Method and device for regulating and controlling operation range of hydrogen production system and computer equipment

Abstract

The invention relates to the technical field of electrolytic hydrogen production, and discloses a method and device for regulating and controlling the operation range of a hydrogen production system and computer equipment, and the method comprises the following steps: establishing an electrochemical model and a hydrogen-in-oxygen model of the hydrogen production system; calculating a polarization curve and a hydrogen-in-oxygen concentration contour line under different operation pressures, different temperatures and different alkali liquor flows based on an electrochemical model and a hydrogen-in-oxygen model; adding a boundary limit line on the polarization curve, and constructing a safe operation boundary envelope diagram based on the boundary limit line, the polarization curve, a hydrogen concentration contour line in oxygen and a gas-liquid separation capacity line; the minimum current, the real-time operation current and the maximum current of the hydrogen production system are obtained, and the safety margin is calculated; and regulating and controlling the operation range of the hydrogen production system based on the safety operation boundary envelope diagram and the safety allowance. According to the method, the purposes of accurately determining the safe operation boundary of the alkali liquor hydrogen production system and effectively regulating and controlling the operation range of the hydrogen production system are achieved.

Description

Technical Field

[0001] The present invention relates to the technical field of electrolytic hydrogen production, and in particular to a method, device and computer equipment for controlling the operating range of a hydrogen production system. Background Art

[0002] With the growing global demand for clean energy, hydrogen, a highly promising clean energy source, boasts advantages such as high energy density, zero pollution, and abundant resources. Its dual properties of energy and material make it superior to other energy storage methods in terms of storage duration and interregional transfer. Therefore, its production technology has become a hot topic of research. Alkaline water electrolysis hydrogen production technology, with its high maturity and relatively low cost, holds a key position in large-scale hydrogen production. However, the safe operation of alkaline water electrolysis hydrogen production faces numerous challenges, among which HTO (Hydrogen in Oxygen) is the most critical safety indicator. Once the HTO content exceeds 2%, the system faces the risk of explosion, which seriously threatens life and property safety. Furthermore, the operation of AWE (Alkaline Water Electrolysis) systems is also constrained by multiple factors, including maximum allowable current, maximum allowable voltage, maximum and minimum operating pressures, maximum and minimum operating temperatures, and gas-liquid separation capacity.

[0003] At present, although some studies have touched upon the operating characteristics and control strategies of AWE systems, the research on the safe operating boundaries of the system is still not in-depth enough. The safe operating boundaries and their evolution laws with operating parameters are still unclear, resulting in insufficient means to regulate the safe operating boundaries. Summary of the Invention

[0004] In view of this, the present invention provides a method, device and computer equipment for controlling the operating range of a hydrogen production system to solve the problems of unclear safe operating boundaries and insufficient control means in the prior art.

[0005] In a first aspect, the present invention provides a method for controlling the operating range of a hydrogen production system, the method comprising:

[0006] Establish electrochemical models and hydrogen-in-oxygen models for hydrogen production systems;

[0007] Based on the electrochemical model and the hydrogen-in-oxygen model, the polarization curves and isolines of hydrogen-in-oxygen concentrations at different operating pressures, temperatures, and alkali solution flow rates are calculated, and the gas-liquid separation capacity line is also calculated.

[0008] Add boundary limit lines to the polarization curve, and construct a safe operation boundary envelope diagram based on the polarization curve with the boundary limit lines added, the hydrogen concentration contour line in oxygen, and the gas-liquid separation ability line;

[0009] Obtain the minimum current, real-time operating current, and maximum current of the hydrogen production system, and calculate the safety margin based on the minimum current, real-time operating current, and maximum current;

[0010] The operating range of the hydrogen production system is regulated based on the safe operating boundary envelope and safety margin.

[0011] The present invention provides a method for controlling the operating range of a hydrogen production system. The method establishes an electrochemical model and a hydrogen-in-oxygen model, can accurately simulate the core process of the hydrogen production system, and can comprehensively monitor the operating status of the system by calculating polarization curves, hydrogen-in-oxygen concentration contour lines, and gas-liquid separation capacity lines under different operating pressures, temperatures, and alkali liquid flow rates. The safe operating boundary is drawn in the form of an HTO envelope diagram based on the observed changes in current, voltage, temperature, pressure, alkali liquid flow rate, and gas-liquid separation capacity, thereby achieving the purpose of accurately determining the safe operating boundary of the alkali liquid hydrogen production system, obtaining the minimum current, real-time operating current, and maximum current of the hydrogen production system, calculating the safety margin based on the minimum current, real-time operating current, and maximum current, and effectively controlling the operating range of the hydrogen production system based on the safe operating boundary and the safety margin, thereby solving the problems of unclear safe operating boundaries and insufficient control means in the prior art.

[0012] In an optional embodiment, establishing an electrochemical model and a hydrogen-in-oxygen model of a hydrogen production system includes:

[0013] Calculate the reversible electrolysis voltage, activation overpotential, ohmic overpotential, and concentration gradient overpotential during the operation of the hydrogen production system, and establish an electrochemical model based on the reversible electrolysis voltage, activation overpotential, ohmic overpotential, and concentration gradient overpotential;

[0014] The hydrogen exchange flux, diffusion flux, convection flux, alkali solution mixing flux and oxygen production rate per unit time during the operation of the hydrogen production system are calculated, and a hydrogen-in-oxygen model is established based on the hydrogen exchange flux, diffusion flux, convection flux, alkali solution mixing flux and oxygen production rate per unit time.

[0015] The present invention provides a method for regulating the operating range of a hydrogen production system. This method uses an electrochemical model developed by integrating reversible electrolysis voltage, activation overpotential, ohmic overpotential, and concentration gradient overpotential to comprehensively and meticulously describe the electrochemical behavior of the hydrogen production system during operation. A hydrogen-in-oxygen model, which comprehensively considers all hydrogen transmission fluxes and oxygen production rate, provides a strong guarantee for the safe operation of the hydrogen production system.

[0016] In an optional embodiment, the polarization curve, the hydrogen in oxygen concentration contour line, and the gas-liquid separation ability line at a preset operating pressure, a preset temperature, and a preset alkali solution flow rate are calculated based on the electrochemical model and the hydrogen in oxygen model, including:

[0017] Different operating pressures, temperatures, and alkali flow rates were input into the electrochemical model to obtain the corresponding polarization curves.

[0018] Different operating pressures, temperatures and alkali solution flow rates were input into the oxygen-hydrogen model to obtain the corresponding isovalues of hydrogen concentration in oxygen.

[0019] The gas-liquid separation capacity line is calculated based on the diameter and length of the gas-liquid separator in the hydrogen production system and the gas-liquid variable parameters under different operating pressures, temperatures and alkali solution flow rates.

[0020] The present invention provides a method for controlling the operating range of a hydrogen production system. Different operating pressures, temperatures, and alkali solution flows are input into an electrochemical model respectively, and the corresponding polarization curves under each operating condition can be accurately obtained. Based on the polarization curves under different operating conditions, a performance comparison analysis can be performed. It can be clearly determined under which combination of operating pressure, temperature, and alkali solution flow the electrochemical reaction efficiency of the hydrogen production system is the highest and the energy consumption is the lowest. Different operating parameters are input into the oxygen-hydrogen model to obtain the corresponding oxygen-hydrogen concentration contour line, which can accurately evaluate the safety risks of the hydrogen production system under different operating conditions. In the hydrogen production process, the gas-liquid separation capacity line of the gas-liquid separator is also taken into account, laying the foundation for dynamic safety monitoring of the hydrogen production system.

[0021] In an optional embodiment, the boundary limit lines include a maximum voltage limit line, a maximum current limit line, a minimum temperature limit line, a maximum temperature limit line, and a hydrogen concentration limit line in oxygen;

[0022] Add boundary limit lines to the polarization curve, and construct a safe operation boundary envelope diagram based on the polarization curve with the boundary limit lines added and the hydrogen concentration contour line in oxygen, including:

[0023] Add the maximum voltage limit line, maximum current limit line, minimum temperature limit line, maximum temperature limit line and hydrogen concentration limit line in oxygen to the polarization curve respectively;

[0024] A safe operation boundary envelope diagram is constructed based on the polarization curve with the addition of the maximum voltage limit line, maximum current limit line, minimum temperature limit line, maximum temperature limit line and hydrogen concentration limit line in oxygen, the isoline of hydrogen concentration in oxygen and the gas-liquid separation ability line.

[0025] The present invention provides a method for controlling the operating range of a hydrogen production system, which adds a maximum voltage limit line, a maximum current limit line, a minimum temperature limit line, a maximum temperature limit line, a hydrogen concentration limit line in oxygen, and a gas-liquid separation ability line to constrain the operating parameters of the hydrogen production system from multiple key dimensions. The polarization curve itself reflects the relationship between current density and electrode potential. After adding the boundary limit line, it can intuitively show whether the hydrogen production system is in a safe operating state under different potentials and current densities. The safe operation boundary envelope diagram integrates the boundary limit lines of the polarization curve and the isoline of hydrogen concentration in oxygen, and can identify potential safety risks in advance. By observing the position of the operating point in the envelope diagram, it can be determined whether the system is close to or exceeds the safety boundary. As the operating time of the hydrogen production system goes on, by continuously observing the moving trajectory of the operating point in the safe operation boundary envelope diagram, the changing trend of the operating risk of the hydrogen production system can be analyzed.

[0026] In an optional embodiment, the hydrogen concentration in oxygen includes a first threshold, a second threshold, and a third threshold, and the values of the first threshold, the second threshold, and the third threshold decrease in sequence; constructing the safe operation boundary envelope diagram based on the polarization curve after adding the boundary limit line, the hydrogen concentration contour line in oxygen, and the gas-liquid separation ability line further includes:

[0027] The area outside the safe operation boundary envelope diagram is called the danger zone; the area from the second threshold value to the first threshold value of the hydrogen concentration in oxygen within the safe operation boundary envelope diagram is called the warning zone; the area from the third threshold value to the second threshold value of the hydrogen concentration in oxygen within the safe operation boundary envelope diagram and less than the gas-liquid separation ability line is called the safety zone.

