Method for determining a temperature for operating an electrolysis system

Abstract

The invention relates to a method for determining a temperature for the operation of an electrolysis plant in which water is converted into oxygen and hydrogen in one or more electrolysis cells, in particular each having a proton exchange membrane, comprising: receiving real measurement data (310, 312) of one or more operating parameters of the electrolysis plant, which have been recorded during operation of the electrolysis plant by means of one or more sensors, determining, based on a model (300) of one or at least one of the several electrolysis cells, and the real measurement data (312) of one or at least one of the several operating parameters, virtual measurement data (320) of a cell temperature of one or at least one of the several electrolysis cells, and providing or outputting the virtual measurement data (320) of the cell temperature for the operation of the electrolysis plant.

Description

[0001] The invention relates to a method for determining a temperature for the operation of an electrolysis plant in which water is converted into oxygen and hydrogen in one or more electrolysis cells, as well as a computing system for this purpose and an electrolysis plant which is used, for example, to produce hydrogen. State of the art

[0002] Hydrogen can be produced using electrolysis, in which, for example, water is split or converted into oxygen and hydrogen using electrical energy. This is also referred to as water electrolysis. One method used is proton exchange membrane electrolysis (PEM electrolysis). In this context, the terms PEM electrolysis plants or PEM electrolyzers are also used.

[0003] During PEM electrolysis, most of the water supplied to each cell or stack typically remains on the oxygen side of the membrane. While the hydrogen is generated on the other side of the membrane and removed with a small partial flow of water, the oxygen initially remains in the water (most of the oxygen is usually in gas bubbles) and is then typically separated from the water in a container.

[0004] During the operation of a PEM electrolysis plant, aging and degradation effects typically occur, reducing the plant's efficiency and, depending on the power electronics design, potentially also lowering hydrogen production. The causes of various degradation mechanisms are not yet fully understood. However, it has been shown that, in addition to water quality, temperature has a significant effect on the degradation rate. In this context, temperature is generally considered to be the block temperature, i.e., the temperature of the stack. Within a block, however, the temperature is usually not perfectly homogeneous; rather, temperatures above and below the block temperature occur locally.

[0005] Within an electrolysis cell, the membrane typically has a higher temperature than the average temperature of the cell.

[0006] As has been shown, the membrane temperature is crucial for the degradation mechanisms, especially in the case of a so-called Nafion™ membrane, since the material is known to decompose more rapidly at higher temperatures (Nafion is a perfluorinated copolymer containing a sulfo group as its ionic group). Therefore, the temperatures in the electrolysis cell should not be too high.

[0007] However, the temperature within the electrolysis cell cannot be measured, or only very inadequately. Against this background, the task arises to improve the operation of an electrolysis plant, especially a PEM electrolysis plant, in particular to provide a better way to avoid excessively high temperatures and thus reduce degradation. Disclosure of the invention

[0008] This problem is solved by a method for determining a temperature for the operation of an electrolysis plant, as well as a computing system and an electrolysis plant with the features of the independent claims. Embodiments are the subject of the dependent claims and the following description. Advantages of the invention

[0009] The invention relates to water electrolysis and electrolysis plants, or rather their operation. Such electrolysis plants typically serve to produce or obtain hydrogen by means of electrolysis. In so-called water electrolysis, water is converted (split) into hydrogen and oxygen; that is, in addition to hydrogen, oxygen is always also obtained or produced simultaneously. Water electrolysis includes, for example, alkaline electrolysis (AEL) and proton exchange membrane electrolysis (PEM electrolysis). There are also solid oxide electrolysis (SOEC) and anion exchange membrane electrolysis (AEM electrolysis). The fundamentals of this are known, for example, from "Bessarabov et al.: PEM electrolysis for Hydrogen production. CRC Press."

[0010] The present invention will be described with a focus on proton exchange membrane electrolysis, but is also suitable for the other types of electrolysis mentioned. In PEM electrolysis, for example, water, and in particular demineralized water, is supplied as the feed medium to one or more electrolysis cells, each containing a proton exchange membrane (PEM) – hereinafter also simply referred to as the membrane – in which the feed medium, i.e., the water, is converted (split) into hydrogen and oxygen.

