of gas cross-contamination and electrode damage under frequent start-stop conditions, providing a complete process control scheme for the safe, stable, and efficient operation of alkaline water electrolysis hydrogen production systems.

[0089] Optionally, the system parameters further include the cell voltage, and the step of determining the corresponding control scheme based on the current operating condition and executing the control scheme under the current operating condition includes: If the current operating condition is a steady-state operating condition or a load increase operating condition, then obtain the steady-state control scheme; According to the steady-state control scheme, the system pressure is controlled to remain within a stable pressure range, and the system temperature is controlled to remain within a stable temperature range. When the system pressure is maintained within the stable pressure range and the system temperature is maintained within the stable temperature range, the current density is adjusted according to a preset energy consumption optimization algorithm so that the cell voltage is maintained below a preset voltage threshold and the Faraday efficiency is greater than or equal to the preset efficiency.

[0090] System pressure and system temperature (especially electrolyzer temperature) are considered key thermodynamic parameters affecting electrochemical reaction rates, gas dissolution and precipitation behavior, and the degree of gas cross-contamination. Experimental results show that when the system pressure is controlled at approximately 0.4 MPa, the overall performance of the chamber voltage and hydrogen content in oxygen is optimal. Further increasing the pressure to approximately 0.8 MPa does not bring significant energy efficiency improvement; instead, it increases the mechanical burden on the equipment and sealing requirements. Under 0.4 MPa conditions, as the temperature increases from approximately 55°C to approximately 95°C, while maintaining a single-chamber voltage of approximately 2.0 V, the current density can increase from approximately 4875 A / m². 2 Increased to approximately 5250 A / m 2 The time required for cold start was significantly shortened, indicating that appropriately increasing the temperature is beneficial for reducing polarization, accelerating the reaction process, and improving start-up performance.

[0091] In the embodiments of this application, during the normal steady-state operation and load increase phases of the alkaline water electrolysis hydrogen production system, i.e., the steady-state operation and load increase phases of the alkaline water electrolysis hydrogen production system, the steady-state control scheme maintains the system pressure within a stable pressure range (e.g., a target pressure of approximately 0.4 MPa) and the system temperature within a stable temperature range (e.g., a target temperature range of 80–95°C). Furthermore, a preset energy consumption optimization algorithm is used to adjust the current density, flow rate, and cooling capacity to minimize the cell voltage (i.e., maintain the cell voltage below a preset voltage threshold) and maximize the Faraday efficiency (i.e., the Faraday efficiency is greater than or equal to a preset efficiency).

[0092] In one embodiment, under steady-state and increased-load conditions of the alkaline water electrolysis hydrogen production system, the system pressure can be maintained at approximately 0.4 MPa, with slight fluctuations allowed within the range of approximately 0.35–0.45 MPa. The pressure controller uses the real-time signal from the hydrogen branch pressure transmitter as input, and adjusts the hydrogen discharge regulating valve and related exhaust valves to ensure smooth and controllable system pressure changes, avoiding excessively rapid pressure fluctuations and frequent pressure shocks, thereby mitigating the impact on the gas-liquid separation process and the diaphragm structure. Simultaneously, by limiting the rate of pressure change, the uncertainty of gas crossover under transient conditions can be reduced, keeping the hydrogen content in oxygen within a predictable and controllable range.

[0093] In one example, the steady-state control scheme of the embodiments of this application is verified experimentally, referring to... Figure 4 This is a graph showing the variation of different parameters with system pressure in an embodiment of the control method of an alkaline water electrolysis hydrogen production system according to this application. The system pressures are 0.4 MPa (triangle point), 0.6 MPa (circle point), and 0.8 MPa (square point).

[0094] in, Figure 4 (a) shows the relationship between cell voltage and system pressure at different current densities, with the horizontal axis representing current density and the vertical axis representing cell voltage. It can be seen that, at the same current density, the cell voltage is lowest when the system pressure is 0.4 MPa. As the pressure increases to 0.6 MPa and 0.8 MPa, the cell voltage gradually increases, indicating that around 0.4 MPa is the optimal pressure range. Figure 4 (b) shows the change in hydrogen production with system pressure, with the horizontal axis representing current density and the vertical axis representing hydrogen production. At the same current density, the difference in hydrogen production under the three pressures is small, indicating that within the experimental range, the effect of pressure on hydrogen production is less sensitive than that of voltage and gas cross-contamination. Figure 4(c) shows the variation of hydrogen content in oxygen with system pressure. The horizontal axis represents current density, and the vertical axis represents the volume fraction of hydrogen in oxygen. Under the same current density, the hydrogen content in oxygen is lowest at a system pressure of 0.4 MPa, and generally increases when the pressure increases to 0.6 MPa and 0.8 MPa. (Summary) Figure 4 (a)~ Figure 4 (c) It can be seen that a system pressure of around 0.4 MPa has comprehensive advantages in taking into account the lower small chamber voltage, the lower hydrogen content in oxygen, and the fact that the hydrogen production capacity is not significantly reduced, which provides a basis for determining the stable pressure range in the embodiments of this application.

[0095] In one embodiment, under both steady-state and load-increase conditions of the alkaline water electrolysis hydrogen production system, the normal operating temperature of the electrolyzer is preferably controlled within the high-efficiency range of 80–95°C, and this temperature range is tightly coupled with the load setting and the load increase / decrease slope constraints. Specifically, when the electrolyzer temperature is below approximately 55°C, operation at a lower current density is permitted, for example, limiting the maximum current density to approximately 2500 A / m. 2 Simultaneously, the load change rate is strictly limited to avoid prolonged operation under low-temperature, high-potential conditions, thus reducing damage to the electrode catalyst layer. As the temperature rises to approximately 55–80°C, the current density is allowed to gradually increase within a safe range, but the load increase slope is still constrained to prevent excessively rapid load changes from causing localized temperature lag, uneven gas evolution, and transient crossover risks. Only when the temperature stabilizes in the approximately 80–95°C range is the system allowed to operate at a wide range of 20%–100% of rated load. Within this range, energy consumption optimization algorithms are used to finely adjust the current density, resulting in lower chamber voltage and higher Faraday efficiency.

[0096] This application embodiment achieves overall optimization of the electrolysis environment at both thermodynamic and kinetic levels by coordinating the setting and constraint of system pressure and system temperature with current density and load change rate. On the one hand, it balances electrolysis efficiency and mechanical safety at an optimal pressure close to 0.4 MPa. On the other hand, by constructing a "temperature-load-change slope" control rule, the system adopts different load strategies at different temperature stages, maintaining a high energy efficiency level and a low risk of gas cross-contamination during steady-state operation, providing stable and predictable thermal boundary conditions for subsequent multi-parameter coordinated control.