[0028] The present invention provides a method for regulating the operating range of a hydrogen production system. This method divides the system into danger zones, warning zones, and safe zones based on a safe operating boundary envelope diagram, clearly defining the degree of danger of the hydrogen production system under different hydrogen-in-oxygen concentrations. If the warning zone is within the safe operating boundary envelope diagram but the hydrogen-in-oxygen concentration is between the second threshold and the first threshold, it indicates that although the system has not yet completely lost control, it is approaching a dangerous state. This level of warning can remind operators to pay close attention to the system's operating status and take measures in advance. The division into different areas facilitates targeted adjustments to operating parameters based on the system's current state.

[0029] In an optional implementation, the safety margin includes an uplink safety margin and a downlink safety margin;

[0030] Obtain the minimum current, real-time operating current, and maximum current of the hydrogen production system, and calculate the safety margin based on the minimum current, real-time operating current, and maximum current, including:

[0031] Calculate the minimum current of the hydrogen production system based on the hydrogen in oxygen model;

[0032] The upstream safety margin and downstream safety margin are calculated based on the minimum current, real-time operating current and maximum current respectively.

[0033] The present invention provides a method for controlling the operating range of a hydrogen production system. The method calculates the minimum current through a hydrogen-in-oxygen model, integrates the real-time operating current and the maximum current, and comprehensively considers the key parameters of the hydrogen production system in the current dimension. The uplink safety margin and the downlink safety margin are calculated based on the minimum current, the real-time operating current, and the maximum current, respectively, and the complex system operating state is converted into a specific numerical value. Compared with relying solely on experience or fuzzy judgment, this quantitative evaluation method greatly improves the accuracy and scientific nature of the safety status assessment. The safety margin shows the changes in the real-time operating current, maximum current, and minimum current of the system under a variety of operating conditions. When the operator observes that the safety margin is low under a certain combination of operating pressure and alkali solution flow, the operating parameters can be adjusted in a targeted manner based on this information, combined with other system operating data such as the polarization curve and the hydrogen-in-oxygen concentration area division.

[0034] In an optional embodiment, the method for controlling the operating range of the hydrogen production system further includes:

[0035] Under different operating pressures and different alkali solution flow rates, the corresponding upstream safety margin and downstream safety margin are calculated based on the upstream safety margin and downstream safety margin respectively;

[0036] Based on the uplink safety margin and downlink safety margin, the relationship between the real-time operating current and the maximum current and minimum current are displayed respectively.

[0037] The present invention provides a method for controlling the operating range of a hydrogen production system. By setting the concept of safety margin and calculating the upward and downward safety margins, a safety margin diagram can be constructed, which can more intuitively display the changing relationship between the real-time operating current and the maximum current and the minimum current, respectively, and can more accurately provide early warning of possible safety risks that the system may face.

[0038] In an optional embodiment, regulating the operating range of the hydrogen production system based on the safe operating boundary envelope diagram and the safety margin includes:

[0039] The impact of different operating pressures, different alkali liquid flow rates and different temperatures on the safety zone, danger zone, warning zone, as well as the upward safety margin and downward safety margin are analyzed, and the operating pressure, alkali liquid flow rate and temperature of the hydrogen production system are regulated based on the impact rules.

[0040] The present invention provides a method for regulating the operating range of a hydrogen production system, which analyzes the influence of different operating pressures, alkali liquid flow rates and temperatures on the three regions and the upward safety margin and downward safety margin, so that operators and managers can accurately grasp the risk changes of the hydrogen production system under different working conditions. Based on these influencing rules, regulation is carried out to achieve the management and control of system risks from multiple dimensions of operating pressure, alkali liquid flow rate and temperature. By studying the influencing rules, the operating pressure, alkali liquid flow rate and temperature combination that is most suitable for safe and efficient operation of the system can be found. Under the premise of ensuring that the system is in a safe area (such as a safe zone), these parameters are adjusted to improve the hydrogen production efficiency.

[0041] In a second aspect, the present invention provides a device for controlling an operating range of a hydrogen production system, the device comprising:

[0042] Model building module, used to build the electrochemical model and hydrogen-in-oxygen model of the hydrogen production system;

[0043] The limit line calculation module is used to calculate the polarization curve and the hydrogen-in-oxygen concentration contour line under different operating pressures, temperatures and alkali solution flow rates based on the electrochemical model and the hydrogen-in-oxygen model, and also calculate the gas-liquid separation ability line;

[0044] A safe operation boundary envelope diagram construction module is used to add boundary limit lines to the polarization curve and construct a safe operation boundary envelope diagram based on the polarization curve with the boundary limit lines added, the hydrogen concentration contour line in oxygen, and the gas-liquid separation ability line;

[0045] A safety margin calculation module is used to obtain the minimum current, real-time operating current, and maximum current of the hydrogen production system, and calculate the safety margin based on the minimum current, real-time operating current, and maximum current;

[0046] The hydrogen production system operating range control module is used to control the operating range of the hydrogen production system based on the safe operating boundary envelope diagram and safety margin.

[0047] In a third aspect, the present invention provides a computer device comprising: a memory and a processor, the memory and the processor being communicatively connected to each other, the memory storing computer instructions, and the processor executing the method for controlling the operating range of a hydrogen production system according to the first aspect or any corresponding embodiment thereof by executing the computer instructions.

[0048] In a fourth aspect, the present invention provides a computer-readable storage medium having computer instructions stored thereon, the computer instructions being used to enable a computer to execute the method for controlling the operating range of a hydrogen production system according to the first aspect or any corresponding embodiment thereof.

[0049] In a fifth aspect, the present invention provides a computer program product comprising computer instructions for causing a computer to execute the method for controlling the operating range of a hydrogen production system according to the first aspect or any corresponding embodiment thereof. BRIEF DESCRIPTION OF THE DRAWINGS

[0050] In order to more clearly illustrate the specific embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for use in the specific embodiments or the description of the prior art. Obviously, the drawings described below are some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

[0051] Figure 1 is a flow chart of a method for controlling the operating range of a hydrogen production system according to an embodiment of the present invention;

[0052] Figure 2 is a flow chart of another method for controlling the operating range of a hydrogen production system according to an embodiment of the present invention;

[0053] Figure 3 is a flow chart of another method for controlling the operating range of a hydrogen production system according to an embodiment of the present invention;

[0054] FIG4( a ) is an envelope diagram of system safe operation under different alkali solution flow rates and different operating pressures according to an embodiment of the present invention;

[0055] FIG4( b ) is another diagram of system safe operation under different alkali solution flow rates and different operating pressures according to an embodiment of the present invention;

[0056] FIG4( c ) is another diagram of the safe operation of the system under different alkali solution flow rates and different operating pressures according to an embodiment of the present invention;

[0057] FIG5( a ) is a schematic diagram of a safe operating range of current under different operating pressures at a constant alkali solution flow rate according to an embodiment of the present invention;

[0058] FIG5( b ) is a schematic diagram of another safe operating range of current under different operating pressures at a constant alkali solution flow rate according to an embodiment of the present invention;

[0059] FIG5( c ) is another schematic diagram of the safe operating range of current under different operating pressures at a constant alkali solution flow rate according to an embodiment of the present invention;

[0060] Figure 6 Schematic diagram of the safety margin of a hydrogen production system under a certain specific pressure and alkali solution flow rate according to an embodiment of the present invention;

[0061] Figure 7 is a schematic diagram of the relationship between system energy efficiency input and output according to an embodiment of the present invention;

[0062] Figure 8 This is a schematic diagram showing how the system energy efficiency is always optimized within the load range according to an embodiment of the present invention under the premise that HTO is ≤ 2%;

[0063] Figure 9 is a schematic diagram showing changes in system energy efficiency and HTO as the load changes within the load range according to an embodiment of the present invention;

[0064] Figure 10 This is a safe operation envelope diagram of the AWE hydrogen production system affected by the separation capacity of the gas-liquid separator according to an embodiment of the present invention.

[0065] Figure 11 is a schematic diagram of a safe operating range of current affected by the separation capacity of a gas-liquid separator according to an embodiment of the present invention;

[0066] Figure 12 is a structural block diagram of a device for controlling an operating range of a hydrogen production system according to an embodiment of the present invention;

[0067] Figure 13 Schematic diagram of the hardware structure of a computer device according to an embodiment of the present invention. DETAILED DESCRIPTION

[0068] To make the purpose, technical solutions, and advantages of the embodiments of the present invention more clear, the technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the accompanying drawings in the embodiments of the present invention. Obviously, the described embodiments are part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without making creative efforts shall fall within the scope of protection of the present invention.

[0069] The safe operating boundary and its evolution with operating parameters in the existing technology are still unclear. Therefore, it is necessary to study the safe operating boundary of the AWE (Alkaline Water Electrolysis, alkaline water electrolysis, abbreviated as AWE) hydrogen production system, explore the influence of operating parameters on the safe operating boundary, and propose a method for widening the safe operating boundary and a control strategy, which has important research significance and value for widening the safe operating range of the AWE hydrogen production system and its comprehensive energy efficiency coupled with green electricity. The embodiment of the present invention provides a hydrogen production system operating range control, which achieves the effect of accurately determining the safe operating boundary of the alkaline liquid hydrogen production system and realizing effective control.

[0070] According to an embodiment of the present invention, an embodiment of a method for regulating the operating range of a hydrogen production system is provided. It should be noted that the steps shown in the flowchart of the accompanying drawings can be executed in a computer system such as a set of computer-executable instructions, and although a logical order is shown in the flowchart, in some cases, the steps shown or described can be executed in an order different from that shown here.

[0071] In this embodiment, a method for controlling the operating range of a hydrogen production system is provided, which can be used in a hydrogen production system. Figure 1 FIG. 1 is a flow chart of a method for controlling the operating range of a hydrogen production system according to an embodiment of the present invention. Figure 1 As shown, the process includes the following steps:

[0072] Step S101 : establishing an electrochemical model and a hydrogen-in-oxygen model of a hydrogen production system.