[0011] As mentioned, most of the water in PEM electrolysis typically remains on the oxygen side of the membrane. While the hydrogen is generated and removed on the other side of the membrane, the oxygen initially remains in the water, or rather in gas bubbles, and is then typically fed as an oxygen-containing fluid stream to a container called an oxygen separator. There, the oxygen is separated from the water, yielding an oxygen product stream, which is typically released into the atmosphere. It should be noted that this is just one example for illustrative purposes; the principle can also be applied to a cathode-side feed (stream) or a dual-circuit system with anode and cathode feeds.

[0012] A fluid stream containing water is then fed from the oxygen separator to one or more electrolysis cells. This is therefore a closed loop, at least with regard to the water.

[0013] A hydrogen-containing fluid stream is fed from one side of the hydrogen side of one or more electrolysis cells to a hydrogen separator. Unlike the oxygen-containing fluid stream, the proportion of water in the hydrogen-containing fluid stream is typically significantly lower, although it may still contain some water.

[0014] The hydrogen separator separates the hydrogen from the water, producing a so-called hydrogen product stream, which is typically intended for further use and can initially be stored for this purpose.

[0015] As mentioned, such an electrolysis system has one or more electrolysis cells, although typically several are provided. Furthermore, several such electrolysis cells can be combined into a so-called stack; the electrolysis system can then have multiple stacks. Each electrolysis cell then has a membrane.

[0016] As mentioned, aging and degradation effects occur during the operation of such an electrolysis plant, reducing the plant's efficiency and thus hydrogen production. Although the causes of various degradation mechanisms are not yet fully understood, the temperature and, potentially, the quality of the demineralized water have an effect on the degradation rate and, more generally, on degradation. In this context, temperature is usually considered to be the stack block temperature or the temperature at the water outlet of the stack on the anode side. These temperatures can typically be measured reliably and with sufficient accuracy using sensors.

[0017] Within an electrolysis cell, at least in the case of PEM electrolysis, the membrane typically has a higher temperature than the stack or the electrolysis cell itself. A corresponding temperature profile within an electrolysis cell is shown in the figures. However, the temperature of the membrane, which is particularly relevant for degradation, or more generally within an electrolysis cell or stack, cannot be measured, or can only be measured inadequately or with great difficulty using physical sensors.

[0018] Against this background, a new method is proposed for determining the temperature of or within an electrolysis cell. This involves receiving real-world measurement data from one or more operating parameters of the electrolysis system, for example, in a processing computer system such as a plant control unit. This real-world measurement data is acquired during operation of the electrolysis system using one or more sensors (primarily physical sensors). Such operating parameters can include, for example, temperatures outside the electrolysis cell, which, as mentioned above, are simple and readily available. Other operating parameters, such as voltage and current for operating the electrolysis cell, or water or gas flow rates, are also suitable.

[0019] In particular, all operating parameters conventionally used for the operation of the electrolysis plant can be used.

[0020] Based on a model of one or at least one of the several electrolysis cells, and the actual measurement data of one or at least one of the several operating parameters, virtual measurement data for the cell temperature of one or at least one of the several electrolysis cells are determined. This virtual cell temperature data is then provided or output for the operation of the electrolysis system. While the actual measurement data is acquired using sensors, the virtual measurement data is not actual measured data but rather hypothetical data that would be measured—at least approximately—if they were measurable by sensors.

[0021] In particular, based on the real measurement data of one or at least one of the several operating parameters and the virtual measurement data of the cell temperature, control data for the operation of the electrolysis system can be determined and output to initiate the operation of the electrolysis system according to the control data.

[0022] The steps mentioned can be carried out, for example, on the executing computer system such as the plant control system; that is, the real measured values ​​are received there, the virtual measured values ​​are determined, and then the control data is determined, which is then output, for example, as control signals to relevant components such as an inverter for the operation of an electrolysis cell and / or valves for regulating water and / or gas flows.

