SAF synthesis gas hydrocarbon ratio dynamic phase lock control method and system for coping with source end power fluctuation

Abstract

The invention discloses an SAF synthesis gas hydrocarbon ratio dynamic phase lock control method and system for coping with source end power fluctuation. Aiming at the problem of catalyst carbon deposition caused by fluid transmission lag due to wind and light fluctuation, the method comprises the following steps: acquiring bottom-layer electrical data of a solid-state transformer at high frequency and extracting a power transient change rate; on the basis of a cross-domain electrical and fluid coupling model, hydrogen pressure trough pneumatic transmission delay time caused by load reduction is predicted; calculating lead phase compensation time of the carbon monoxide regulating valve by combining mechanical dead zone characteristics of the valve; before a hydrogen trough actually reaches the reaction kettle, a fluid feedback link is crossed, and a carbon monoxide valve is triggered by feedforward to execute nonlinear turn-off. Complex fluid lagging dimension reduction is converted into phase compensation of a time axis, dynamic phase locking of flow attenuation tracks of two synthetic gases is achieved, and the catalyst carbon deposition scrap risk in the transient falling period is thoroughly eradicated.

Description

A method and system for dynamic phase-locked loop control of C-H ratio in SAF syngas to address source-side power fluctuations Technical Field

[0001] This invention relates to the fields of flexible synthesis of sustainable aviation fuel (SAF), power-to-liquid (PtL) electro-liquid conversion technology and cross-physical domain automatic control technology. Specifically, it relates to a method and system for dynamic phase-locked control of the syngas C-H ratio to cope with strong source-end fluctuations of renewable energy sources such as wind and solar power and to prevent carbon deposition on Fischer-Tropsch synthesis catalysts from the bottom layer of millisecond-level electrical control. Background Technology

[0002] Against the backdrop of deep decarbonization in the aviation industry, using renewable energy sources such as wind and solar power to generate electricity, and then using advanced high-power power electronic devices such as solid-state transformers (SST) to power water electrolysis devices (such as ALK, PEM, or SOEC electrolyzers) to produce green hydrogen, and then further coupling it with carbon sources such as carbon monoxide (CO) or carbon dioxide (CO2) under high temperature and high pressure to synthesize sustainable aviation fuel (SAF), is currently recognized as one of the most commercially promising and emission reduction potential technologies.

[0003] However, in the practical engineering implementation of flexible synthesis systems that couple wind and solar hydrogen production with SAF (Self-Fuel-Aerosol) synthesis, the Fischer-Tropsch (FT) synthesis reaction stage, the core of the entire process, faces a critical bottleneck in microscopic automated control. The FT reaction is essentially a highly exothermic surface-catalyzed polymerization reaction that is extremely sensitive to chain growth probability. It demands extremely stringent control over the molar ratio of hydrogen (H2) to carbon monoxide (CO) in the inlet gas (i.e., the syngas C-H ratio, typically requiring strict and precise control at around 2:1). In existing chemical engineering technologies, the syngas ratio primarily relies on mass flow meters (MFC) or Coriolis flow meters installed near the reactor end of the inlet pipeline, combined with traditional proportional-integral-derivative (PID) algorithms for closed-loop feedback control.

[0004] This traditional control mode performs well in steady-state chemical engineering scenarios where the power grid provides a continuous and stable supply, but it completely fails in "flexible chemical engineering" scenarios directly driven by wind and solar energy. Due to the typical intermittent and highly volatile characteristics of wind and solar energy, when extreme weather factors such as clouds rapidly passing through and blocking photovoltaic panels or sudden gusts of wind cause a sharp drop in power supply at the source, the solid-state transformer will perform deep load reduction on the electrolyzer within a few milliseconds to tens of milliseconds to protect the electrolyzer hardware, resulting in a sudden and precipitous drop in the absolute amount of green hydrogen produced.

[0005] The fatal contradiction lies in the fact that, on the spatial topology of the physical system, between the electrolyzer outlet and the Fischer-Tropsch reactor, large-capacity hydrogen buffer tanks and long-distance distribution pipelines are inevitably arranged due to the process requirements of gas separation, purification, and pressure stabilization. These physical devices and pipelines constitute a huge "gas capacity" and "gas resistance" in fluid mechanics, causing severe low-pass filtering and transmission hysteresis when the transient drop in hydrogen production propagates as a pressure wave in the gas medium. This phenomenon is called "aerodynamic delay" or "dead-time" in control engineering, and its delay time is typically as high as several seconds or even tens of seconds.