[0097] Optionally, the system parameters further include system load, and after determining the Faraday efficiency of the alkaline water electrolysis hydrogen production system based on the current density and the hydrogen production rate, the method further includes: If the Faraday efficiency is less than the preset efficiency and the system load is lower than the preset load threshold, then the continuous operating time of the alkaline water electrolysis hydrogen production system at a system load lower than the preset load threshold is limited, and an energy consumption anomaly alert is sent. If the Faraday efficiency is less than the preset efficiency, and the system load is equal to or higher than the preset load threshold, then the current density, the alkali flow rate, and the system pressure are adjusted to increase the Faraday efficiency to the preset efficiency under the constraint of the preset safety parameter threshold.

[0098] In the embodiments of this application, the Faraday efficiency is not only used for post-event evaluation, but can also be directly used as a feedback quantity for operational optimization. During system operation, the Faraday efficiency can be monitored simultaneously, and the system operation can be adjusted according to the current Faraday efficiency and system load.

[0099] Specifically, when the Faraday efficiency is less than the preset efficiency, the control system will adopt different adjustment strategies according to the current system load. If the system is in a low load range, that is, the system load is lower than the preset load threshold, such as less than 40% of the rated power, the long-term operation of the alkaline water electrolysis hydrogen production system is prone to efficiency decline. At this time, the control logic will limit the continuous low-load operation time of the alkaline water electrolysis hydrogen production system and issue an energy consumption anomaly warning to the upper-level dispatch or operation personnel, suggesting that the load be increased or the system be switched to equipment more suitable for low-power operation.

[0100] When the system is operating in the medium-high load range (i.e., the system load is equal to or higher than the preset load threshold) and the Faraday efficiency is still low, the system will first fine-tune parameters such as current density, alkali flow rate and system pressure to find more efficient chamber voltage and reaction conditions under the safety boundary constraints, so that the Faraday efficiency gradually converges to the preset efficiency.

[0101] This application embodiment organically combines Faraday efficiency calculation, bypass current diagnosis, and parameter adjustment. In addition to the original conventional electrical quantities such as voltage and current, it adds a control channel that focuses on "current utilization quality". This enables the alkaline water electrolysis hydrogen production system to continuously approach a better energy efficiency level while ensuring safe and stable operation, and reduces hidden energy waste during long-term operation.

[0102] Optionally, triggering the execution of a preset security scheme includes: Perform rapid load reduction, nitrogen purging, and / or emergency shutdown operations on the alkaline water electrolysis hydrogen production system. When the rapid load reduction operation, the nitrogen purging operation, and / or the emergency shutdown operation are completed, or when the hydrogen content in the oxygen, the system pressure, the system temperature, and the system liquid level are lower than the preset safety parameter thresholds, the preset safety scheme is determined to have been completed.

[0103] In this embodiment, during system operation, key system parameters can be monitored simultaneously to ensure they do not exceed preset safety parameter thresholds. When a key system parameter exceeds the preset safety parameter threshold, the system enters an inert gas purging and safety handling mode, triggering a safety interlock and executing a preset safety plan. The preset safety plan includes rapid load reduction, nitrogen purging, and / or emergency shutdown. In one embodiment, during the safety interlock triggering period, all energy efficiency-related optimization adjustments give way to safety handling until the gas composition and operating parameters return to a safe range—that is, the hydrogen content in oxygen, system pressure, system temperature, and system liquid level are below the preset safety parameter thresholds—or after the rapid load reduction, nitrogen purging, and / or emergency shutdown operations are completed. Only then is the system allowed to gradually recover to normal operation according to predetermined logic.

[0104] In this embodiment of the application, during system operation, key system parameters such as hydrogen content in oxygen, system pressure, system temperature, and system liquid level are simultaneously monitored to see if they exceed preset safety parameter thresholds. If these key system parameters exceed the preset safety parameter thresholds, a preset safety scheme is executed to achieve safe operation of the alkaline water electrolysis hydrogen production system under fluctuating power supply conditions.

[0105] Optionally, the method includes: Based on the current density and the current operating conditions, determine the target flow range for the alkali solution flow rate; Based on the hydrogen content in the oxygen, the target flow range is corrected to obtain the corrected target flow range; The flow rate of the alkali solution is controlled to remain within the corrected target flow rate range.

[0106] In the control method of the alkaline water electrolysis hydrogen production system proposed in this application, the alkaline solution flow rate is considered one of the core regulating variables affecting the mass transfer conditions of the electrolysis reaction, the chamber voltage level, and the gas cross-linking behavior. In one example, experimental studies have shown that, when other conditions are basically stable, appropriately increasing the alkaline solution circulation flow rate is beneficial to enhancing the convective mass transfer and heat removal capabilities of the electrolyte, which can reduce the degree of polarization, thereby reducing the chamber voltage and increasing the hydrogen production rate. However, increasing the alkaline solution flow rate will also change the residence time and flow state of the gas and liquid phases in the electrolyzer and gas-liquid separator, leading to an increase in the hydrogen content in the oxygen, which, if not properly controlled, will approach the safety threshold. Therefore, a simple "the higher the better" flow control strategy is not applicable, and a balance needs to be found between energy efficiency improvement and safety boundaries.

[0107] In one example, the characteristic region division of alkali flow rate-system load-hydrogen content in oxygen was determined experimentally, referring to... Figure 5This is a schematic diagram illustrating the alkali flow rate, system load, and hydrogen content in oxygen characteristic regions according to an embodiment of the control method for an alkaline water electrolysis hydrogen production system of this application. It includes cases where the alkali flow rate is 150 L / min (triangular point), 200 L / min (circular point), and 250 L / min (square point).