[0073] Specifically, the electrochemical model accurately describes the voltage-current relationship of the hydrogen production system's electrolyzer under different operating conditions, fully accounting for factors such as reversible voltage, activation overpotential, and ohmic overpotential. The hydrogen-in-oxygen model (HTO model) comprehensively considers factors such as gas diffusion mass transfer across the diaphragm, pressure differential permeation mass transfer, and electrolyte mixing to effectively predict HTO (hydrogen-in-oxygen) content.

[0074] Step S102 , based on the electrochemical model and the hydrogen in oxygen model, polarization curves and isolines of hydrogen in oxygen concentration at different operating pressures, different temperatures, and different alkali solution flow rates are calculated, and a gas-liquid separation capability line is calculated simultaneously.

[0075] Specifically, a polarization curve represents the relationship between electrode potential and polarization current or polarization current density. When a chemical reaction occurs at an electrode, its electrode potential shifts as the reaction proceeds. This shift is reflected on the polarization curve as the relationship between potential and current (or current density). The polarization curve, abbreviated as the IU curve, is an important indicator for evaluating the static characteristics of an electrolytic cell and is affected by the cell's characteristic parameters and operating conditions.

[0076] Polarization curves and hydrogen-in-oxygen concentration contours are calculated using the electrochemical model and the hydrogen-in-oxygen model, respectively. The parameters are set based on the actual operating conditions of the hydrogen production system under different operating pressures, temperatures, and alkali flow rates.

[0077] The capacity of the gas-liquid separator is designed based on the estimated hydrogen production rate of the electrolyzer. This means the size of the gas-liquid separator is predetermined according to the operating conditions, and its separation capacity is fixed during the design phase and cannot be adjusted during operation. However, as the electrolysis reaction continues and system regulation is implemented, the system pressure may fluctuate, thereby affecting the actual hydrogen production rate. Therefore, the gas-liquid separation capacity of the gas-liquid separator must be calculated to ensure the safe operation of the hydrogen production system.

[0078] Step S103 : adding a boundary limit line to the polarization curve, and constructing a safe operation boundary envelope diagram based on the polarization curve with the boundary limit line added, the hydrogen concentration contour line in oxygen, and the gas-liquid separation ability line.

[0079] Specifically, the boundary limit lines are determined by the voltage and current of the power supply of the hydrogen production system, and may include: a maximum voltage limit line, a maximum current limit line, a minimum temperature limit line, a maximum temperature limit line, and a hydrogen concentration limit line in oxygen.

[0080] On the drawn polarization curve, accurately draw the maximum voltage limit line, maximum current limit line, minimum temperature limit line, maximum temperature limit line, and hydrogen concentration limit line determined above. These limit lines divide the area where the polarization curve is located into different parts, clarifying the safe boundary of the system operation. Integrate the polarization curve with the boundary limit line added with the isoline of hydrogen concentration in oxygen and the gas-liquid separation ability line. In a unified coordinate system, with current density as the horizontal coordinate and electrode potential as the vertical coordinate, display the polarization curve, boundary limit line, isoline of hydrogen concentration in oxygen, and gas-liquid separation ability line at the same time. Use different colors or line styles to distinguish different curves and isolines to form a safe operation boundary envelope diagram.

[0081] Step S104 , obtaining the minimum current, real-time operating current, and maximum current of the hydrogen production system, and calculating a safety margin based on the minimum current, real-time operating current, and maximum current.

[0082] Specifically, the minimum current of the hydrogen production system can be defined as the current corresponding to a hydrogen-in-oxygen concentration of 2% calculated using the hydrogen-in-oxygen model; the real-time operating current is defined as the real-time current provided to the electrolyzer in the hydrogen production system; the maximum current is defined as the maximum current that can be provided by the power supply end (or rectifier cabinet) in the hydrogen production system or the maximum load limit of the electrolyzer in the hydrogen production system.

[0083] For each combination of operating pressure and caustic soda flow rate, the corresponding safety margin is calculated by combining the real-time operating current, the minimum current calculated using the oxygen-hydrogen model, and the known maximum current. The safety margin intuitively displays the relationship between the real-time operating current and the maximum and minimum currents.

[0084] Step S105 : regulating the operating range of the hydrogen production system based on the safe operating boundary envelope diagram and the safety margin.

[0085] Specifically, by observing the safe operating boundary envelope diagram and safety margin, the impact of different operating pressures, alkali solution flow rates, and temperatures on the safe operating boundary envelope diagram and safety margin are analyzed. For example, the direction and amplitude of movement of the boundaries of each region in the safe operating boundary envelope diagram, as well as the changing trend of the safety margin, are observed when the operating pressure increases. The changes in the hydrogen concentration contours in oxygen as the alkali solution flow rate increases are analyzed, thereby affecting the scope of each region. Because the operating conditions of the hydrogen production system may change over time, the system's operating status is continuously monitored, and the operating pressure, alkali solution flow rate, and temperature are dynamically adjusted based on real-time feedback from the safe operating boundary envelope diagram and safety margin. For example, when the system load changes, resulting in a change in the real-time operating current, the operating parameters are adjusted in a timely manner based on the change in the safety margin to keep the system operating safely and efficiently.

[0086] The method for controlling the operating range of a hydrogen production system provided in this embodiment establishes an electrochemical model and a hydrogen-in-oxygen model, which can accurately simulate the core processes of the hydrogen production system. By calculating polarization curves, hydrogen-in-oxygen concentration contours, and gas-liquid separation capacity lines under different operating pressures, temperatures, and alkali liquid flow rates, the system operating status can be comprehensively monitored. Based on the observed changes in current, voltage, temperature, pressure, alkali liquid flow rate, and gas-liquid separation capacity, the safe operating boundary is plotted in the form of an HTO envelope diagram, thereby accurately determining the safe operating boundary of the alkali liquid hydrogen production system, obtaining the minimum current, real-time operating current, and maximum current of the hydrogen production system, calculating the safety margin based on the minimum current, real-time operating current, and maximum current, and effectively controlling the operating range of the hydrogen production system based on the safe operating boundary and safety margin, thereby solving the problems of unclear safe operating boundaries and insufficient control measures in the prior art.

[0087] In this embodiment, a method for controlling the operating range of a hydrogen production system is provided, which can be used in a hydrogen production system. Figure 2 FIG. 1 is a flow chart of a method for controlling the operating range of a hydrogen production system according to an embodiment of the present invention. Figure 2 As shown, the process includes the following steps:

[0088] Step S201 : establishing an electrochemical model and a hydrogen-in-oxygen model of a hydrogen production system.

[0089] Specifically, the above step S201 includes:

[0090] Step S2011, calculating the reversible electrolysis voltage, activation overpotential, ohmic overpotential and concentration difference overpotential during the operation of the hydrogen production system, and establishing an electrochemical model based on the reversible electrolysis voltage, activation overpotential, ohmic overpotential and concentration difference overpotential.

[0091] Specifically, the electrochemical model is represented by the cell voltage of the electrolytic cell, the cell voltage V cell By reversible electrolysis voltage V rev, cathode activation overpotential V act，c , anode activation overpotential V act，a , Ohmic overpotential V ohm As well as the concentration difference overpotential, the concentration difference overpotential can usually be ignored due to the low current density of alkaline water electrolysis (AWE) technology.

[0092] Battery voltage V cell The formula is as follows:

[0093] V cell =V rev +V act，c +V act，a +V ohm (1);

[0094] The formula for calculating the reversible electrolysis voltage is as follows:

[0095]

[0096] Wherein, R is the gas constant, R = 8.314 J / (mol·K); T is the reaction temperature; F is the Faraday constant (F = 96485); P is the electrolytic cell pressure; P H2O It represents the water vapor partial pressure, which can be expressed by an empirical formula related to the molar concentration of the alkali solution m and T. Since the parameters in the empirical formula contain model confidentiality, please refer to the detailed empirical formula of the relevant technology for details. H2O represents the activity of water, Represents the starting reversible electrolysis voltage.

[0097] The activation overpotential calculation formula is as follows:

[0098]

[0099] Where N represents the number of charges transferred when 1 mol of hydrogen is generated (N = 2); α a , α c They represent the charge transfer coefficients of the anode and cathode, respectively, which can be calculated by the empirical formula related to temperature; J is the current density; J 0，a 、J 0，c Represent the exchange current density of the anode and cathode respectively, where T0 and P0 represent the initial reference temperature and pressure respectively; θ is the bubble coverage rate on the electrode surface. Cathode activation overpotential V act，c , anode activation overpotential V act，a All are calculated using formula (3).

[0100] The formula for calculating the ohmic overpotential is as follows:

[0101] V ohm =(R c +R a +Rele +R mem +R bubble )×I / 2 (4);

[0102] The ohmic overpotential includes the anode resistance R a , cathode resistance R c , electrolyte resistance R ele , bubble resistance R bubble and diaphragm resistance R mem , I represents the electrolysis current.

[0103] Step S2012, calculate the hydrogen exchange flux, diffusion flux, convection flux, alkali solution mixing flux and oxygen production rate per unit time during the operation of the hydrogen production system, and establish a hydrogen-in-oxygen model based on the hydrogen exchange flux, diffusion flux, convection flux, alkali solution mixing flux and oxygen production rate per unit time.

[0104] Specifically, the hydrogen-in-oxygen (HTO) model: The hydrogen and oxygen produced during the electrolysis process initially exist in a dissolved state in the electrolyte. Affected by the environment, bubbles will move through the diaphragm to each other. The mixing of oxygen in hydrogen will cause the hydrogen purity to deteriorate, while the mixing of hydrogen in oxygen will limit the system's minimum allowable load and easily cause safety risks. Therefore, the HTO content during the operation of the hydrogen production system becomes a core indicator of concern. The HTO calculation formula is as follows:

[0105]

[0106] in, is the hydrogen exchange flux per unit time; is the hydrogen diffusion flux; is the convection flow; is the alkali solution mixing flux; is the oxygen production rate, n c is the number of electrolysis chambers.