[0006] Therefore, when the flow meter located at the inlet of the reactor detects and reports a substantial decrease in hydrogen flow, the system's adjustment timing is already severely lagging behind the actual deterioration of the operating conditions. At this point, the second high-speed regulating valve (controlling CO intake) that fails to close in advance and in time will allow high concentrations and excessive amounts of carbon monoxide to enter the reactor unimpeded, resulting in a severe "hydrogen-poor and carbon-rich" extreme environment being formed in a localized area of ​​the reactor.

[0007] This transient carbon-hydrogen imbalance can easily disrupt the original thermodynamic equilibrium, instantly triggering the irreversible Boudouard side reaction (disproportionation reaction: 2CO ⇌ C + CO2). The generated free carbon (C) will rapidly coat and block the microporous active sites of extremely expensive cobalt-based or iron-based synthesis catalysts. In industrial practice, carbon buildup lasting only a few seconds can lead to irreversible and permanent deactivation and scrapping of catalysts worth millions of dollars, forcing the entire synthesis plant to shut down for several weeks for catalyst replacement.

[0008] In summary, traditional co-domain feedback control algorithms based on "fluid-to-fluid" measurement are mathematically constrained by the physical limitations of aerodynamic transmission delay constants (which cannot overcome the physical limits of sound speed and fluid viscosity), making them fundamentally incapable of handling sudden changes in source power on the order of seconds or even milliseconds. This control failure, caused by the huge time gap between the "speed of electricity (speed of light)" and the "speed of gas (speed of sound / flow velocity)," has become a core engineering challenge hindering the large-scale commercialization and long-term stable operation of green electricity-green hydrogen-SAF flexible systems. Summary of the Invention

[0009] To address the serious technical problem in existing technologies where the failure of conventional feedback control algorithms and transient imbalance of the syngas C-H ratio due to physical delays in fluid transport lead to irreversible carbon deposition and waste of expensive catalysts, this invention provides a dynamic phase-locked loop control method and system for the SAF syngas C-H ratio based on the concept of electrical feedforward dimensionality reduction, which addresses power fluctuations at the source.

[0010] The technical solution adopted by this invention to solve its technical problem is: a dynamic phase-locked loop control method for the C-H ratio of SAF syngas to cope with source-end power fluctuations. This method is applied to a flexible synthesis system across physical domains driven by fluctuating renewable energy sources and including a solid-state transformer, a water electrolysis hydrogen production device, and a Fischer-Tropsch reactor. The method is characterized by including the following continuously executed control steps:

[0011] State perception step: By establishing a high-frequency communication link across the electrical domain and the fluid chemistry domain, the underlying operating electrical data of the solid-state transformer that directly supplies power to the water electrolysis hydrogen production device is collected in real time and at high frequency. Electrical characteristic parameters that characterize the transient rate of change of the output energy of the solid-state transformer are extracted from the underlying operating electrical data. These parameters are used as the feedforward trigger source of the entire control system, thereby completely avoiding the time lag caused by traditional chemical fluid sensors at the source.

[0012] Delay prediction step: Real-time monitoring of the electrical characteristic parameters. When the instantaneous drop amplitude or change slope of the electrical characteristic parameters meets the preset load reduction trigger condition, the pre-established cross-domain electrical and fluid coupling model is activated. The model comprehensively considers the physical spatial distance of the hydrogen transmission and distribution network, the gas capacity of the buffer tank, and the gas resistance of the pipeline. Based on this, it accurately calculates the dynamic pneumatic transmission delay time necessary for the fluid pressure trough formed by the sudden drop in hydrogen production due to the load reduction of the solid-state transformer to be physically transmitted from the outlet of the water electrolysis hydrogen production device to the inlet of the Fischer-Tropsch reactor.

[0013] Phase compensation step: The dynamic pneumatic transmission delay time is used as the reference advance amount on the time control axis, and combined with the mechanical dead zone and valve core action response characteristics of the carbon monoxide intake regulating valve, a dynamic advance phase compensation time for the carbon monoxide intake regulating valve is calculated and generated. This advance phase compensation time is used to characterize the time difference that the carbon monoxide valve must perform the shut-off action in advance to compensate for the fluid delay.