[0108] Figure 5 (a) The horizontal axis represents the current density, which is used to characterize the load of the electrolyzer (i.e., the system load), and the vertical axis represents the voltage of the small chamber. Different characteristic curves correspond to different alkaline flow rate conditions. Figure 5 (b) The horizontal axis represents the current density, and the vertical axis represents the hydrogen production (i.e., the amount of hydrogen produced). Different characteristic curves correspond to different alkaline solution flow conditions. Figure 5 (c) The horizontal axis represents current density, and the vertical axis represents the hydrogen volume fraction in oxygen. Different characteristic curves correspond to different alkaline solution flow rates under different operating conditions. Based on the experimentally obtained relationship between alkaline solution flow rate, system load, and hydrogen content in oxygen, the envelope curve is divided into regions, dividing the operating space into a safe and efficient zone (preferably with a hydrogen volume fraction in oxygen not exceeding approximately 1.5%), a restricted operating zone (approximately 1.5%–2%), and a prohibited operating zone (with a hydrogen volume fraction in oxygen not lower than approximately 2% or close to the lower explosive limit of 4%). The control system uses this relationship when determining operating conditions and setting the alkaline solution flow rate. Figure 5 Based on this, the allowable range of alkali flow rate and the corresponding safety boundary under different loads are selected, thereby realizing the regionalized optimization control of alkali flow rate across the entire load range.

[0109] Specifically, based on Figure 5 2Nm 3 Experimental data from a / h-level alkaline electrolysis system clearly show the relationship between alkaline solution flow rate, system load, and hydrogen content in oxygen. For example, at a current density of approximately 5000 A / m³, 2 Under the specified operating conditions, when the alkali flow rate increases from approximately 150 L / min to approximately 250 L / min, hydrogen production increases by approximately 1 L / min, the chamber voltage decreases slightly, but the hydrogen volume fraction in oxygen increases from approximately 1.24% to approximately 3.43%. The former is beneficial for improving system efficiency and hydrogen production capacity, while the latter significantly approaches or even exceeds the 2% safety interlock setting and nears the 4% lower explosive limit. Therefore, the effect of alkali flow rate on system performance and safety under different loads, temperatures, and pressures exhibits distinct regional characteristics.

[0110] This application's embodiments, based on the regional characteristics corresponding to the above-mentioned regional division, propose to pre-calibrate the relationship between alkaline solution flow rate, system load, and hydrogen content in oxygen, and construct a system as follows: Figure 5 The diagram shows the multidimensional characteristics of the "flow-load-gas crossover".

[0111] Specifically, during the experimental phase, a database reflecting safety boundaries and energy efficiency characteristics was established by systematically scanning the electrolyzer voltage, hydrogen production rate, and hydrogen content in oxygen under different combinations of current density and alkali flow rate. In engineering operation, the control system selects the corresponding target flow range for the alkali flow rate from the characteristic graph based on the current current density and operating conditions. This target flow range is then corrected by incorporating real-time feedback from the gas analyzer regarding the hydrogen content in oxygen, ensuring the alkali flow rate remains within the corrected target range. This ensures the system always operates within an optimal range that balances safety and efficiency.

[0112] In one embodiment, under high system load during steady-state operation, the alkali flow rate can be set in a relatively high range to fully leverage the advantages of reducing chamber voltage and increasing hydrogen production. At this point, system pressure and temperature are already within optimized ranges, and the hydrogen content in oxygen is typically maintained at an acceptable level. Appropriately increasing the flow rate can further improve mass transfer and heat dissipation conditions, thereby reducing energy consumption per unit of hydrogen production. However, under medium-to-low load during steady-state operation, especially near 20%–50% of rated load and during load transitions, gas cross-contamination becomes more sensitive due to decreased electrode reaction rates, reduced gas release, and relatively longer residence times. In this case, the target flow rate range can be lowered, and the gas composition signal can be given higher weight, allowing the alkali flow rate adjustment to prioritize the safety constraints of oxygen-to-hydrogen control. That is, the optimization of chamber voltage and energy efficiency should only be considered after ensuring that the hydrogen content in oxygen is below approximately 2%.

[0113] In one embodiment, the mechanism of alkali flow rate differs from that of steady-state operation during cold start, load reduction, shutdown, and inert gas purging and safety handling conditions. Before and after system shutdown, and during the inert gas purging phase, it is necessary to vent or dilute the mixed gas in the electrolyzer and pipelines within a short period to reduce the concentration of combustible gases. In these conditions, the alkali flow rate can be moderately increased within a certain range to coordinate with the venting and purging processes, accelerate gas replacement and temperature reduction, while the operating condition judgment logic ensures that this high-flow-rate phase is staggered from the electrolysis reaction phase with current flow, avoiding the risk of new gas cross-contamination caused by the superposition of high current under high-flow-rate conditions.

[0114] This application embodiment no longer treats the alkali flow rate as a single, fixed operating parameter, but rather incorporates it into a control framework that dynamically adjusts according to load conditions, gas cross-states, and energy efficiency targets. Based on characteristic diagrams and real-time monitoring data, the control system selects appropriate flow target ranges for different operating stages, prioritizing safety, and uses continuous closed-loop adjustment to ensure that the actual operating conditions fall within this range. This achieves a comprehensive goal across the entire lifecycle, coordinating safety boundary constraints, energy consumption optimization, and equipment lifespan protection.

[0115] To enable those skilled in the art to more clearly understand the technical solution of the control method for an alkaline water electrolysis hydrogen production system shown in the embodiments of this application, through... Figure 6 The specific control flow of the control method for an alkaline water electrolysis hydrogen production system shown in the embodiments of this application will be explained.

[0116] Reference Figure 6 This is a control flowchart of an embodiment of a control method for an alkaline water electrolysis hydrogen production system according to this application.

[0117] Figure 6 The control flow diagram of an embodiment of the control method for an alkaline water electrolysis hydrogen production system of this application is shown. In step S1, the system first monitors key parameters in real time such as current density, alkaline solution flow rate, system pressure, electrolyzer temperature, gas composition (including oxygen in hydrogen and hydrogen in oxygen), gas-liquid separator level, hydrogen production flow rate, cell pressure, and voltage, collects data, and writes the data into a time-series database.

[0118] Subsequently, in step S2, the operating status is determined based on the current load, temperature, and start / stop commands. The system operation is divided into cold start condition, normal steady-state operation condition, load increase condition, load decrease or shutdown condition, and inert gas purging and safety handling condition. The corresponding control strategies are then invoked as control schemes, including cold start control strategy, steady-state operation control strategy, load increase control strategy, load decrease / shutdown control strategy, and safety handling control strategy.

[0119] In step S3, the control strategies for various operating conditions are uniformly implemented as multi-parameter collaborative control. By linking and adjusting the current density, alkali flow rate, cooling water valve opening and pressure regulating valve opening, and setting load change rate constraints, the drastic changes in temperature, voltage and gas are avoided, so that the hydrogen content in oxygen is kept below the safe threshold, the electrolytic cell temperature is kept within the set range, and the small chamber voltage is reduced as much as possible.