[0023] This means that the model is also executed on the computer system, i.e., the calculations to be performed with it are carried out there. However, it is also conceivable that the model and the calculations to be performed with it are executed on a computer system separate from the plant control system, and the virtual measurement data – as well as any real measurement data – are then transferred to the plant control system.

[0024] In both cases, the model is operated and executed in parallel and simultaneously with the operation of the electrolysis plant. This allows the necessary temperatures of the electrolysis cell to be determined in real time and used for ongoing operation.

[0025] In one embodiment, the cell temperature comprises the temperature of the proton exchange membrane of one or at least one of the several electrolysis cells. In another embodiment, the cell temperature comprises a temperature profile across a structure of one or at least one of the several electrolysis cells, i.e., a kind of temperature profile as a function of position within the electrolysis cell or at least along a path through the electrolysis cell.

[0026] In the case of multiple electrolysis cells, the same model can be used for all of them. However, an individual model for each or at least some of the multiple electrolysis cells is also conceivable, for example, if there are different electrolysis cells; electrolysis cells may differ from each other in size or age, for example.

[0027] This model is, in particular, a so-called digital twin, which depicts the electrolysis cell as faithfully as possible, including its structure and assembly. Further details will be explained in relation to the figures.

[0028] One advantage of PEM electrolysis, in particular, should actually be its high rate of load changes. While highly fluctuating operation of PEM electrolysis could lead to significantly increased degradation, this can now be avoided or at least reduced with the current temperature of the electrolysis cell, as overheating in the membrane can be prevented.

[0029] Load changes on the electrical side typically occur rapidly, resulting in a short-term increase in heat release in or at the membrane. However, heat dissipation effects are relatively slow, meaning that increased heat removal only follows the increased heat release with a delay. This leads to a temperature increase in the membrane region. This can be counteracted by knowing the current temperature of the membrane or at least the area around it.

[0030] Ideally, the load change or the rate of load change can now be controlled so that a certain temperature in the electrolysis cell or around the membrane is not exceeded. Control is possible, for example, via the temperature of the inlet current to the anode circuit, any existing cooling circuits, or by limiting the rate of load change. However, a desired target variable for the control – the temperature in the cell – which is difficult or impossible to measure, can now also be used.

[0031] In one embodiment, initiating the operation of the electrolysis system according to the control data includes adjusting the operation of one or at least one of the several electrolysis cells depending on the cell temperature, as already indicated. In other words, it is possible to react to potentially excessively high or impending excessively high temperatures in the electrolysis cell. In particular, excessively high temperatures can be counteracted.

[0032] This can be achieved through various measures. For example, the rate of load change of one or at least one electrolysis cell can be limited. The temperature of the water or cooling water in one or at least one electrolysis cell can also be lowered, particularly temporarily. The flow rate of water or cooling water in one or at least one electrolysis cell can also be increased or operated in pulsed mode; this too can be done temporarily. Heat losses from the electrolysis system (to the environment) can also be increased, possibly temporarily. Furthermore, the pressure of raw hydrogen and / or raw oxygen at the outlet of one or at least one electrolysis cell can be lowered, possibly temporarily. All these measures counteract overheating in the electrolysis cell, particularly of the membrane, and thus reduce degradation.

[0033] Optimal efficiency and load change rate with minimized degradation can be achieved by minimizing the overtemperature or peak temperature in the membrane.

[0034] This results in improved efficiency during base load operation, reduced degradation during fluctuating operation, and an increase in the membrane core temperature during partial load operation to optimize efficiency versus lifespan.

[0035] In one embodiment, virtual measurement data for one or at least one of the selected operating parameters are determined based on the model and the real measurement data of that one or at least one of the selected operating parameters. Thus, not only are virtual measurement data for the cell temperature determined, but also further virtual measurement data for operating parameters for which real measurement data also exist. The measurement data is then compared with the virtual measurement data, and, if necessary, the model is adjusted based on any difference between the measurement data and the virtual measurement data. In this way, the model can always be kept as close to reality as possible. For example, state estimation or a suitable algorithm, such as a Kalman filter, can be used. This comparison and adjustment can be performed for different operating points.In particular, the model comparison is carried out continuously or repeatedly during the operation of the electrolysis plant.