[0107] The calculation formula of hydrogen diffusion flux is as follows:

[0108]

[0109] Among them, δ m Indicates the thickness of the diaphragm; represents the dissolved gas concentration gradient; It represents the solubility of hydrogen in KOH solution, and the formula is as follows:

[0110]

[0111] Among them, m KOH represents the molar concentration of the electrolyte; K is the Sechenov constant, whose value is related to the type of electrolyte and gas, and K=3.14; It represents the solubility of hydrogen in pure water, and the formula is as follows:

[0112]

[0113] in, is the water density; is the Henry coefficient of hydrogen, It represents the effective diffusion coefficient of hydrogen through the diaphragm. Since the diaphragm is filled with KOH solution, Diffusion coefficient of hydrogen in KOH solution The formula for the effective diffusion coefficient of hydrogen through the membrane is as follows:

[0114]

[0115] Among them, p m , τ m represent the membrane porosity and tortuosity, respectively.

[0116] The formula for calculating hydrogen convective flux is as follows:

[0117]

[0118] Where ΔP represents the pressure difference between the anode and cathode; η KOH Indicates the viscosity of KOH solution; K sep It represents the membrane permeability, which is closely related to the membrane parameters, including membrane porosity, tortuosity and pore size d m The relevant formula is expressed.

[0119] The calculation formula of hydrogen mixing flux is as follows:

[0120]

[0121] Among them, v lye Indicates the alkali solution flow rate.

[0122] The oxygen generation rate is calculated as follows:

[0123]

[0124] Among them, η F represents the Faraday efficiency.

[0125]

[0126] Where I is the current, A is the electrode area, and f1 and f2 are empirical parameters.

[0127] In addition, the effects of the established electrochemical model and hydrogen-in-oxygen model on the energy efficiency of the hydrogen production system are described in detail as follows:

[0128] First, the energy efficiency calculation formula of the hydrogen production system is established as follows:

[0129]

[0130] Among them, η sys Indicates system efficiency, in %. The higher the value, the higher the efficiency of converting electrical energy into hydrogen. Indicates the hydrogen generation rate, LHV is the lower heating value of hydrogen, which is 242×103 (J / mol), W com is the power of the hydrogen compressor. The calculation method of its value varies depending on the compressor used. W cell is the power of the electrolytic cell, and the calculation formula is as follows:

[0131] W cell =n c ×I×V cell (15);

[0132] Based on the system energy efficiency calculation formula, electrochemical model and oxygen-hydrogen model, the input-output relationship diagram can be obtained, such as Figure 7 As shown, the input pressure, alkali solution flow rate and temperature are input to the electrochemical model and the hydrogen in oxygen model, and the corresponding voltage and hydrogen in oxygen concentration values are output. The voltage and hydrogen in oxygen concentration values, as well as the input pressure, Jianye flow rate, current, temperature and other physical parameters are input into the energy efficiency calculation formula. The hydrogen in oxygen (HTO) concentration value is constrained to be less than or equal to 2%, and the optimal system energy efficiency is required to be obtained under the conditions of the input voltage, pressure, Jianye flow rate, current, temperature and other physical parameters.

[0133] Based on the above input-output relationship of system energy efficiency, multiple sets of optimal values of pressure and alkali solution flow rate within the load range (if the electrolytic cell can withstand a maximum of 3500A, the load range is 0 to 3500A) can be obtained.

[0134] This is the method of regulating the system energy efficiency by adjusting the pressure and alkali solution flow rate to ensure that the system energy efficiency is always at the best level. Figure 8 Shown and Figure 9 As shown, Figure 8 This is a schematic diagram showing how the system energy efficiency is always at its best within the load range and under the premise of HTO ≤ 2%. Figure 9 Schematic diagram of the changes in system energy efficiency and HTO with load within the load range.

[0135] Step S202 , based on the electrochemical model and the hydrogen in oxygen model, polarization curves and isolines of hydrogen in oxygen concentration at different operating pressures, different temperatures, and different alkali solution flow rates are calculated, and a gas-liquid separation capability line is calculated simultaneously.

[0136] Specifically, the above step S202 includes:

[0137] In step S2021, different operating pressures, different temperatures, and different alkali solution flow rates are input into the electrochemical model to obtain polarization curves corresponding to the different operating pressures, different temperatures, and different alkali solution flow rates.

[0138] Polarization curve calculation: First, determine a series of different combinations of operating pressure (P), temperature (T) and alkali flow rate (Q). For example, the operating pressure can be selected from multiple values in the range of 0.1-1.0MPa, the temperature can be set with different gradients between 30-90°C, and the alkali flow rate can be changed from 0.1-1.0L / min. Each operating parameter combination is input into the electrochemical model separately. Under each operating parameter combination, a series of data points are obtained by iteratively calculating the relationship between the electrode potential and the current density in the electrochemical model. These data points are connected to draw polarization curves corresponding to different operating pressures, temperatures and alkali flow rates. For example, at a specific operating pressure, temperature and alkali flow rate, starting from a low current density, gradually increasing the current density, calculating the corresponding electrode potential, obtaining a set of (i, E) data, and finally drawing a polarization curve.

[0139] In step S2022, different operating pressures, different temperatures, and different alkali solution flow rates are input into the hydrogen in oxygen model to obtain isovalues of hydrogen in oxygen concentration corresponding to the different operating pressures, different temperatures, and different alkali solution flow rates.

[0140] Calculation of isovalue lines of hydrogen concentration in oxygen: Use the same series of operating pressure, temperature and alkali solution flow combinations as those used for polarization curve calculation. Input each operating parameter combination into the hydrogen in oxygen model, solve the mass conservation equation of the hydrogen in oxygen model by numerical methods, and obtain the spatial distribution of hydrogen concentration in oxygen under different operating parameters. In two-dimensional or three-dimensional space, select a series of hydrogen concentration values in oxygen and draw the corresponding isovalue lines. For example, on a plane, the hydrogen concentration in oxygen at different positions is obtained by calculation. For a specific hydrogen concentration value in oxygen (such as 0.5%), connect all points with concentration values equal to this value to form an isovalue line of hydrogen concentration in oxygen. By drawing multiple isovalue lines of different concentration values, the distribution of hydrogen concentration in oxygen under different operating conditions is displayed.

[0141] Step S2023 , calculating the gas-liquid separation capacity line based on the diameter and length of the gas-liquid separator in the hydrogen production system and the gas-liquid variable parameters under different operating pressures, different temperatures, and different alkali solution flow rates.

[0142] Specifically, in engineering applications, the capacity matching of the gas-liquid separator is designed based on the estimated hydrogen production rate of the electrolyzer, that is, the size of the gas-liquid separator is predetermined according to the working conditions, and its separation capacity is fixed in the design stage and cannot be adjusted during operation. However, as the electrolysis reaction continues and the system is regulated, the system pressure may change, thereby affecting the actual hydrogen production rate. For the convenience of calculation, the hydrogen volume flow rate at the outlet of the electrolyzer is directly compared with the separation capacity of the gas-liquid separator to quantitatively analyze the constraint effect of the gas-liquid separator on the operating range of the system. According to relevant chemical industry standards, the key parameters in the design of horizontal gravity separators are the diameter and length of the separator, which are expressed as D and L, respectively. T and L N The calculation method is as shown in formula (16) and formula (17), and the formula is as follows:

[0143]

[0144] Among them, V L represents the volume flow rate of the liquid, t represents the residence time of the liquid, C represents the ratio of diameter to length, A represents the variable liquid area in the separator.

[0145]

[0146] Among them, L′ N Indicates the distance between the inlet and outlet pipes of the gas-liquid separator, D' T represents the diameter of the gas-liquid separator, a represents the height of the gas space, V G represents the gas flow rate, ρ L , ρ G Represent the density of alkali solution and the density of hydrogen respectively, A a Represents the cross-sectional area of the gas portion of the gas-liquid separator, R represents the droplet diameter coefficient, R = τ a / τ T , when the droplet diameter d * =350μm, R=0.167, d * =200μm, R=0.127. The gas-liquid variable parameters include gas flow rate, gas liquid density, droplet diameter coefficient, gas space height and cross-sectional area of the gas part.

[0147] Step S203 : adding a boundary limit line to the polarization curve, and constructing a safe operation boundary envelope diagram based on the polarization curve with the boundary limit line added, the hydrogen concentration contour line in oxygen, and the gas-liquid separation ability line.

[0148] Specifically, the boundary limit lines include a maximum voltage limit line, a maximum current limit line, a minimum temperature limit line, a maximum temperature limit line, and a hydrogen concentration limit line in oxygen; the above step S203 includes:

[0149] Step S2031 : adding a maximum voltage limit line, a maximum current limit line, a minimum temperature limit line, a maximum temperature limit line, and a hydrogen concentration limit line in oxygen to the polarization curve.

[0150] 4(a), 4(b), 4(c) and 5(a), 5(b), 5(c), ① is the maximum voltage limit line, which is defined as the maximum voltage that the power supply end (or rectifier cabinet) in the hydrogen production system can provide; ② is the maximum current limit line, which is defined as the maximum current that the power supply end (or rectifier cabinet) in the hydrogen production system can provide or the maximum load limit of the electrolyzer in the hydrogen production system; ③ is the minimum temperature limit line, which is defined as 0°C or any manually defined temperature (must be less than the maximum temperature limit line); ④ is the maximum temperature limit line, which is defined as 95°C or any manually defined temperature (must be greater than the minimum temperature limit line); ⑤ is the hydrogen in oxygen concentration limit line, which is defined as the current corresponding to a hydrogen in oxygen concentration of 2% calculated using the above-mentioned hydrogen in oxygen model.

[0151] We have added various boundary limit lines to the polarization curve, resulting in a polarization curve graph that includes lines for maximum voltage, maximum current, minimum and maximum temperatures, and hydrogen-in-oxygen concentration. We also provide contour plots of hydrogen-in-oxygen concentration at different operating pressures, temperatures, and caustic soda flow rates.