[0120] In step S4, the system calculates the Faraday efficiency based on the theoretical hydrogen production and the measured hydrogen production, estimates the bypass current ratio, and optimizes the operating state by readjusting the current density, operating mode and related parameters when the Faraday efficiency is found to deviate from the preset efficiency.

[0121] Based on this, a safety inspection process is used to determine whether the hydrogen content in the oxygen is close to the interlock threshold, and whether safety parameters such as pressure, temperature, and liquid level exceed limits. If any abnormality is found, step S5 is initiated to trigger the safety strategy, executing interlocking protection measures such as rapid load reduction, inert gas purging, and emergency shutdown to achieve automatic interlocking protection.

[0122] Once the safety measures are completed or the safety parameters remain within the normal range, the process returns to monitoring step S1, forming a closed-loop control process of "monitoring → operating condition determination → multi-parameter collaborative control → energy efficiency and bypass current optimization → safety interlock → re-monitoring," thereby achieving safe, efficient, and stable operation of the alkaline water electrolysis hydrogen production system under fluctuating power conditions.

[0123] The following example illustrates the practical application of a control method embodiment for an alkaline water electrolysis hydrogen production system according to this application. This example is for a 2Nm... 3 Multi-parameter coordinated control of an / h-level alkaline electrolysis system.

[0124] This example uses a set of hydrogen-capacitance equipment with a rated capacity of approximately 2 Nm³. 3 The controlled object is an alkaline water electrolysis unit with a capacity of [number] h. The system consists of 22 small cells connected in series to form the main body of the electrolysis cell, and the operating current density ranges from approximately 1500 to 5500 A / m. 2 The rated operating pressure is approximately 0.4 MPa, and the electrolyte is a KOH solution with a mass fraction of approximately 30 wt%. The typical alkaline solution circulation flow rate is controlled between 150 and 250 L / h, and the normal operating temperature is maintained between 80 and 95℃. Within this operating range, the electrolyzer can operate stably while balancing energy efficiency and lifespan, providing a foundation for multi-parameter collaborative optimization control.

[0125] During the cold start phase, this example first places the system in a completely shut-down state and checks that all valves are in their safe initial positions. Then, the electrolyzer and pipelines are pretreated by nitrogen purging, and the system pressure is repeatedly varied within the range of 0.1–0.2 MPa to ensure that the internal air is fully replaced by inert gas and electrolyte, preventing the formation of a dangerous mixture of flammable gas and air during startup. After purging, the alkali circulation pump is started and the separator heating is activated, allowing the electrolyte temperature to slowly rise from room temperature to approximately 30–40°C. Simultaneously, the liquid levels in the hydrogen and oxygen gas-liquid separators are confirmed to be within the set range using level and differential pressure signals.

[0126] Based on this, the cold start process employs a strategy combining segmented current ramp-up with temperature ramp-up. The current density initially increases rapidly to approximately 1000 A / m. 2 Maintain this temperature for about ten minutes to allow the electrolytic cell to complete the initial heating and electrode activation under relatively mild conditions; once the temperature reaches approximately 55–60°C and the pressure and liquid level stabilize, increase the current density to approximately 2000–2500 A / m. 2 Meanwhile, the alkaline solution flow rate is maintained at 150–180 L / h to balance heat and mass transfer. As the temperature further rises to above approximately 70°C, the control system gradually increases the current density to the target load according to a preset slope, with a typical current increase rate of approximately 500 A / m every 10 minutes. 2During the flow ramping process, the alkali flow rate is simultaneously increased to 200–220 L / h until the temperature stabilizes in the high-efficiency range of 80–95 °C. Compared with traditional constant-current cold start, this gradual pressurization strategy significantly shortens the start-up time and substantially reduces the duration of low-temperature, high-potential operation, which helps to mitigate the deactivation of the electrode catalyst layer.

[0127] During normal operation, the control system calculates the target current density based on external power commands and matches it with the current temperature, pressure, and operating condition. When the load is above 50% of the rated capacity, the system preferentially sets the alkali flow rate to 200–250 L / h. Under conditions of approximately 0.4 MPa pressure and 80–95°C temperature, the system moderately increases the flow rate to reduce the chamber voltage and improve hydrogen production efficiency. Simultaneously, the online gas analyzer continuously monitors the hydrogen volume fraction in oxygen, and the control strategy prioritizes maintaining it below approximately 1.5% over a safe threshold of no more than 2%. For medium-low load conditions (20%–50% of rated load), to suppress gas cross-contamination under low gas flow conditions, the system automatically reduces the alkali flow rate to 150–200 L / h and limits the rate of load change to avoid drastic fluctuations in temperature, pressure, and gas composition caused by sudden increases or decreases.

[0128] During the load reduction and shutdown phases, this example prioritizes safety. When the host computer issues a load reduction or shutdown command, the control system first and gradually reduces the current density at a set slope while maintaining a relatively high alkaline solution circulation flow rate to facilitate the timely removal and separation of gases generated during electrolysis. The real-time output of the hydrogen volume fraction in oxygen from the online gas analyzer is used as a key criterion. When this value rises and approaches the warning level of approximately 1.8%, the system considers it to have entered a gas cross-risk zone. It then prohibits continuing to linearly reduce the load at the original rate and instead, according to a pre-set safety strategy, either rapidly cuts off the current and coordinates with nitrogen purging, or maintains a certain current density for a short period while increasing the flow rate and exhaust intensity to accelerate the discharge of the mixed gas. After shutdown, the alkaline solution circulation continues for a period of time, allowing the electrolyzer to cool naturally in a flowing state and purge residual gases, thereby reducing the risk of subsequent gas evolution and localized accumulation.

[0129] In terms of energy efficiency and bypass current evaluation, this example installs a flow meter at the hydrogen outlet. Combining current, effective electrode area, and the number of chambers, the theoretical hydrogen production is calculated in real-time according to Faraday's law, and the Faraday efficiency is obtained by comparing it with measured values. The control system sets the efficiency threshold at approximately 95%. When the actual efficiency is lower than this value or significantly deviates from the existing characteristic curve, it is considered that there is an increase in bypass current or an unreasonable operating point selection. For medium-to-high load conditions, the system adjusts the current density, alkali flow rate, and pressure setpoints to move the operating point towards the higher efficiency chamber voltage range. For long-term low loads and significantly low efficiency, an energy consumption anomaly warning is issued to the upper-level dispatch center, suggesting adjustments to power allocation or operating strategies. Long-term operating data can be further used to analyze the effects of electrode aging, diaphragm performance degradation, and structural modifications.