[0036] A computing system according to the invention (i.e., a data processing system) is configured to execute a method according to the invention or its method steps; it therefore comprises means for executing the method according to the invention or its method steps. The computing system can be a computer or server, e.g., in a so-called cloud or cloud environment, or, as already mentioned, a plant control system or part thereof. The invention also relates to an electrolysis plant with such a computing system. With regard to the electrolysis plant and its further details, reference is also made to the preceding explanations.

[0037] The invention is explained in more detail below with reference to the accompanying drawing, which shows a system according to a preferred embodiment of the present invention.

[0038] Brief description of the drawing Figure 1 schematically shows an electrolysis plant in one embodiment. Figures 2a, 2b show diagrams to illustrate the invention. Figure 3 schematically shows a sequence of steps in one embodiment of a process. Detailed description of the drawing

[0039] In Figure 1Figure 100 schematically depicts an electrolysis plant 100 in an embodiment in which a method according to the invention can also be carried out. This is, by way of example, an electrolysis plant for water electrolysis using PEM. However, as mentioned, an electrolysis plant for water electrolysis using AEM or SOEC is also conceivable. In particular, the electrolysis plant shown here, and generally described within the scope of the invention, is an industrial-scale electrolysis plant for, for example, producing hydrogen on an industrial scale. A typical power output of such an electrolysis plant is, for example, more than 10 MW or even more than 20 MW.

[0040] The electrolysis system 100 features two electrolysis units or stacks 110a and 110b as examples, of which only stack 110a is shown in more detail, namely with two electrolysis cells 110.1 and 110.2, each containing a proton exchange membrane (PEM) 112. The PEM 112 separates each electrolysis cell into an oxygen side 114 and a hydrogen side 116. The oxygen sides 114 and the hydrogen sides 116 can be considered together as the oxygen side and hydrogen side, respectively, of a stack or of the entire electrolysis system.

[0041] Stack 110b can be constructed similarly to Stack 110a, and further stacks of this type can also be provided. Generally, an electrolysis system can have one or more electrolysis cells. In the case of multiple electrolysis cells, several of them—for example, two, four, six, eight, or more—are arranged as a stack and, for example, supplied with electrical energy together. For instance, 40, 100, or even up to 400 or more electrolysis cells per stack are conceivable.

[0042] The electrolysis system 100 also includes a vessel 120, which serves as an oxygen separator or oxygen-water separator. The oxygen separator 120 is connected via a fluid connection to the stacks 110a, 110b, and to each of the electrolysis cells 110.1, 110.2 within the stacks. This allows a fluid flow b to be pumped from the oxygen separator 120 to the electrolysis cells, for example, by means of a pump 124, via a suitable fluid connection 122, such as pipes. Depending on the type of electrolysis system and, for example, the number of electrolysis cells and / or stacks, several fluid connections (i.e., separate lines) may be provided. For example, one fluid connection may be provided for two or four stacks.

[0043] The stacks or electrolysis cells are also connected to the oxygen separator 120 via a fluid connection 126, e.g., pipes. A fluid flow c can be pumped from the electrolysis cells, specifically from the oxygen side 114 of each electrolysis cell, to the oxygen separator 120 via the fluid connection 126; the pump 124 may also be sufficient for this purpose. Depending on the type of electrolysis system and, for example, the number of electrolysis cells, several fluid connections (i.e., separate lines) may be provided. For example, one fluid connection may be provided for two or four stacks.

[0044] Furthermore, the electrolysis system 100 includes an additional container 130, which serves as a hydrogen separator or hydrogen-water separator. The stacks or electrolysis cells are connected to the hydrogen separator 130 via a fluid connection 132, e.g., pipes. A fluid flow e from the electrolysis cells, specifically the hydrogen side 116 of each electrolysis cell, can be conveyed to the hydrogen separator 130 via the fluid connection 132. Depending on the type of electrolysis system and, for example, the number of electrolysis cells, several fluid connections (i.e., separate lines) may be provided. For instance, one fluid connection may be provided for two or four electrolysis cells. Multiple hydrogen separators are also conceivable.