[0014] Phase-locked execution steps: During the advance phase compensation time before the pressure trough actually reaches the inlet of the Fischer-Tropsch reactor along the pipeline, at the physical control level, the conventional hydrogen flow detection feedback loop is forcibly bypassed, and a nonlinear feedforward shut-off command is directly issued to the carbon monoxide inlet regulating valve. This forces the carbon monoxide inlet flow curve to accurately follow the predicted hydrogen flow decay curve in time phase, so that during the entire transient impact cycle of source-end unloading, the real-time dynamic carbon-hydrogen ratio of hydrogen to carbon monoxide input to the Fischer-Tropsch reactor is strictly locked above the preset safety threshold to prevent catalyst carbon buildup and waste.

[0015] Preferably, in the state perception step, the extracted electrical characteristic parameter is the first time derivative of the active power output of the solid-state transformer; the preset load reduction trigger condition is that the first time derivative is less than the preset negative sudden drop threshold. When this condition is met, the trigger control system immediately switches from steady-state closed-loop mode to transient feedforward phase-locked mode.

[0016] Preferably, in the delay prediction step, the pre-established electrical-fluid coupling model integrates the physical gas capacity parameters and physical gas resistance parameters in the hydrogen buffer distribution branch; the process of calculating the pneumatic transmission delay time is essentially mapping the spatial distribution attenuation in fluid mechanics to the phase difference parameter on the time axis of the control system.

[0017] Preferably, the specific control logic of the phase-locked execution step is as follows: using the predicted hydrogen flow rate decay curve as the reference phase signal and the mechanical displacement action of the valve core of the carbon monoxide intake regulating valve as the tracking signal; within the advance phase compensation time, controlling the carbon monoxide intake regulating valve to perform nonlinear shut-off at a preset exponential function rate, thereby realizing dynamic phase locking of the two synthesis gas flow rate decline curves in the time dimension.

[0018] Preferably, the preset safety threshold is set to a real-time dynamic carbon-hydrogen ratio of not less than 1.8 to 1; during the entire transient adjustment cycle of the phase-locked execution step, the system executes the underlying hard clamping logic in parallel: when the calculated local transient carbon-hydrogen ratio approaches the preset safety threshold, the carbon monoxide intake is forcibly cut off to ensure that the catalyst in the reactor does not undergo irreversible carbon deposition.

[0019] Preferably, the system further includes an anti-disturbance recovery step: when the first time derivative of the active power of the solid-state transformer is detected to be greater than a preset positive recovery threshold, the control system enters a power ramp-up period; during the power ramp-up period, the opening phase of the carbon monoxide intake regulating valve is controlled to lag behind the recovery phase of the hydrogen pressure, so as to ensure that the hydrogen-rich state is maintained during the process of the system recovering to steady state.

[0020] This invention also provides a dynamic phase-locked control system for the C-H ratio of SAF syngas to cope with source-end power fluctuations, comprising: an electrical power supply assembly including a solid-state transformer and a water electrolysis hydrogen production device; a fluid gas supply assembly including a hydrogen buffer distribution branch and a carbon monoxide supply branch; a Fischer-Tropsch reactor; a flow actuator including a first high-speed regulating valve and a second high-speed regulating valve respectively disposed on the hydrogen buffer distribution branch and the carbon monoxide supply branch; a cross-domain phase-locked controller, which is communicatively connected to the underlying main control board of the solid-state transformer and electrically connected to the second high-speed regulating valve; the cross-domain phase-locked controller has an embedded microprocessor configured to execute the above-described dynamic phase-locked control method for the C-H ratio of SAF syngas to cope with source-end power fluctuations.

[0021] The beneficial effects of this invention are:

[0022] (I) A Cross-Domain Dimensional Reduction Strategy in Algorithms, Completely Eliminating the Risk of Carbon Accumulation (Significantly Reducing OPEX): This invention completely breaks away from the rigid mindset of the traditional chemical industry that relies solely on "fluid detection of fluid" for closed-loop PID feedback. It pioneered a cross-domain feedforward dynamic phase-locked loop (DPLL) algorithm based on the underlying "first derivative of electrical power." By utilizing electrical signals transmitted at the speed of light to predict fluid changes transmitted at the speed of sound, it creatively constructs the extremely complex problem of fluid lag in chemical processes into a spatiotemporally strongly coupled control mechanism that spans the three physical domains of [electron-fluid-catalytic reaction]. This achieves a generational leap in control philosophy from "passively compensating only after seeing fluctuations" to "predicting fluctuations and proactively blocking and intercepting them," truly preventing problems before they occur and completely eliminating the risk of catalyst carbon accumulation and scrapping caused by transient drops. This can save large SAF plants millions of yuan in catalyst replacement and downtime maintenance costs (OPEX) annually.