[0130] This application's embodiments achieve safe, stable, and efficient operation of the alkaline water electrolysis hydrogen production system under fluctuating power supply conditions such as wind power and photovoltaic power by incorporating key parameters such as current density, alkali flow rate, system pressure, electrolyzer temperature, start-up and shutdown procedures, gas composition, and bypass current into a unified control framework. Compared with traditional operating methods that primarily rely on "constant current" or "constant pressure" and are supplemented by simple temperature and pressure control, this application's embodiments exhibit significant comprehensive advantages in several aspects.

[0131] First, this application's embodiments construct a safety boundary control mechanism around the hydrogen volume fraction in oxygen, tightly coupling alkaline flow rate, system pressure, load level, and online gas analysis results. This ensures that the system can stably control the hydrogen content in oxygen below a preset threshold across the entire operating range, avoiding safety risks associated with approaching the lower explosive limit. Based on this, the electrolyzer can operate within a wide range of approximately 20% to 100% of its rated load, eliminating the need to reduce the available load range due to concerns about gas crosstalk at low loads. This significantly improves the system's adaptability to fluctuations in renewable energy output.

[0132] Secondly, the embodiments of this application employ a systematic and procedural collaborative optimization design for the cold start and start-up / shutdown processes. By implementing multiple rounds of nitrogen purging and liquid level pre-adjustment before startup, and adopting a segmented current ramp-up and gradual pressurization cold start strategy, the current ramp-up process is coordinated with state variables such as temperature and pressure. This not only shortens the startup time from room temperature to a stable operating state but also significantly reduces the operating time under low-temperature, high-potential conditions, mitigating irreversible damage to the electrode catalyst layer. In wind-solar coupling scenarios with frequent start-ups and shutdowns, this collaborative control method helps extend the service life of electrodes and key components, improving the long-term reliability of the system.

[0133] Furthermore, this application embodiment, through joint optimization of system pressure and electrolyzer temperature, clarifies the pressure optimization range centered at approximately 0.4 MPa, and organically combines the efficient operating temperature band of 80–95°C with load setting and load change rate control. Under this temperature and pressure combination, the cell voltage is lower and the current density increase is smoother, which is beneficial for reducing the energy consumption per unit of hydrogen production and also helps to reduce polarization fluctuations and local overheating during load increases and decreases, further improving the economy and stability of operation.

[0134] Finally, this embodiment introduces online evaluation of Faraday efficiency and bypass current into the control system, quantifying and visualizing previously imperceptible ineffective energy consumption. By comparing theoretical and actual hydrogen production in real time, the system can identify abnormal efficiency conditions without interrupting operation and adjust parameters such as current density, alkali flow rate, and pressure accordingly, gradually converging the operating point towards the high-efficiency region. Simultaneously, the long-term accumulated efficiency and energy consumption data can provide a basis for subsequent structural optimization, maintenance decisions, and operational strategy adjustments, facilitating the transformation of traditional "experience-based" operation into "data-driven" refined management.

[0135] Overall, the embodiments of this application unify safety control, start-up and shutdown process optimization, energy efficiency improvement and life protection into a set of multi-parameter collaborative optimization operation control methods, providing systematic technical support for the engineering application of alkaline water electrolysis hydrogen production systems in fluctuating power supply scenarios such as wind power and photovoltaics, and have good promotion value and application prospects.

[0136] It should be noted that, for the sake of simplicity, the method embodiments are all described as a series of actions. However, those skilled in the art should understand that the embodiments of this application are not limited to the described order of actions, because according to the embodiments of this application, some steps can be performed in other orders or simultaneously. Secondly, those skilled in the art should also understand that the embodiments described in the specification are all preferred embodiments, and the actions involved are not necessarily required by the embodiments of this application.

[0137] Based on the above embodiments, this embodiment also provides a control device for an alkaline water electrolysis hydrogen production system, which can be applied to terminal equipment, servers and other electronic devices.

[0138] Reference Figure 7 The diagram illustrates a structural block diagram of a control device embodiment for an alkaline water electrolysis hydrogen production system according to this application. The driving power supply for the alkaline water electrolysis hydrogen production system includes a fluctuating power supply, which may specifically include the following modules: The parameter acquisition module 701 is used to acquire the system parameters and system commands of the alkaline water electrolysis hydrogen production system. The system parameters include at least current density, system pressure, system temperature, system liquid level, hydrogen production, and hydrogen content in oxygen. Operating condition determination module 702 is used to determine the current operating condition of the alkaline water electrolysis hydrogen production system based on the system parameters and the system instructions; The system control module 703 is used to determine the corresponding control scheme according to the current operating condition, and execute the control scheme under the current operating condition to control the alkaline water electrolysis hydrogen production system; The efficiency determination module 704 is used to determine the Faraday efficiency of the alkaline water electrolysis hydrogen production system based on the current density and the hydrogen production amount when executing the control scheme. The safety confirmation module 705 is used to determine whether the hydrogen content in the oxygen, the system pressure, the system temperature, and the alkali liquid level exceed the preset safety parameter threshold if the Faraday efficiency is greater than or equal to the preset efficiency. The safety control module 706 is used to trigger the execution of a preset safety scheme to perform safety control on the alkaline water electrolysis hydrogen production system if the hydrogen content in the oxygen, the system pressure, the system temperature and / or the alkaline liquid level exceed the preset safety parameter threshold.

[0139] Optionally, the system temperature includes the alkaline solution temperature in the alkaline water electrolysis hydrogen production system, the system liquid level includes the alkaline solution level, and the system control module 703 includes: The cold start scheme acquisition submodule is used to acquire a cold start control scheme if the current operating condition is a cold start operating condition. The startup processing submodule is used to perform nitrogen purging operation on the alkaline water electrolysis hydrogen production system according to the cold start control scheme, and adjust the system liquid level to the preset initial liquid level range; The heating submodule is activated to heat the alkaline solution; The first start-up submodule is used to increase the current density to the first start-up density when the alkaline solution temperature reaches the first start-up temperature, and to maintain the current density at the first start-up density within a first time range. The second startup submodule is used to increase the current density from the first startup density to the second startup density in stages when the alkaline solution temperature reaches the second startup temperature. The third start-up submodule is used to increase the current density from the second start-up density to the third start-up density according to a preset start-up slope when the temperature of the alkali solution reaches the third start-up temperature, and then stop heating the alkali solution.