[0045] During operation of the electrolysis plant 100, the fluid stream b, which contains water, is pumped from the oxygen separator 120 to the stacks or their electrolysis cells. There, the water is converted into oxygen and hydrogen. For this purpose, an electrical voltage is applied to the electrolysis cells. The hydrogen is electrochemically transported through the PEM 112 to the hydrogen side 116 and can then be fed, possibly mixed with water vapor and a liquid water phase, as stream e – a hydrogen-containing fluid stream – to the hydrogen separator 130. There, the hydrogen can be separated and, for example, discharged or stored as stream f for further use. Water separated in the hydrogen separator 130 can, for example, be treated (not shown here) and then returned to the main water circuit as fluid stream g.

[0046] It is understood that the PEM 112 is only present in PEM electrolysis; in AEM or SOEC electrolysis, a ceramic membrane may be used instead.

[0047] The oxygen remains on the oxygen side 114 along with most of the water. The resulting fluid flow c therefore contains water and oxygen – it is an oxygen-containing fluid flow. As mentioned, the fluid flow c is fed to the oxygen separator 120.

[0048] It should be mentioned here that fluid stream c may also contain a certain small proportion of hydrogen. Similarly, fluid stream e may also contain a certain small proportion of oxygen.

[0049] Since water is converted into oxygen and hydrogen in the electrolysis cells and the oxygen and hydrogen are removed, the amount of water decreases and therefore - in order to maintain continuous operation - new water (so-called make-up water) can be supplied externally as electricity a.

[0050] This water can be pre-treated, for example (not shown here), which is not relevant to the present invention. Water separated in the hydrogen separator 130, i.e., the fluid stream g already mentioned, can be fed to stream a and then back to the oxygen separator 120, possibly also after prior treatment.

[0051] As mentioned, oxygen is separated from the water in the oxygen separator 120; the oxygen separated or separated in this process can be discharged as an oxygen stream d e.g. for further use and possibly stored.

[0052] Furthermore, the electrolysis plant 100 includes a computer system 150 designed as a plant control system, as well as a control unit 152 for the operation of the electrolysis cells or stacks and a control unit 154 for controlling, for example, water flow rates and, if necessary indirectly, temperatures. Corresponding sensors can provide measured values ​​or data for this purpose. The control unit 152 can, for example, include an inverter or be part of one itself, which allows, in particular, the specification of an electrical load and thus also load changes.

[0053] In the plant control unit 150, various calculations can be performed within the scope of the invention, in particular determining control data for the operation of the electrolysis plant. These can then be transferred to the control unit 152 and the control unit 154.

[0054] In Figure 2aA schematic cross-section through an electrolysis cell 210 is shown. The electrolysis cell is depicted in a diagram where a temperature 200 is plotted against a position 202 through the electrolysis cell. One or more such electrolysis cells 210 can be used, for example, in the electrolysis system 100 according to Figure 1 be used.

[0055] The electrolysis cell 210 has a membrane, or PEM 212, which separates the electrolysis cell 210 into an oxygen side 214 and a hydrogen side 216. Extending outwards from the membrane 212, the oxygen side 214 comprises a porous transport layer 240, a flow channel 242 for water or oxygen, and a bipolar plate 244. The bipolar plate 244 serves as an electrode, specifically the anode. Similarly, extending outwards from the membrane 212, the hydrogen side 216 comprises a porous transport layer 240', a flow channel 242' for water or hydrogen, and a bipolar plate 244'. The bipolar plate 244' serves as an electrode 241', specifically the cathode. Membrane 212 itself may have a coating applied to both sides, and the same membrane may also be catalytically active in or between the individual layers.

[0056] Figure 260 now shows the temperature profile through electrolysis cell 210; this could, for example, be a steady-state temperature profile. As has been shown, the temperature value at or around the membrane is significantly higher than at the outer edges.

[0057] If the temperature at the membrane rises too sharply or becomes too high, this can lead to accelerated membrane degradation. Particularly during rapid load changes on the current side, higher heat releases can occur in the short term, while heat dissipation cannot occur as quickly. This results in a temperature increase, especially in the membrane region. A temperature profile for such a case is shown in Figure 262; this could, for example, be a transient temperature profile.