[0023] (II) Adaptive Nonlinear Following and Low-Level Safety Clamping Logic: This invention not only achieves proactive action but also solves the fluid dynamics equations for the dynamic pneumatic transmission delay time in real time. Combined with a unique nonlinear exponential shutdown logic, this ensures that the mechanical action of the carbon monoxide valve perfectly matches the decay curve of hydrogen gas due to the gas capacity effect in the time domain, avoiding secondary oscillation disturbances caused by linear shutdown. Supplemented by a 1.8:1 low-level hard clamping defense mechanism and an asymmetric recovery period delayed opening mechanism, an absolute safety digital barrier is constructed for the system under extreme operating conditions throughout its entire lifecycle, including full load, sudden drop, hibernation, and severe ramp-up.

[0024] (III) Significantly Optimizes Fixed Asset Investment in Hydrogen Production and Synthesis Plants (Reducing CAPEX): In traditional processes, to cope with aerodynamic delays, engineers are often forced to adopt a passive approach of constructing extremely large and expensive high-pressure buffer gas storage tank clusters to smooth out fluctuations, essentially "trading space for time." This invention, through extremely fast algorithm feedforward, perfectly replaces the cumbersome "physical buffer architecture" with a very low-cost "software and communication architecture," thereby making the system no longer dependent on large physical gas volumes and significantly reducing the land area and fixed asset infrastructure investment (CAPEX) of hydrogen production and synthesis chemical plants. Attached Figure Description

[0025] Figure 1 is a schematic diagram of the physical topology of the SAF syngas control system based on cross-domain electrical feedforward provided in an embodiment of the present invention.

[0026] Figure 2 is a schematic diagram of the main flow of the dynamic phase-locked loop control method for the carbon-hydrogen ratio provided in an embodiment of the present invention.

[0027] Figure 3 is a comparison of the time-domain response and phase compensation waveforms of hydrogen and carbon monoxide when subjected to a power drop impact at the source end in an embodiment of the present invention.

[0028] Explanation of reference numerals in the attached diagram: 1-External fluctuating power supply; 10-Solid-state transformer; 11-Underlying main control board; 20-Electrolysis water hydrogen production device; 30-Hydrogen buffer tank; 40-Carbon monoxide gas source; 50-First high-speed regulating valve; 60-Second high-speed regulating valve; 70-Static mixer; 80-Fischer-Tropsch reactor; 99-High-frequency hard-wired communication link; 100-Inter-domain phase-locked loop controller; 110-Mass flow meter. Detailed Implementation

[0029] To make the objectives, technical solutions, physical mechanisms, and significant advancements of this invention clearer, the invention will be further described in great detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the principles and processes of this invention and are not intended to limit the invention.

[0030] Referring to Figure 1, the method of the present invention relies on a cross-physical domain hardware architecture that breaks through the boundaries of traditional processes. The system macroscopically includes an electrical power supply assembly and a fluid gas supply assembly. The core of the electrical power supply assembly is a solid-state transformer (10) and an electrolytic water hydrogen production device (20); the fluid gas supply assembly includes a hydrogen buffer tank (30) with huge gas resistance and gas capacity characteristics, a carbon monoxide gas source (40), a first high-speed regulating valve (50), a second high-speed regulating valve (60), a static mixer (70), and a Fischer-Tropsch reactor (80) filled with a cobalt-based / iron-based catalyst that is extremely sensitive to the carbon-hydrogen ratio. Among them, the most core digital hub of the system is a cross-domain phase-locked controller (100), which is directly connected to the underlying main control board (11) of the solid-state transformer (10) with a microsecond delay through a high-frequency hardwired communication link (99) that supports clock synchronization, such as optical fiber, PROFINET IRT, or EtherCAT. Based on this high-speed communication hardware base, this embodiment elaborates in detail the SAF syngas C-H ratio dynamic phase-locked loop control method for dealing with source power fluctuations.