[0152] Step S2032: construct a safe operation boundary envelope diagram based on the polarization curve, the maximum voltage limit line, the maximum current limit line, the minimum temperature limit line, the maximum temperature limit line, and the hydrogen concentration limit line in oxygen, the hydrogen concentration contour line, and the gas-liquid separation ability line.

[0153] Specifically, in order to make the safe operation boundary envelope diagram clear and easy to understand, different colors, line styles or marks are used to distinguish the polarization curves, various boundary limit lines and isolines of hydrogen concentration in oxygen. As shown in Figure 4(a), Figure 4(b) and Figure 4(c), the axis names, units and scale values are clearly marked on the horizontal and vertical axes (electrode potential axes) of the envelope diagram. For isolines of hydrogen concentration in oxygen, legends are added at appropriate locations in the figure to explain the hydrogen concentration values in oxygen represented by different colors or line styles. At the same time, in the title or annotation part of the figure, key information such as the type of hydrogen production system and the range of operating conditions corresponding to the envelope diagram is briefly described so that users can accurately understand the meaning of the graphic.

[0154] By observing the distribution of various boundary limit lines and isovalue lines of hydrogen concentration in oxygen in the envelope diagram, the boundary of the safe operating area is determined. The safe operating area is usually a closed or semi-closed area surrounded by the maximum voltage limit line, the maximum current limit line, the minimum temperature limit line, the maximum temperature limit line and the hydrogen concentration limit line in oxygen. In this area, the operating parameters of the system (current density, electrode potential, temperature and hydrogen concentration in oxygen, etc.) meet the safety and performance requirements. Use fill color or special mark to highlight the safe operating area. As shown in Figure 4 (a), Figure 4 (b) and Figure 4 (c), when the operating pressure is 1.6Mpa, 1.0Mpa and 0.6Mpa respectively, the alkali solution flow rate is 3m 3 / h、5m 3 / h and 7m 3 / h, and the temperatures are 0℃, 15℃, 35℃, 75℃ and 95℃ respectively, with the vertical axis being the voltage value and the horizontal axis being the current value.

[0155] In step S2033, the hydrogen concentration in oxygen includes a first threshold, a second threshold, and a third threshold, and the values of the first threshold, the second threshold, and the third threshold decrease in sequence; the area outside the safe operation boundary envelope diagram is called a danger zone; the area within the safe operation boundary envelope diagram where the hydrogen concentration in oxygen ranges from the second threshold to the first threshold is used as a warning zone; the area within the safe operation boundary envelope diagram where the hydrogen concentration in oxygen ranges from the third threshold to the second threshold and is less than the gas-liquid separation ability line is used as a safe zone.

[0156] Specifically, in the embodiment of the present invention, the first threshold, the second threshold, and the third threshold are set to 2%, 1.5%, and 0%, respectively.

[0157] The range outside the safe operation boundary envelope is called the danger zone, the range of 1.5% to 2% of hydrogen in oxygen within the safe operation boundary envelope is called the warning zone, and the area within the safe operation boundary envelope where the hydrogen in oxygen concentration ranges from 0% to 1.5% and is less than the gas-liquid separation capacity line (such as Figure 10 The dotted line shown is the gas-liquid separation ability line, and the area to the left (the area smaller than the gas-liquid separation ability line) is called the safety zone.

[0158] From formula (17), it can be found that after confirming the diameter and length of the horizontal gravity separator, the gas-liquid variable parameters only include the gas flow rate, the gas liquid density, the droplet diameter coefficient, the gas space height, and the cross-sectional area of the gas part. According to the standard operating condition parameter design of the electrolyzer, that is, the hydrogen flow rate of a 250kW electrolyzer at 3500A current, 1.6MPa pressure, and 95℃ operating temperature is 4.788m 3 / h, considering 20% margin, it is 5.746m 3 / h. It should be noted that when the hydrogen production rate is too high and the gas stays in the gas-liquid separator for too short a time, incompletely separated gas may flow back into the electrolyzer along with the alkaline solution. At the same time, alkaline droplets in hydrogen and oxygen may enter the downstream washing, drying, and purification stages along with the gas, shortening the lifespan and reliability of downstream components and purification, affecting system reliability, safety, and gas purity.

[0159] For the convenience of calculation, the following assumptions are made: ① The flow rate of hydrogen at the outlet of the electrolyzer will not change after it flows into the gas-liquid separator; ② It is assumed that the alkali liquid droplets in the gas-liquid separator are always kept at 200μm; ③ It is assumed that the height of the gas space in the separator is always half of the diameter of the gas-liquid separator. Based on the above assumptions and equations (16) and (17), the diameter and length of the gas-liquid separator are determined, and then the limiting effect of its separation capacity on the operating range of the system is analyzed. The safe operation envelope diagram of the AWE hydrogen production system affected by the separation capacity of the gas-liquid separator (1.0MPa, 3m^3 / h, 0.6MPa, 3m^3 / h) is shown as follows Figure 10 As shown; and the current safety operating range diagram affected by the separation capacity of the gas-liquid separator (1.0MPa, 3m^3 / h, 0.6MPa, 3m^3 / h) is shown as Figure 11 shown.

[0160] According to the above, the hydrogen flow rate remains unchanged, and according to the model introduction in step S201, the change of the alkali solution flow rate will not affect the hydrogen flow rate. 3 / h, the impact of different pressures on the system operating range. It should be noted that the horizontal gravity gas-liquid separator is designed for a 1.6 MPa pressure condition, with a 20% margin reserved. Therefore, system operation at this pressure level is not constrained by separator capacity. The main focus is on the changes in the system operating range under 1.0 MPa and 0.6 MPa conditions.

[0161] like Figure 10 and Figure 11As shown in the figure, the influence of the separation capacity of the gas-liquid separator on the safe operating range of the system is represented by a dotted line in the figure, that is, the gas-liquid separator limit line. The hydrogen production rate corresponding to the area to the right of the dotted line exceeds the separation capacity of the gas-liquid separator and is called the inoperable area. Under the premise of a pressure of 1.0MPa and an alkali liquid flow rate of 3m^3 / h, when the temperature is 95℃, the safe operating range is reduced from [825A, 3500A] to [825A, 3175A] due to the limitation of the separation capacity of the gas-liquid separator, a reduction of 12.1%. When the temperature is 75℃, the safe operating range is reduced from [750A, 3500A] to [750A, 3350A], a reduction of 5.5%. As the temperature drops to 60.5℃, the gas-liquid separator limitation disappears, and the temperature influence range is [60.5℃ ,95℃]; under the premise of pressure of 0.6MPa and alkali solution flow rate of 3m^3 / h, when the temperature is 95℃, the safe operating range is reduced from [500A,3500A] to [500A,1900A], with a reduction of 53.3%. When the temperature is 55℃, the safe operating range is reduced from [375A,3500A] to [375A,2125A], with a reduction of 44.0%. As the temperature drops to 24.5℃, the gas-liquid separator limitation disappears, and the temperature influence range is [24.5℃,95℃].

[0162] From a pressure control perspective, the temperature range restricted by the gas-liquid separator is wider at 0.6 MPa than at 1.0 MPa, reaching 70.5°C. Furthermore, the safe operating range is significantly reduced at 0.6 MPa due to the gas-liquid separator's restriction. As the pressure decreases from 1.0 MPa to 0.6 MPa, the gas-liquid separator's restriction increases from [3175A, 3500A] to [1900A, 3500A] at 95°C, representing 36.4% of the rated current. At 60.5°C, the gas-liquid separator's restriction increases from [0A, 0A] to [2070A, 3500A], representing 40.9% of the rated current. It's important to note that increasing system pressure helps reduce the gas-liquid separator's constraints on the safe operating range. However, at low pressure, the gas-liquid separator's temperature range is wider, significantly reducing the operable range. Although lowering the pressure at high temperature can optimize gas purity and thus widen the safe operating range, due to the limitations of the gas-liquid separator's separation capacity, the pressure drop itself cannot widen the safe operating range. Instead, it expands the restricted area, which has a more significant impact on system operation.

[0163] It should be noted that although a large-capacity gas-liquid separator will weaken the limitation of separation capacity, it will worsen the thermal mass hysteresis, thereby increasing the difficulty of dynamic regulation.

[0164] In alkaline hydrogen production systems, the core difference between one-to-one and many-to-one hydrogen production systems lies in the system integration and applicable scenarios: the one-to-one system adopts an independent modular design (single electrolyzer adapted to a single post-processing system), with flexible deployment and strong fault isolation, suitable for small-scale or distributed scenarios, but with higher costs and lower energy efficiency; while the many-to-one hydrogen production system has scale cost advantages, dynamic load adjustment capabilities, and higher redundancy by sharing a single post-processing system among multiple electrolyzers, suitable for large-scale scenarios such as industrial-grade hydrogen production or coupling with renewable energy, but with high initial investment, complex operation and maintenance, and the need to guard against centralized failure risks. In the many-to-one hydrogen production system scenario, the gas-liquid separator limit remains the same as in the one-to-one scenario. This is because the pressure of each electrolyzer in the many-to-one system is consistent with that in the gas-liquid separator. The separator also considers the hydrogen production rate of multiple electrolyzers and retains a margin when designing it. When regulating the pressure, the change in the hydrogen production rate is consistent with the number of electrolyzers. To sum up, when making a choice, you need to weigh production capacity requirements, cost budget and technical capabilities. If you are pursuing long-term scale benefits and high output, many-to-one has more potential, while one-to-one is preferred in decentralized, low-risk scenarios.

[0165] Step S204: Obtain the minimum current, real-time operating current, and maximum current of the hydrogen production system, and calculate the safety margin based on the minimum current, real-time operating current, and maximum current. Figure 1 Step S104 of the illustrated embodiment will not be described in detail here.

[0166] Step S205: Regulate the operating range of the hydrogen production system based on the safe operating boundary envelope diagram and the safety margin. Figure 1 Step S105 of the illustrated embodiment will not be described in detail here.