[0058] In Figure 2a Is the electrolysis cell 210 made of Figure 2aThis is shown again, also with curve 260; it should be noted that axis 200 is slightly shifted. A curve 264 is also shown here, which could also represent a transient temperature profile. Unlike curve 262, however, the maximum temperature at the membrane does not exceed the value of curve 260. Instead, the temperature is lower further out. This can be achieved, for example, by increasing the water flow.

[0059] It should be noted that the maximum temperature allowed here does not necessarily have to be the one from steady-state operation, but can also be another appropriate value determined by other means.

[0060] In Figure 3A schematic flow diagram for a process in one embodiment is shown. Several components of the electrolysis plant 100 are shown, namely the plant control unit 150, the control unit 152, and the control unit 154, and, by way of example, the stack 110a with the electrolysis cells. Corresponding fluid flows b, c, and 3 are also shown as in Figure 1 shown. For this, reference is made to the explanations of the Figure 1 referred.

[0061] Furthermore, a Model 300 electrolysis cell is shown. The Model 300 can be used as an electrolysis cell, such as in... Figure 1 or 2 shown as a so-called digital twin, depicting it as accurately as possible. In particular, for example, the [unclear text] can be used. Figure 2 The structure shown should be replicated in order to determine the temperature profile that develops in the electrolysis cell and through its cross-section.

[0062] During operation of the electrolysis plant, various operating parameters are measured using sensors. The resulting real-time measurement data 310 can be received by the control unit 150 in the usual manner to generate control data for the operation of the electrolysis plant. Examples of such control data 330 and 332 are shown. Control data 330 is used to control the electrical load via the control unit 152. Control data 332 is used to control the flow rate of water, specifically the fluid flow b, via the control unit 154.

[0063] The measurement data of some, or possibly all, of the various operating parameters of the electrolysis plant are used to determine the temperature in the electrolysis cell or all electrolysis cells. The corresponding measurement data are designated here as 312 and may be part of the measurement data 310. However, it is also conceivable that the measurement data 312 includes values ​​for operating parameters that are not contained in the measurement data 310.

[0064] Real measurement data 310, 312 are received, which were recorded during operation of the electrolysis plant by means of one or more sensors. Based on the model 300 and the real measurement data 312, virtual measurement data 320 of a cell temperature of one or at least one of the several electrolysis cells are then determined. These are then made available.

[0065] The use of the model can, for example, involve obtaining the real measurement data (310) and then, if necessary, adapting it for use in the model. The model is then used to make a prediction for the temperature in the electrolysis cell, which is then output as the virtual measurement data.

[0066] Based on the real measurement data 310 and virtual measurement data 320 of the cell temperature, the control data 330, 332 are then used for the operation of the

[0067] The electrolysis system is determined. In contrast to regular operation, which is based only on the real measurement data 310, the virtual measurement data 320 of the cell temperature are additionally used here to operate the electrolysis system.

[0068] As mentioned, this allows the operation to be adjusted accordingly to avoid excessively high temperatures in the electrolysis cell, and especially at the membrane. This can be achieved, for example, by limiting the rate of load change (this would be done, for example, via control data 330) or by increasing the water flow rate (this would be done, for example, via control data 332).

[0069] In addition to cell temperature, other operating parameters can also be predicted using the model, i.e., corresponding virtual measurement data can be determined. These operating parameters can include, for example, the efficiency of the electrolysis cells, mechanical stresses in the stacks, a gas crossover current, or even the condition or damage of individual components (so-called health status of the electrolysis system).

[0070] In addition to the measures already mentioned, the cooling water or water inlet temperature (or the temperature of the stack) can also be lowered before increasing the load in the electrolysis cell in order to reduce the overall membrane temperature. This could then be done, for example, as part of a pre-control system.

[0071] Another variable or operating parameter that needs to be controlled is the gas crossover, which must not be exceeded during continuous operation, although higher rates can be tolerated for short periods if the electrolysis plant is subsequently operated below the limits (so-called dilution effect).