[0140] Optionally, the system parameters further include alkali flow rate and exhaust volume, and the system control module 703 includes: The shutdown scheme acquisition submodule is used to acquire a load reduction shutdown control scheme if the current operating condition is a load reduction operating condition or a shutdown operating condition. The first shutdown submodule is used to reduce the current density according to the first shutdown slope based on the load reduction shutdown control scheme, and to monitor the hydrogen content in the oxygen. The shutdown safety control submodule is used to perform the nitrogen purging operation and reduce the current density according to a second shutdown slope when the hydrogen content in the oxygen is greater than or equal to a preset safety content threshold, wherein the second shutdown density is greater than the first shutdown slope; or, when the hydrogen content in the oxygen is greater than or equal to a preset safety content threshold, maintain the current density above a preset density threshold and increase the alkali flow rate and the exhaust volume to a preset risk handling threshold. The second shutdown submodule is used to perform a shutdown operation on the alkaline water electrolysis hydrogen production system when the hydrogen content in the oxygen decreases to less than the preset safe content threshold.

[0141] Optionally, the system parameters further include the cell voltage, and the system control module 703 includes: The steady-state scheme acquisition submodule is used to acquire a steady-state control scheme if the current operating condition is a steady-state operating condition or a load increase operating condition. The stability control submodule is used to control the system pressure to remain within a stable pressure range and the system temperature to remain within a stable temperature range according to the steady-state control scheme. The stabilization adjustment submodule is used to adjust the current density according to a preset energy consumption optimization algorithm when the system pressure is maintained in the stable pressure range and the system temperature is maintained in the stable temperature range, so as to keep the cell voltage below a preset voltage threshold and the Faraday efficiency greater than or equal to the preset efficiency.

[0142] Optionally, the system parameters further include system load, and the device further includes: The first efficiency adjustment module is used to limit the continuous operation time of the alkaline water electrolysis hydrogen production system when the system load is below the preset load threshold if the Faraday efficiency is less than the preset efficiency and the system load is lower than the preset load threshold, and to send an energy consumption abnormality prompt. The second efficiency adjustment module is used to adjust the current density, the alkali flow rate, and the system pressure if the Faraday efficiency is less than the preset efficiency and the system load is equal to or higher than the preset load threshold, so as to increase the Faraday efficiency to the preset efficiency under the constraint of the preset safety parameter threshold.

[0143] Optionally, the security control module 706 includes: The safety operation execution submodule is used to perform rapid load reduction operation, nitrogen purging operation and / or emergency shutdown operation on the alkaline water electrolysis hydrogen production system. The safety judgment submodule is used to determine that the preset safety scheme has been completed when the rapid load reduction operation, the nitrogen purging operation and / or the emergency shutdown operation are completed, or when the hydrogen content in the oxygen, the system pressure, the system temperature and the system liquid level are lower than the preset safety parameter threshold.

[0144] Optionally, the device includes: The alkali flow rate determination module is used to determine the target flow rate range of the alkali flow rate based on the current density and the current operating conditions. A flow range correction module is used to correct the target flow range based on the hydrogen content in the oxygen, so as to obtain the corrected target flow range. A flow control module is used to control the flow rate of the alkali solution to remain within the corrected target flow range.

[0145] Optionally, the parameter acquisition module 701 includes: The initial parameter acquisition submodule is used to acquire the initial system parameters of the alkaline water electrolysis hydrogen production system; The first preprocessing submodule is used to filter and denoise the initial system parameters to obtain intermediate system parameters. The parameter to be processed determination submodule is used to determine the parameters to be processed in the intermediate system parameters. The parameters to be processed include intermediate system parameters that exceed a preset boundary threshold and intermediate system parameters with missing signals. The second preprocessing submodule is used to mark and / or fault-tolerantly process the parameters to be processed in the intermediate system parameters to obtain the system parameters of the alkaline water electrolysis hydrogen production system.

[0146] This application also provides a non-volatile readable storage medium storing one or more modules (programs). When these modules are applied to a device, they enable the device to execute the instructions for the method steps in this application.

[0147] This application provides one or more machine-readable media storing instructions that, when executed by one or more processors, cause an electronic device to perform one or more of the methods described in the above embodiments. In this application, the electronic device includes various types of devices such as terminal devices and servers (clusters).

[0148] The embodiments of this disclosure can be implemented as an apparatus configured as desired using any suitable hardware, firmware, software, or any combination thereof, including electronic devices such as terminal devices, servers (clusters), etc. Figure 8 An exemplary apparatus 800 is schematically shown that can be used to implement the various embodiments described in this application.

[0149] In one embodiment, Figure 8 An exemplary device 800 is shown, which includes one or more processors 802, a control module (chipset) 804 coupled to at least one of the processors 802, a memory 806 coupled to the control module 804, a non-volatile memory (NVM) / storage device 808 coupled to the control module 804, one or more input / output devices 810 coupled to the control module 804, and a network interface 812 coupled to the control module 804.

[0150] Processor 802 may include one or more single-core or multi-core processors, and processor 802 may include any combination of general-purpose processors or special-purpose processors (e.g., graphics processors, application processors, baseband processors, etc.). In some embodiments, device 800 can serve as a terminal device, server (cluster), or other device as described in the embodiments of this application.

[0151] In some embodiments, apparatus 800 may include one or more computer-readable media (e.g., memory 806 or NVM / storage device 808) having instructions 814 and one or more processors 802 that are combined with the one or more computer-readable media and configured to execute the instructions 814 to implement the module and thus perform the actions described in this disclosure.

[0152] In one embodiment, the control module 804 may include any suitable interface controller to provide any suitable interface to at least one of the processors 802 and / or any suitable device or component communicating with the control module 804.

[0153] The control module 804 may include a memory controller module to provide an interface to the memory 806. The memory controller module may be a hardware module, a software module, and / or a firmware module.

[0154] Memory 806 may be used, for example, to load and store data and / or instructions 814 for device 800. In one embodiment, memory 806 may include any suitable volatile memory, such as suitable DRAM. In some embodiments, memory 806 may include double data rate type quad synchronous dynamic random access memory (DDR4 SDRAM).

[0155] In one embodiment, the control module 804 may include one or more input / output controllers to provide an interface to the NVM / storage device 808 and (one or more) input / output devices 810.

[0156] For example, NVM / storage device 808 may be used to store data and / or instructions 814. NVM / storage device 808 may include any suitable non-volatile memory (e.g., flash memory) and / or may include any suitable (one or more) non-volatile storage devices (e.g., one or more hard disk drive (HDD), one or more optical disc (CD) drives, and / or one or more digital universal optical disc (DVD) drives).