[0167] The method for controlling the operating range of the hydrogen production system provided in this embodiment comprehensively considers the various fluxes of hydrogen transmission and the oxygen-in-hydrogen model established by the oxygen production rate, which provides a strong guarantee for the safe operation of the hydrogen production system. By inputting different operating pressures, temperatures and alkali solution flows into the electrochemical model respectively, the corresponding polarization curves under each operating condition can be accurately obtained. Based on the polarization curves under different operating conditions, performance comparison analysis can be performed. It can be clearly determined under which operating pressure, temperature and alkali solution flow combination the electrochemical reaction efficiency of the hydrogen production system is the highest and the energy consumption is the lowest. By inputting different operating parameters into the oxygen-in-hydrogen model to obtain the corresponding oxygen-in-hydrogen concentration contour line, the safety risks of the hydrogen production system under different operating conditions can be accurately assessed. In the hydrogen production process, the gas-liquid separation capacity line of the gas-liquid separator is also taken into account, laying the foundation for dynamic safety monitoring of the hydrogen production system. The safe operation boundary envelope diagram integrates the boundary limit line of the polarization curve and the oxygen-in-hydrogen concentration contour line, which can identify potential safety risks in advance. By observing the position of the operating point in the envelope diagram, it can be determined whether the system is close to or exceeds the safety boundary. As the hydrogen production system operates over time, the changing trend of the operating risk of the hydrogen production system can be analyzed by continuously observing the movement trajectory of the operating point in the safe operation boundary envelope diagram.

[0168] In this embodiment, a method for controlling the operating range of a hydrogen production system is provided, which can be used in a hydrogen production system. Figure 3 FIG. 1 is a flow chart of a method for controlling the operating range of a hydrogen production system according to an embodiment of the present invention. Figure 3 As shown, the process includes the following steps:

[0169] Step S301: Establish an electrochemical model and an oxygen-hydrogen model for the hydrogen production system. Figure 2 Step S201 of the illustrated embodiment will not be described in detail here.

[0170] Step S302: Based on the electrochemical model and the hydrogen in oxygen model, the polarization curves and the isoline of hydrogen in oxygen concentration at different operating pressures, temperatures and alkali solution flow rates are calculated, and the gas-liquid separation capacity line is also calculated. Figure 2 Step S202 of the illustrated embodiment will not be described in detail here.

[0171] Step S303: Add boundary limit lines to the polarization curve, and construct a safe operation boundary envelope diagram based on the polarization curve with boundary limit lines added, the hydrogen concentration contour line in oxygen, and the gas-liquid separation ability line. Figure 2 Step S203 of the illustrated embodiment will not be described in detail here.

[0172] Step S304 : obtaining the minimum current, real-time operating current, and maximum current of the hydrogen production system, and calculating a safety margin based on the minimum current, real-time operating current, and maximum current.

[0173] Specifically, the above step S304 includes:

[0174] Step S3041 : Calculate the minimum current of the hydrogen production system based on the hydrogen in oxygen model.

[0175] Specifically, in the hydrogen-in-oxygen model, a strict upper limit is set for the hydrogen-in-oxygen concentration based on safety standards. For example, the volume fraction of hydrogen in oxygen must not exceed Cmax = 2%. This upper limit serves as a key safety constraint for calculating the minimum current.

[0176] Given a series of initial operating pressure, temperature and alkali solution flow combinations. The operating pressure can be selected in the range of 0.1MPa-1.0MPa, the temperature can be set in the range of 0℃-90℃, and the alkali solution flow rate can be set from 3m 3 / h-10m 3 / h. These initial parameter combinations represent possible operating conditions for the hydrogen production system. The above initial operating parameters are input into the hydrogen-in-oxygen model. Starting from a low current density, the current density value is gradually increased while monitoring the calculated results of the hydrogen-in-oxygen concentration. When the hydrogen-in-oxygen concentration reaches the pre-set maximum allowable value Cmax = 2%, the corresponding current density is the minimum current of the hydrogen production system under this specific operating pressure, temperature and alkali solution flow combination.

[0177] As shown in Figure 5(a), Figure 5(b) and Figure 5(c), when the alkali solution flow rate is 3m 3 / h、5m 3 / h and 7m 3 The safe operating range of current is obtained by combining the operating pressures of 1.6 MPa, 1.0 MPa, and 0.6 MPa, and the temperatures of 0°C, 15°C, 35°C, 75°C, and 95°C. The vertical axis is temperature, and the horizontal axis is current.

[0178] Step S3042 : Calculate the uplink safety margin and the downlink safety margin based on the minimum current, the real-time operating current, and the maximum current.

[0179] Specifically, uplink safety margin = maximum current A1 - real-time operating current A;

[0180] Downstream safety margin = real-time operating current A - minimum current A2.

[0181] In step S305, the corresponding uplink safety margin and downlink safety margin are calculated based on the uplink safety margin and downlink safety margin under different operating pressures and different alkali solution flow rates, and the relationship between the real-time operating current and the maximum current and the minimum current is displayed based on the uplink safety margin and the downlink safety margin.

[0182] Specifically, uplink safety margin = (maximum current A1 - real-time operating current A) / (maximum current A1 - minimum current A2);

[0183] Downstream safety margin = (real-time operating current A - minimum current A2) / (maximum current A1 - minimum current A2).

[0184] like Figure 6 As shown in the figure, the horizontal axis shows the time variation for different combinations of operating pressure and alkali solution flow rate, and the vertical axis shows the safety margin value. The calculated safety margins under different operating conditions are plotted as contour lines on the graph. Different colors or line styles represent different safety margin values, forming a safety margin diagram. This diagram intuitively shows the distribution of the system's safety margin under different operating pressures and alkali solution flow rates, providing an intuitive reference for regulating the system's operating range. Figure 6 In order to show the fluctuation of the real-time running current, a random number between 0 and 1 is taken as the maximum current.

[0185] In the embodiment of the present invention, the safety margin ranges from 0 to 1, that is, the fourth threshold is 0 and the fifth threshold is 1. The area where the safety margin is less than 0 is regarded as a danger zone. That is, when the safety margin is below 0, it indicates that the hydrogen concentration in oxygen in the current hydrogen production system has exceeded 2%, and safety regulation is required.

[0186] The median of 0 and 1 is 1 / 2, and the range from 0 to 1 / 2 is used as the warning zone. That is, when the safety margin is close to 0, it means that the current (real-time current) received by the electrolyzer in the hydrogen production system is close to the minimum current (minimum load limit), indicating that the current operating conditions of the hydrogen production system are relatively dangerous.

[0187] The range from 1 / 2 to 1 is regarded as the safety zone. That is, when the safety margin is close to 1, it indicates that the current received by the electrolyzer in the hydrogen production system (real-time operating current) is far from the minimum current (minimum load limit), indicating that the current operating conditions of the hydrogen production system are relatively safe.

[0188] For example, if the maximum current is 3500, the minimum current is 0, and the operating current is 2000, the safety margin is calculated to be 0.5714, which is in the middle. If the operating current is 100, the safety margin is 0.0285, which is very close to 0 and is in the warning zone. In other words, the safety margin determines how close the real-time current is to the minimum current.

[0189] It should be noted that the role of the safety margin is the same as that of the safety margin, both of which are to show the changing relationship between the real-time operating current and the maximum current and the minimum current respectively. According to the safety margin diagram, the changing relationship between the real-time operating current and the maximum current and the minimum current respectively can be seen more intuitively. The safety margin and the safe operation boundary envelope diagram are the main control indicators. The safety margin is reflected in the safe operation boundary envelope diagram, which limits the safe area in the hydrogen production process of the hydrogen production system.

[0190] Step S306 : regulating the operating range of the hydrogen production system based on the safe operating boundary envelope diagram and the safety margin.

[0191] Specifically, the influence of different operating pressures, different alkali liquid flow rates and different temperatures on the safety zone, danger zone, warning zone, as well as the upward safety margin and downward safety margin are analyzed, and the operating pressure, alkali liquid flow rate and temperature of the hydrogen production system are regulated based on the influence rules.

[0192] As shown in Figures 4(a), 4(b), and 4(c) and Figures 5(a), 5(b), and 5(c), the system's operating status is continuously monitored and recorded under different combinations of operating pressures, alkali solution flow rates, and temperatures. Sensors collect key data such as real-time operating current and hydrogen-in-oxygen concentration. A safety margin is calculated using the safety margin formula. Based on the hydrogen-in-oxygen concentration, the system determines the hydrogen-in-oxygen concentration zone (safe zone, warning zone, or danger zone), as well as the upward and downward safety margins. Data analysis tools such as multivariate linear regression and machine learning algorithms (e.g., decision trees and neural networks) are used to establish mathematical models of the relationships between operating pressure, alkali solution flow rate, temperature, and the ranges of each zone. Visualization software (e.g., Matplotlib and Tableau) is used to display the relationships between operating parameters and each zone in the form of three-dimensional graphs or two-dimensional contour maps. In the three-dimensional graph, with operating pressure, alkali liquid flow rate, and temperature as coordinate axes and the scope of each region (such as area, volume, etc.) as the dependent variable, the changing trends of each region (safety zone, warning zone, danger zone, upward safety margin, and downward safety margin) under different parameter combinations are intuitively presented as the influencing rules.

[0193] Formulate automatic control strategies based on the influencing rules. If the system predicts that it will enter the danger zone, and analysis shows that it is caused by excessively high operating pressure, the automatic control system can reduce the operating pressure according to pre-set rules. For example, by adjusting the pressure regulating valve, the operating pressure is reduced at a rate of 0.05MPa / min, and the alkali solution flow rate and temperature are adjusted according to the model prediction to maintain the system operating in a safe area. If it is found that the system approaches the danger zone due to abnormal alkali solution flow rate, the automatic control system can adjust the speed of the alkali solution pump and change the alkali solution flow rate. For example, when the model determines that the alkali solution flow rate is too large, the speed of the alkali solution pump is automatically reduced to keep the alkali solution flow rate at 0.05m3 / h rate is reduced while monitoring the system status to ensure that the system returns to the safe area after adjustment.