[0031] Referring to Figure 2, this dynamic phase-locked control method (DPLL algorithm) is executed continuously and cyclically in the microprocessor of the cross-domain phase-locked controller (100) at an extremely high polling frequency (e.g., 1 millisecond or less). The core of the method covers four main logical steps:

[0032] Step S1 (State Awareness and High-Frequency Filtering Feature Extraction): In this step, the cross-domain phase-locked controller (100) completely abandons the traditional path of relying on the mass flow meter (110) on the fluid pipeline for reactive feedback, and instead directly extracts the transient active power P(t) output by the solid-state transformer (10) in real time via the high-frequency hard-wired communication link (99). In order to prevent the normal harmonic interference or high-frequency noise of the power grid from triggering malfunctions, the controller microprocessor runs a high-frequency edge filtering algorithm for the characteristics of high-power power electronic switches to smooth P(t) (the high-frequency edge filtering algorithm refers to a customized filtering logic specifically used to strip away the specific electromagnetic harmonics generated by the high-frequency switching of the solid-state transformer IGBT and extract the pure power grid drop envelope), and then performs a first-order time differential calculation to obtain the accurate active power change slope dP / dt. When the microprocessor determines that dP / dt is less than the preset negative drop threshold (e.g., the characteristic slope of a power drop within tens of milliseconds caused by cloud shading of a photovoltaic array), it triggers the system to jump out of the conventional steady-state fluid hysteresis regulation link (which represents the conventional operating condition mechanism that relies on fluid sensors to eliminate large inertia and long-period errors during the grid's stable period) and instantly switch to the highest priority cross-domain electrical forced takeover mode (the cross-domain electrical forced takeover mode refers to the underlying protection mechanism in which, within a millisecond window of a sharp drop at the source, the system's highest authority deprives the fluid domain of control, and the fluid actuator is completely driven by the first derivative of the electrical domain).

[0033] Step S2 (Navier-Stokes fluid delay prediction): After entering phase-locked mode, the system does not immediately and blindly close the downstream valve (because at this time, due to the presence of residual gas in the pipeline, the hydrogen at the reactor inlet does not decrease immediately). The microprocessor instantly starts the preset cross-domain electrical and fluid dynamics coupling model. Since the hydrogen production drops sharply from the water electrolysis hydrogen production unit (20), to the volume flowing through the hydrogen buffer tank (30) (equivalent to a large capacitor in the circuit), and then along the long-distance pipeline with friction loss, there must be a physical propagation delay that conforms to the fluid dynamics equation. The controller solves the simplified model of the fluid partial differential equation in real time based on the current dynamic operating pressure of the pipeline, the liquid level / gas pressure state of the buffer tank, and the gas constant, and accurately estimates the dynamic pneumatic transmission delay time T_delay (this value usually fluctuates dynamically between several seconds and more than ten seconds) necessary for the "pressure trough" formed by this hydrogen production reduction to physically diffuse from the generation end and reach the front end of the first high-speed regulating valve (50). This method, which precisely maps the attenuation of fluid pressure distribution in space to the phase difference parameter on the controller's time axis, is one of its core original features.

[0034] Step S3 (Dead Zone Compensation and Phase Lead Generation): After obtaining the core parameter T_delay, the control algorithm is further backward compatible with the mechanical characteristics of the actuator. Considering that even the highest performance second high-speed regulating valve (60), its electric positioner, after receiving the electrical signal command, overcomes static friction, overcomes mechanical spring resistance, and pushes the valve core to actually move into position, also has an inherent mechanical response time constant and action dead zone T_stroke. Therefore, the microprocessor extracts the reference advance amount on the time control axis and calculates the dynamic lead phase compensation time T_adv for the carbon monoxide intake valve through the preset fluid-mechanical dynamic coupling timing model. This coupling model nonlinearly integrates the decay time constant of the fluid pressure trough and the electromagnetic drive dead zone time constant of the pneumatic servo valve core overcoming static friction. This timing reconstruction is not a simple linear time addition and subtraction, but constitutes a nonlinear spatiotemporal phase anchoring (i.e., a time-domain-spatial conversion compensation equation calculated based on the Navier-Stokes fluid decay equation). This step establishes a clear rule for the system: "In order for the valve to be in the closed position exactly at the moment when the hydrogen actually decreases, the system must forcibly pull the trigger to close the valve at a time T_adv milliseconds before the trough arrives."