[0157] NVM / storage device 808 may include storage resources that are physically part of a device on which device 800 is mounted, or that are accessible to the device but do not necessarily have to be part of the device. For example, NVM / storage device 808 may be accessed via a network via one or more input / output devices 810.

[0158] One or more input / output devices 810 may provide an interface for device 800 to communicate with any other suitable device. Input / output devices 810 may include communication components, audio components, sensor components, etc. A network interface 812 may provide an interface for device 800 to communicate via one or more networks. Device 800 may wirelessly communicate with one or more components of a wireless network according to any of one or more wireless network standards and / or protocols, such as accessing a wireless network based on a communication standard, such as WiFi, 2G, 3G, 4G, 5G, etc., or a combination thereof.

[0159] In one embodiment, at least one of the processors 802 may be logically packaged with one or more controllers (e.g., memory controller modules) of the control module 804. In one embodiment, at least one of the processors 802 may be logically packaged with one or more controllers of the control module 804 to form a system-in-package (SiP). In one embodiment, at least one of the processors 802 may be integrated with the logic of one or more controllers of the control module 804 on the same die. In one embodiment, at least one of the processors 802 may be integrated with the logic of one or more controllers of the control module 804 on the same die to form a system-on-a-chip (SoC).

[0160] In various embodiments, device 800 may be, but is not limited to, a terminal device such as a server, desktop computing device, or mobile computing device (e.g., laptop computing device, handheld computing device, tablet computer, netbook, etc.). In various embodiments, device 800 may have more or fewer components and / or different architectures. For example, in some embodiments, device 800 includes one or more cameras, a keyboard, a liquid crystal display (LCD) screen (including a touchscreen display), a non-volatile memory port, multiple antennas, a graphics chip, an application-specific integrated circuit (ASIC), and a speaker.

[0161] The detection device can use a main control chip as a processor or control module, and sensor data, position information, etc. can be stored in a memory or NVM / storage device. The sensor group can be used as an input / output device, and the communication interface can include a network interface.

[0162] As the apparatus embodiment is basically similar to the method embodiment, it is described in a relatively simple manner. For relevant details, please refer to the description of the method embodiment.

[0163] The various embodiments in this specification are described in a progressive manner, with each embodiment focusing on the differences from other embodiments. The same or similar parts between the various embodiments can be referred to each other.

[0164] This application describes embodiments with reference to flowchart illustrations and / or block diagrams of methods, terminal devices (systems), and computer program products according to embodiments of this application. It should be understood that each block of the flowchart illustrations and / or block diagrams, and combinations of blocks in the flowchart illustrations and / or block diagrams, can be implemented by computer program instructions. These computer program instructions can be provided to a processor of a general-purpose computer, special-purpose computer, embedded processor, or other programmable alkaline water electrolysis hydrogen production system control terminal device to produce a machine, such that the instructions executable by the processor of the computer or other programmable alkaline water electrolysis hydrogen production system control terminal device generate instructions for implementing the process... Figure 1 One or more processes and / or boxes Figure 1 A device that provides the functions specified in one or more boxes.

[0165] These computer program instructions may also be stored in a computer-readable storage medium that can direct a computer or other programmable alkaline water electrolysis hydrogen production system to operate in a specific manner, such that the instructions stored in the computer-readable storage medium produce an article of manufacture including instruction means, which are implemented in the process. Figure 1 One or more processes and / or boxes Figure 1 The function specified in one or more boxes.

[0166] These computer program instructions can also be loaded onto a computer or other programmable alkaline water electrolysis hydrogen production system control terminal equipment, causing a series of operational steps to be executed on the computer or other programmable terminal equipment to produce computer-implemented processing, thereby providing instructions that execute on the computer or other programmable terminal equipment for implementing the process. Figure 1 One or more processes and / or boxes Figure 1 Figure 1 The steps of the function specified in one or more boxes.

[0167] Although preferred embodiments of the present application have been described, those skilled in the art, upon learning the basic inventive concept, can make other changes and modifications to these embodiments. Therefore, the appended claims are intended to be interpreted as including the preferred embodiments as well as all changes and modifications falling within the scope of the embodiments of the present application.

[0168] Finally, it should be noted that in this document, relational terms such as "first" and "second" are used only to distinguish one entity or operation from another, and do not necessarily require or imply any such actual relationship or order between these entities or operations. Furthermore, the terms "comprising," "including," or any other variations thereof are intended to cover non-exclusive inclusion, such that a process, method, article, or terminal device that comprises a list of elements includes not only those elements but also other elements not expressly listed, or elements inherent to such a process, method, article, or terminal device. Without further limitations, an element defined by the phrase "comprising one..." does not exclude the presence of other identical elements in the process, method, article, or terminal device that includes said element.

[0169] The control method and apparatus for an alkaline water electrolysis hydrogen production system, an electronic device, and a storage medium provided in this application have been described in detail above. Specific examples have been used to illustrate the principles and implementation methods of this application. The descriptions of the above embodiments are only for the purpose of helping to understand the method and core ideas of this application. At the same time, for those skilled in the art, there will be changes in the specific implementation methods and application scope based on the ideas of this application. Therefore, the content of this specification should not be construed as a limitation of this application.

Claims

1. A control method for an alkaline water electrolysis hydrogen production system, characterized in that, The driving power supply for the alkaline water electrolysis hydrogen production system includes a fluctuating power supply, and the method includes: Obtain the system parameters and system commands of the alkaline water electrolysis hydrogen production system. The system parameters include at least the current density, system pressure, system temperature, system liquid level, hydrogen production, and hydrogen content in oxygen. The current operating condition of the alkaline water electrolysis hydrogen production system is determined based on the system parameters and system instructions. A corresponding control scheme is determined based on the current operating conditions, and the control scheme is executed under the current operating conditions to control the alkaline water electrolysis hydrogen production system. When implementing the control scheme, the Faraday efficiency of the alkaline water electrolysis hydrogen production system is determined based on the current density and the hydrogen production rate. If the Faraday efficiency is greater than or equal to the preset efficiency, then determine whether the hydrogen content in the oxygen, the system pressure, the system temperature, and the system liquid level exceed the preset safety parameter threshold. If the hydrogen content in the oxygen, the system pressure, the system temperature, and / or the system liquid level exceed the preset safety parameter threshold, a preset safety scheme is triggered to perform safety control on the alkaline water electrolysis hydrogen production system.