[0194] For example, (a) in terms of pressure control, a vertical comparison of the sub-graphs in Figures 4(a), 4(b), and 4(c) and Figures 5(a), 5(b), and 5(c) shows that pressure significantly affects the safe operating range. It is clear that an increase in pressure shrinks the safe range and increases the warning range, and the impact is greater at high temperatures than at low temperatures. At high alkali flow rates, pressure is more sensitive to the safe operating range because the hydrogen content in oxygen is relatively high at high alkali flow rates, approaching the 2% safety limit as pressure increases, causing more safe operating areas to become warning or dangerous zones. Therefore, when the system allows, the pressure can be appropriately reduced to expand the operating range, but the limitations of the gas-liquid separator's separation capacity must be considered.

[0195] (b) In terms of alkali solution flow control, a horizontal comparison of the sub-graphs of Figure 4(a), Figure 4(b), Figure 4(c) and Figure 5(a), Figure 5(b), and Figure 5(c) shows that an increase in the alkali solution flow rate will slightly reduce the safe area and slightly increase the warning area. In addition, the pressure change at high alkali solution flow rate has a greater impact on the safe operating area. Therefore, the problem of the reduction of the safe operating area caused by pressure can be alleviated by appropriately reducing the alkali solution flow rate.

[0196] (c) In terms of temperature control, horizontal and vertical comparisons of the sub-graphs show that increasing temperature gradually expands the safe operating range from 0°C to a specific value (40.5°C-42°C), then gradually shrinks to 95°C. Furthermore, the expansion / shrinkage rate decreases as the alkali solution flow rate increases. From Figures 4(a), 4(b), 4(c), and 5(a), 5(b), and 5(c), it can be seen that each operating condition has a temperature inflection point, and under these pressure and alkali solution flow conditions, the temperature inflection point has the widest system safe operating range. This temperature inflection point is defined as the "minimum full-production temperature." Therefore, raising the temperature to this point during the initial cold start can shorten the cold start time and widen the safe operating range, making subsequent adjustment of other parameters more convenient.

[0197] The method for regulating the operating range of the hydrogen production system provided in this embodiment analyzes the influence of different operating pressures, alkali liquid flow rates and temperatures on the six areas, which allows operators and managers to accurately grasp the risk changes of the hydrogen production system under different working conditions. Regulation is carried out based on these influence laws, and system risks are controlled from multiple dimensions such as operating pressure, alkali liquid flow rate and temperature. By studying the influence laws, it is possible to find the operating pressure, alkali liquid flow rate and temperature combination that is most suitable for safe and efficient operation of the system. Under the premise of ensuring that the system is in a safe area (such as a safe zone and a safe zone), these parameters are adjusted to improve the efficiency of hydrogen production.

[0198] This embodiment also provides a hydrogen production system operating range control device, which is used to implement the above-mentioned embodiments and preferred embodiments. Details already described are not repeated here. As used below, the term "module" may refer to a combination of software and / or hardware that implements a predetermined function. Although the devices described in the following embodiments are preferably implemented in software, implementation using hardware, or a combination of software and hardware, is also possible and contemplated.

[0199] This embodiment provides a device for controlling the operating range of a hydrogen production system. Figure 12 Shown, including:

[0200] Model building module 1201, used to build an electrochemical model and a hydrogen-in-oxygen model of the hydrogen production system;

[0201] The limit line calculation module 1202 is used to calculate the polarization curve and the hydrogen-in-oxygen concentration contour line under different operating pressures, different temperatures and different alkali solution flow rates based on the electrochemical model and the hydrogen-in-oxygen model, and simultaneously calculate the gas-liquid separation ability line;

[0202] A safe operation boundary envelope diagram construction module 1203 is used to add boundary limit lines to the polarization curve, and construct a safe operation boundary envelope diagram based on the polarization curve with the boundary limit lines added, the hydrogen concentration contour line in oxygen, and the gas-liquid separation ability line;

[0203] A safety margin calculation module 1204 is configured to obtain the minimum current, real-time operating current, and maximum current of the hydrogen production system, and calculate the safety margin based on the minimum current, real-time operating current, and maximum current;

[0204] The hydrogen production system operating range control module 1205 is used to control the hydrogen production system operating range based on the safe operation boundary envelope diagram and the safety margin.

[0205] In some optional implementations, the model building module 1201 includes:

[0206] The electrochemical model establishment unit is used to calculate the reversible electrolysis voltage, activation overpotential, ohmic overpotential and concentration difference overpotential during the operation of the hydrogen production system, and to establish an electrochemical model based on the reversible electrolysis voltage, activation overpotential, ohmic overpotential and concentration difference overpotential.

[0207] The hydrogen-in-oxygen model establishment unit is used to calculate the hydrogen exchange flux, diffusion flux, convection flux, alkali solution mixing flux and oxygen production rate per unit time during the operation of the hydrogen production system, and establish the hydrogen-in-oxygen model based on the hydrogen exchange flux, diffusion flux, convection flux, alkali solution mixing flux and oxygen production rate per unit time.

[0208] In some optional implementations, the limit line calculation module 1202 includes:

[0209] The polarization curve calculation unit is used to input different operating pressures, different temperatures and different alkali solution flow rates into the electrochemical model to obtain polarization curves corresponding to different operating pressures, different temperatures and different alkali solution flow rates.

[0210] The hydrogen concentration isoline calculation unit in oxygen is used to input different operating pressures, different temperatures and different alkali solution flow rates into the hydrogen concentration model to obtain the hydrogen concentration isoline in oxygen corresponding to the different operating pressures, different temperatures and different alkali solution flow rates.

[0211] The gas-liquid separation capacity line calculation unit is used to calculate the gas-liquid separation capacity line based on the diameter and length of the gas-liquid separator in the hydrogen production system and the gas-liquid variable parameters under different operating pressures, different temperatures and different alkali liquid flow rates.

[0212] In some optional embodiments, the boundary limit lines include a maximum voltage limit line, a maximum current limit line, a minimum temperature limit line, a maximum temperature limit line, and a hydrogen concentration limit line in oxygen; and the safe operation boundary envelope diagram construction module 1203 includes:

[0213] The limit line adding unit is used to add a maximum voltage limit line, a maximum current limit line, a minimum temperature limit line, a maximum temperature limit line and a hydrogen concentration limit line in oxygen to the polarization curve.

[0214] The safe operation boundary envelope diagram construction unit is used to construct the safe operation boundary envelope diagram based on the polarization curve to which the maximum voltage limit line, the maximum current limit line, the minimum temperature limit line, the maximum temperature limit line and the hydrogen concentration limit line in oxygen are added, the hydrogen concentration contour line in oxygen and the gas-liquid separation ability line.

[0215] In some optional embodiments, the hydrogen concentration in oxygen includes a first threshold, a second threshold, and a third threshold, and the values of the first threshold, the second threshold, and the third threshold decrease in sequence; the safe operation boundary envelope diagram construction module 1203 further includes:

[0216] The danger zone, warning zone and safety zone determination unit is used to define the area outside the safe operation boundary envelope diagram as a danger zone; define the area within the safe operation boundary envelope diagram from the second threshold value to the first threshold value of the hydrogen concentration in oxygen as a warning zone; and define the area within the safe operation boundary envelope diagram from the third threshold value to the second threshold value of the hydrogen concentration in oxygen and less than the gas-liquid separation ability line as a safety zone.

[0217] In some optional implementations, the safety margin includes an uplink safety margin and a downlink safety margin; the safety margin calculation module 704 includes:

[0218] The minimum current calculation unit is used to calculate the minimum current of the hydrogen production system based on the hydrogen in oxygen model.

[0219] The safety margin calculation unit is used to calculate the uplink safety margin and the downlink safety margin respectively based on the minimum current, the real-time operating current and the maximum current.

[0220] In some optional embodiments, the hydrogen production system operating range control device further includes:

[0221] The safety margin calculation module is used to calculate the corresponding upstream safety margin and downstream safety margin respectively under different operating pressures and different alkali solution flow rates based on the upstream safety margin and downstream safety margin; based on the upstream safety margin and downstream safety margin, it displays the changing relationship between the real-time operating current and the maximum current and minimum current respectively.

[0222] In some optional embodiments, the hydrogen production system operating range control module 1205 includes:

[0223] The hydrogen production system operating range control unit is used to analyze the impact of different operating pressures, different alkali liquid flow rates and different temperatures on the safety zone, danger zone, warning zone, as well as the upward safety margin and downward safety margin, and to control the operating pressure, alkali liquid flow rate and temperature of the hydrogen production system based on the impact rules.

[0224] The further functional description of each of the above modules and units is the same as that of the above corresponding embodiments and will not be repeated here.

[0225] The hydrogen production system operating range control device in this embodiment is presented in the form of a functional unit, where the unit refers to an ASIC (Application Specific Integrated Circuit) circuit, a processor and memory that executes one or more software or fixed programs, and / or other devices that can provide the above functions.

[0226] The embodiment of the present invention also provides a computer device having the above Figure 12 The operating range control device of the hydrogen production system is shown.

[0227] See also Figure 13 , Figure 13 is a structural diagram of a computer device provided by an optional embodiment of the present invention, such as Figure 13As shown, the computer device includes: one or more processors 10, memory 20, and interfaces for connecting various components, including high-speed interfaces and low-speed interfaces. Various components utilize different buses to communicate with each other and can be installed on a common mainboard or installed in other ways as needed. The processor can process the instructions executed in the computer device, including instructions stored in the memory or on the memory to display the graphical information of the GUI on an external input / output device (such as, a display device coupled to the interface). In some optional embodiments, if necessary, multiple processors and / or multiple buses can be used together with multiple memories and multiple memories. Equally, multiple computer devices can be connected, and each device provides part of the necessary operations (for example, as a server array, a group of blade servers, or a multi-processor system). Figure 13 A processor 10 is taken as an example.

[0228] The processor 10 may be a central processing unit, a network processor, or a combination thereof. The processor 10 may further include a hardware chip. The hardware chip may be an application-specific integrated circuit, a programmable logic device, or a combination thereof. The programmable logic device may be a complex programmable logic device, a field programmable gate array, a general purpose array logic, or any combination thereof.