Claims

1. Method for determining a temperature for the operation of an electrolysis plant (100) in which water is converted into oxygen and hydrogen in one or more electrolysis cells (110.1, 110.2), in particular each comprising a proton exchange membrane (112, 212), comprising: receiving real measurement data (310, 312) of one or more operating parameters of the electrolysis plant (100), which have been recorded during operation of the electrolysis plant by means of one or more sensors; determining, based on a model (300) of one or at least one of the several electrolysis cells and the real measurement data (312) of one or at least one of the several operating parameters, virtual measurement data (320) of a cell temperature of one or at least one of the several electrolysis cells; and providing or outputting the virtual measurement data (320) of the cell temperature for the operation of the electrolysis plant (100).

2. Method according to claim 1, further comprising: determining, based on the real measurement data (310) of one or at least one of the several operating parameters and the virtual measurement data (320) of the cell temperature, control data (330, 332) for the operation of the electrolysis system, and outputting the control data (330, 332) and initiating operation of the electrolysis system according to the control data.

3. Method according to claim 2, wherein initiating the operation of the electrolysis system (100) according to the control data comprises: adjusting the operation of one or at least one of the several electrolysis cells depending on the cell temperature.

4. The method of claim 3, wherein the adjustment of the operation comprises at least one of the following measures: - limiting the rate of change of load of one or the at least one electrolysis cell, - lowering, in particular temporarily lowering, the temperature of water or cooling water of one or the at least one electrolysis cell, - increasing or pulsating operation, in particular temporarily increasing or temporarily pulsating operation, the flow rate of water or cooling water of one or the at least one electrolysis cell, - increasing, in particular temporarily increasing, heat losses of the electrolysis plant, - lowering, in particular temporarily lowering, the pressure of raw hydrogen and / or raw oxygen at the outlet of one or the at least one electrolysis cell.

5. A method according to any of the preceding claims, further comprising a model matching process, comprising: determining, based on the model (300) and the real measurement data of one or at least one of the several operating variables selected for matching, virtual measurement data of one or at least one of the several operating variables selected for matching; matching the measurement data with the virtual measurement data; and, if necessary, adjusting the model based on a difference between the measurement data and the virtual measurement data.

6. The method of claim 5, wherein the model matching is performed continuously or repeatedly during the operation of the electrolysis plant.

7. Method according to one of the preceding claims, wherein one or each of the several electrolysis cells (110.1, 110.2) comprises a proton exchange membrane (112, 212), and wherein the cell temperature comprises a temperature of the proton exchange membrane of one or at least one of the several electrolysis cells.

8. Method according to one of the preceding claims, wherein the cell temperature comprises a profile (260, 262, 264) of a temperature across a structure of one or at least one of the several electrolysis cells.

9. A method according to any of the preceding claims, further comprising: determining, based on the model (300) and the real measurement data (310, 312) of one or at least one of the several operating parameters, virtual measurement data of one or more further operating parameters of the electrolysis plant, and outputting the virtual measurement data of one or more further operating parameters of the electrolysis plant, wherein the one or more further operating parameters of the electrolysis plant comprise at least one of the following parameters: - An efficiency of one or at least one of the several electrolysis cells or of the electrolysis plant, - A mechanical stress in one or in or between the several electrolysis cells, - A gas crossover current, - A condition or damage of one or more components of one or at least one of the several electrolysis cells or of the electrolysis plant.

10. Computing system (150) for the operation of an electrolysis plant (100), wherein the control device is configured to carry out a method according to one of the preceding claims.

11. Electrolysis system (100) with a computing system (150) according to claim 10.

12. Electrolysis system (100) according to claim 11, further comprising one or more electrolysis cells (110.1, 110.2) in which water can be converted into oxygen and hydrogen, an oxygen separator (120) and a hydrogen separator (130), wherein the electrolysis system (100) is configured to supply a fluid stream (b) containing water from the oxygen separator to one or more electrolysis cells, to supply an oxygen-containing fluid stream (c) from an oxygen side of one or more electrolysis cells to the oxygen separator, and to supply a hydrogen-containing fluid stream (e) from a hydrogen side of one or more electrolysis cells to the hydrogen separator.

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