2. The method according to claim 1, characterized in that, The system temperature includes the alkaline solution temperature in the alkaline water electrolysis hydrogen production system, and the system liquid level includes the alkaline solution level. The step of determining a corresponding control scheme based on the current operating conditions and executing the control scheme under the current operating conditions includes: If the current operating condition is a cold start condition, then obtain the cold start control scheme; According to the cold start control scheme, nitrogen purging is performed on the alkaline water electrolysis hydrogen production system, and the system liquid level is adjusted to the preset initial liquid level range; The alkaline solution is heated; When the temperature of the alkaline solution reaches the first start-up temperature, the current density is increased to the first start-up density, and the current density is maintained at the first start-up density within a first time range; When the temperature of the alkaline solution reaches the second start-up temperature, the current density is gradually increased from the first start-up density to the second start-up density. When the temperature of the alkali solution reaches the third start-up temperature, the current density is increased from the second start-up density to the third start-up density according to the preset start-up slope, and the heating of the alkali solution is stopped.

3. The method according to claim 2, characterized in that, The system parameters also include alkali flow rate and exhaust volume. The step of determining the corresponding control scheme based on the current operating conditions and executing the control scheme under the current operating conditions includes: If the current operating condition is a load reduction condition or a shutdown condition, then obtain the load reduction and shutdown control scheme; According to the load reduction shutdown control scheme, the current density is reduced according to the first shutdown slope, and the hydrogen content in the oxygen is monitored; When the hydrogen content in the oxygen is greater than or equal to a preset safe content threshold, the nitrogen purging operation is performed, and the current density is reduced according to a second shutdown slope, where the second shutdown density is greater than the first shutdown slope; or, when the hydrogen content in the oxygen is greater than or equal to a preset safe content threshold, the current density is maintained at a level higher than a preset density threshold, and the alkaline flow rate and the exhaust volume are increased to a preset risk treatment threshold. When the hydrogen content in the oxygen decreases to below the preset safe content threshold, the alkaline water electrolysis hydrogen production system is shut down.

4. The method according to claim 1, characterized in that, The system parameters also include the cell voltage. The step of determining the corresponding control scheme based on the current operating condition and executing the control scheme under the current operating condition includes: If the current operating condition is a steady-state operating condition or a load increase operating condition, then obtain the steady-state control scheme; According to the steady-state control scheme, the system pressure is controlled to remain within a stable pressure range, and the system temperature is controlled to remain within a stable temperature range. When the system pressure is maintained within the stable pressure range and the system temperature is maintained within the stable temperature range, the current density is adjusted according to a preset energy consumption optimization algorithm so that the cell voltage is maintained below a preset voltage threshold and the Faraday efficiency is greater than or equal to the preset efficiency.

5. The method according to claim 3, characterized in that, The system parameters also include system load. After determining the Faraday efficiency of the alkaline water electrolysis hydrogen production system based on the current density and the hydrogen production rate, the method further includes: If the Faraday efficiency is less than the preset efficiency and the system load is lower than the preset load threshold, then the continuous operating time of the alkaline water electrolysis hydrogen production system at a system load lower than the preset load threshold is limited, and an energy consumption anomaly alert is sent. If the Faraday efficiency is less than the preset efficiency, and the system load is equal to or higher than the preset load threshold, then the current density, the alkali flow rate, and the system pressure are adjusted to increase the Faraday efficiency to the preset efficiency under the constraint of the preset safety parameter threshold.

6. The method according to claim 1, characterized in that, The triggering of the preset security scheme includes: Perform rapid load reduction, nitrogen purging, and / or emergency shutdown operations on the alkaline water electrolysis hydrogen production system. When the rapid load reduction operation, the nitrogen purging operation, and / or the emergency shutdown operation are completed, or when the hydrogen content in the oxygen, the system pressure, the system temperature, and the system liquid level are lower than the preset safety parameter thresholds, the preset safety scheme is determined to have been completed.

7. The method according to claim 3, characterized in that, The method includes: Based on the current density and the current operating conditions, determine the target flow range for the alkali solution flow rate; Based on the hydrogen content in the oxygen, the target flow range is corrected to obtain the corrected target flow range; The flow rate of the alkali solution is controlled to remain within the corrected target flow rate range.

8. The method according to claim 1, characterized in that, The process of obtaining the system parameters of the alkaline water electrolysis hydrogen production system includes: Obtain the initial system parameters of the alkaline water electrolysis hydrogen production system; The initial system parameters are filtered and denoised to obtain intermediate system parameters; Determine the parameters to be processed in the intermediate system parameters, including intermediate system parameters that exceed a preset boundary threshold and intermediate system parameters with missing signals; The parameters to be processed in the intermediate system parameters are marked and / or fault-tolerant to obtain the system parameters of the alkaline water electrolysis hydrogen production system.

9. A control device for an alkaline water electrolysis hydrogen production system, characterized in that, The driving power supply for the alkaline water electrolysis hydrogen production system includes a fluctuating power supply, and the device includes: The parameter acquisition module is used to acquire the system parameters and system commands of the alkaline water electrolysis hydrogen production system. The system parameters include at least current density, system pressure, system temperature, system liquid level, hydrogen production, and hydrogen content in oxygen. The operating condition determination module is used to determine the current operating condition of the alkaline water electrolysis hydrogen production system based on the system parameters and the system instructions. The system control module is used to determine the corresponding control scheme according to the current operating conditions, and execute the control scheme under the current operating conditions to control the alkaline water electrolysis hydrogen production system; An efficiency determination module is used to determine the Faraday efficiency of the alkaline water electrolysis hydrogen production system based on the current density and the hydrogen production amount when executing the control scheme. The safety confirmation module is used to determine whether the hydrogen content in the oxygen, the system pressure, the system temperature, and the alkali liquid level exceed the preset safety parameter threshold if the Faraday efficiency is greater than or equal to the preset efficiency. The safety control module is used to trigger the execution of a preset safety scheme to perform safety control on the alkaline water electrolysis hydrogen production system if the hydrogen content in the oxygen, the system pressure, the system temperature and / or the alkaline solution level exceed the preset safety parameter threshold.

10. An electronic device, characterized in that, include: processor; and A memory having executable code stored thereon, which, when executed, causes the processor to perform the control method for the alkaline water electrolysis hydrogen production system as described in any one of claims 1-8.

11. A machine-readable medium having executable code stored thereon, which, when executed, causes a processor to perform a control method for an alkaline water electrolysis hydrogen production system as described in any one of claims 1-8.

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