[0229] The memory 20 stores instructions that can be executed by at least one processor 10, so that the at least one processor 10 executes the method shown in the above embodiment.

[0230] The memory 20 may include a program storage area and a data storage area, wherein the program storage area may store an operating system and application programs required for at least one function; the data storage area may store data created based on the use of the computer device, etc. In addition, the memory 20 may include a high-speed random access memory, and may also include a non-transient memory, such as at least one disk storage device, a flash memory device, or other non-transient solid-state storage device. In some optional embodiments, the memory 20 may optionally include a memory remotely located relative to the processor 10, and these remote memories may be connected to the computer device via a network. Examples of the above-mentioned network include, but are not limited to, the Internet, an intranet, a local area network, a mobile communication network, and combinations thereof.

[0231] The memory 20 may include a volatile memory, such as a random access memory; the memory may also include a non-volatile memory, such as a flash memory, a hard disk or a solid-state drive; the memory 20 may also include a combination of the above types of memory.

[0232] The computer device further includes an input device 30 and an output device 40. The processor 10, the memory 20, the input device 30 and the output device 40 may be connected via a bus or other means. Figure 13 The bus connection is taken as an example.

[0233] The input device 30 can receive input digital or character information and generate key signal input related to user settings and function control of the computer device, such as a touch screen, a keypad, a mouse, a trackpad, a touch pad, an indicator stick, one or more mouse buttons, a trackball, a joystick, etc. The output device 40 can include a display device, an auxiliary lighting device (e.g., an LED), and a tactile feedback device (e.g., a vibration motor). The above-mentioned display device includes but is not limited to a liquid crystal display, a light emitting diode, a display, and a plasma display. In some optional embodiments, the display device can be a touch screen.

[0234] The embodiment of the present invention also provides a computer-readable storage medium. The above-mentioned method according to the embodiment of the present invention can be implemented in hardware, firmware, or implemented as a computer code that can be recorded in a storage medium, or implemented as a computer code that is originally stored in a remote storage medium or a non-temporary machine-readable storage medium and downloaded through a network and will be stored in a local storage medium, so that the method described herein can be stored in such software processing on a storage medium using a general-purpose computer, a dedicated processor, or programmable or dedicated hardware. Among them, the storage medium can be a magnetic disk, an optical disk, a read-only storage memory, a random access memory, a flash memory, a hard disk or a solid-state drive, etc.; further, the storage medium can also include a combination of the above-mentioned types of memory. It can be understood that a computer, a processor, a microprocessor controller or programmable hardware includes a storage component that can store or receive software or computer code. When the software or computer code is accessed and executed by a computer, a processor or hardware, the method shown in the above embodiment is implemented.

[0235] A portion of the present invention may be applied as a computer program product, such as a computer program instruction, which, when executed by a computer, can call or provide the method and / or technical solution according to the present invention through the operation of the computer. Those skilled in the art should understand that the form in which the computer program instruction exists in a computer-readable medium includes, but is not limited to, a source file, an executable file, an installation package file, etc. Accordingly, the way in which the computer program instruction is executed by the computer includes, but is not limited to: the computer directly executes the instruction, or the computer compiles the instruction and then executes the corresponding compiled program, or the computer reads and executes the instruction, or the computer reads and installs the instruction and then executes the corresponding installed program. Here, the computer-readable medium may be any available computer-readable storage medium or communication medium that can be accessed by the computer.

[0236] Although the embodiments of the present invention have been described with reference to the accompanying drawings, those skilled in the art may make various modifications and variations without departing from the spirit and scope of the present invention. Such modifications and variations are all within the scope defined by the appended claims.

Claims

1. A method for controlling the operating range of a hydrogen production system, characterized in that: The method comprises: Establish electrochemical models and hydrogen-in-oxygen models for hydrogen production systems; Based on the electrochemical model and the hydrogen-in-oxygen model, polarization curves and isolines of hydrogen-in-oxygen concentrations at different operating pressures, temperatures, and alkali solution flow rates are calculated, and a gas-liquid separation capability line is also calculated; Adding a boundary limit line to the polarization curve, and constructing a safe operation boundary envelope diagram based on the polarization curve with the boundary limit line added, the hydrogen concentration contour line in oxygen, and the gas-liquid separation ability line; obtaining a minimum current, a real-time operating current, and a maximum current of the hydrogen production system, and calculating a safety margin based on the minimum current, the real-time operating current, and the maximum current; The operating range of the hydrogen production system is regulated based on the safe operating boundary envelope diagram and the safety margin.

2. The method according to claim 1, characterized in that The electrochemical model and the hydrogen-in-oxygen model of the hydrogen production system are established, including: Calculating the reversible electrolysis voltage, activation overpotential, ohmic overpotential, and concentration gradient overpotential during operation of the hydrogen production system, and establishing an electrochemical model based on the reversible electrolysis voltage, activation overpotential, ohmic overpotential, and concentration gradient overpotential; The hydrogen exchange flux, diffusion flux, convection flux, alkali solution mixing flux and oxygen production rate per unit time during the operation of the hydrogen production system are calculated, and a hydrogen-in-oxygen model is established based on the hydrogen exchange flux, diffusion flux, convection flux, alkali solution mixing flux and oxygen production rate per unit time.

3. The method according to claim 1, characterized in that Based on the electrochemical model and the hydrogen-in-oxygen model, polarization curves and isolines of hydrogen-in-oxygen concentration at a preset operating pressure, a preset temperature, and a preset alkali solution flow rate are calculated, and a gas-liquid separation capability line is calculated, including: Different operating pressures, temperatures, and alkali flow rates were input into the electrochemical model to obtain the corresponding polarization curves. Different operating pressures, temperatures and alkali solution flow rates were input into the oxygen-hydrogen model to obtain the corresponding isovalues of hydrogen concentration in oxygen. The gas-liquid separation capacity line is calculated based on the diameter and length of the gas-liquid separator in the hydrogen production system and the gas-liquid variable parameters under different operating pressures, temperatures and alkali solution flow rates.

4. The method according to claim 1, wherein The boundary limit lines include a maximum voltage limit line, a maximum current limit line, a minimum temperature limit line, a maximum temperature limit line and a hydrogen concentration limit line in oxygen; Adding a boundary limit line to the polarization curve, and constructing a safe operation boundary envelope diagram based on the polarization curve with the boundary limit line added, the hydrogen concentration contour line in oxygen, and the gas-liquid separation ability line, including: Adding a maximum voltage limit line, a maximum current limit line, a minimum temperature limit line, a maximum temperature limit line and a hydrogen concentration limit line in oxygen to the polarization curve respectively; A safe operation boundary envelope diagram is constructed based on the polarization curve, the maximum voltage limit line, the maximum current limit line, the minimum temperature limit line, the maximum temperature limit line and the hydrogen concentration limit line in oxygen, the hydrogen concentration contour line in oxygen and the gas-liquid separation ability line.

5. The method according to claim 4, characterized in that The hydrogen concentration in oxygen includes a first threshold, a second threshold, and a third threshold, and the values of the first threshold, the second threshold, and the third threshold decrease in sequence; The safe operation boundary envelope diagram constructed based on the polarization curve with added boundary limit lines, the hydrogen concentration contour line in oxygen, and the gas-liquid separation ability line also includes: The area outside the safe operation boundary envelope diagram is called a danger zone; The area between the second threshold value and the first threshold value of the hydrogen concentration in oxygen in the safe operation boundary envelope diagram is used as a warning area; The area within the safe operation boundary envelope diagram where the concentration of hydrogen in oxygen ranges from the third threshold to the second threshold and is less than the gas-liquid separation capability line is used as a safe zone.

6. The method according to claim 5, characterized in that The safety margin includes an uplink safety margin and a downlink safety margin; Obtaining a minimum current, a real-time operating current, and a maximum current of the hydrogen production system, and calculating a safety margin based on the minimum current, the real-time operating current, and the maximum current, including: Calculating the minimum current of the hydrogen production system based on the hydrogen in oxygen model; The upstream safety margin and downstream safety margin are calculated based on the minimum current, real-time operating current and maximum current respectively.

7. The method according to claim 6, characterized in that The method further comprises: Under different operating pressures and different alkali solution flow rates, the corresponding upstream safety margin and downstream safety margin are calculated based on the upstream safety margin and downstream safety margin; Based on the uplink safety margin and downlink safety margin, the relationship between the real-time operating current and the maximum current and minimum current are displayed respectively.

8. The method according to claim 7, characterized in that The operating range of the hydrogen production system is regulated based on the safe operating boundary envelope diagram and the safety margin, including: The impact of different operating pressures, different alkali liquid flow rates and different temperatures on the safety zone, danger zone, warning zone, as well as the upward safety margin and downward safety margin are analyzed, and the operating pressure, alkali liquid flow rate and temperature of the hydrogen production system are regulated based on the impact rules.

9. A hydrogen production system operating range control device, characterized in that: The device comprises: Model building module, used to build the electrochemical model and hydrogen-in-oxygen model of the hydrogen production system; a limit line calculation module for calculating polarization curves and isolines of hydrogen-in-oxygen concentrations at different operating pressures, temperatures, and alkali solution flow rates based on the electrochemical model and the hydrogen-in-oxygen model, and simultaneously calculating a gas-liquid separation capability line; a safe operation boundary envelope diagram construction module, configured to add boundary limit lines to the polarization curve, and construct a safe operation boundary envelope diagram based on the polarization curve to which the boundary limit lines have been added, the isoline of hydrogen concentration in oxygen, and the gas-liquid separation ability line; A safety margin calculation module is used to obtain the minimum current, real-time operating current and maximum current of the hydrogen production system, and calculate the safety margin based on the minimum current, real-time operating current and maximum current; The hydrogen production system operating range control module is used to control the operating range of the hydrogen production system based on the safe operating boundary envelope diagram and the safety margin.

10. A computer device, characterized in that: include: A memory and a processor, wherein the memory and the processor are communicatively connected to each other, the memory stores computer instructions, and the processor executes the method for controlling the operating range of a hydrogen production system according to any one of claims 1 to 7 by executing the computer instructions.

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