[0035] Step S4 (Nonlinear Phase-Locked Execution): Referring to the waveform comparison principle in Figure 3, when the countdown reaches T_adv at the predicted trough arrival time, the controller forcibly bypasses the measurement feedback of any flow meter and directly drives the second high-speed regulating valve (60) to move downstream. To prevent the sudden change in the flow field and the violent oscillation of the syngas ratio caused by the simple and crude "one-time linear shutdown", this system adopts nonlinear following logic. **Because the attenuation of gas in long-distance complex pipelines is affected not only by the gas capacity of the buffer tank, but also by the dynamic change of the gas resistance along the path. Therefore, the controller does not call the statically preset exponential curve, but integrates the current fluid damping coefficient and the electrical power drop depth in real time, and dynamically calculates a nonlinear shutdown command with adaptive spatial damping characteristics, so that the carbon monoxide intake shutdown trajectory is highly consistent with the natural physical attenuation trajectory of hydrogen due to the aerodynamic spatial diffusion effect in terms of geometry. This process forces the carbon monoxide flow curve to perfectly track the hydrogen decay curve in time phase, achieving absolute "phase-locked" operation of the two gases during the complex transient decline process.

[0036] Parallel safety control (low-level hard clamping): During the entire load reduction and phase-locked loop execution cycle, the system's background thread executes the low-level hard clamping defense logic at high speed with the highest interrupt priority: Regardless of whether the front-end prediction model deviates or the valve mechanism jams, once the microprocessor calculates through the pipeline fluid dynamics state that the actual dynamic ratio of H2 to CO in the mixed gas entering the Fischer-Tropsch reactor (80) in the current or future tens of milliseconds is close to the absolute safety bottom line (usually set to not less than 1.8:1), the second high-speed regulating valve (60) is immediately and unconditionally cut off. The underlying engineering value of the system is: "It is better to have no synthesis gas available for a short time and put the reactor into hibernation than to allow even a millisecond of hydrogen-poor and carbon-rich environment to cause local carbon deposition and coking of the catalyst."

[0037] Anti-disturbance asymmetric recovery mechanism: In addition, the flexible chemical system not only has to cope with load reduction, but also with strong ramp-up. When the source-end gusts recover or the clouds move away, the power of the solid transformer (10) recovers rapidly, and dP / dt shows a very large positive value, and the system enters the power ramp-up period. Since hydrogen pressure build-up is slow, while CO gas pressure build-up is fast, if the two valves open simultaneously and quickly, carbon enrichment will still occur instantly. Therefore, during the ramp-up period, the controller adopts a very intelligent "asymmetric phase shift compensation strategy". That is, the opening rate of the second high-speed regulating valve (60) is deliberately delayed by the algorithm to make it significantly lag behind the actual recovery ramp-up phase of hydrogen pressure. This lag phase difference is not a fixed parameter, but is determined by the real-time reverse clamping of the transient thermodynamic anti-carbon deposition boundary conditions inside the Fischer reactor. **From the algorithm logic, it is guaranteed that the entire system strictly maintains a "hydrogen-rich state" throughout the entire process of experiencing severe disturbance and recovering to steady state, thus avoiding any possibility of the Boudouard side reaction.

[0038] The detailed deductions and steps described above are merely preferred examples of specific implementations of the present invention, but the scope of protection and technical concept of the present invention are not limited thereto. Any equivalent deductions, parameter changes, or component substitutions that can be easily conceived by those skilled in the art of cross-physical domain control (such as electrical automation and fluid chemical engineering) within the scope of the technical mechanisms disclosed in the present invention, such as changing the extracted electrical characteristics from active power to DC current, or changing exponential turn-off to polynomial fitting turn-off, should undoubtedly be covered within the legal protection scope of the present invention.

Claims

1. A dynamic phase-locked loop control method for the C-H ratio of SAF syngas to cope with source-end power fluctuations, the method being applied to a flexible synthesis system across physical domains driven by fluctuating renewable energy sources and comprising a solid-state transformer, a water electrolysis hydrogen production unit, and a Fischer-Tropsch reactor, characterized in that, The control process includes the following continuously executed steps: State awareness step: By establishing a high-frequency communication link across the electrical and fluid chemistry domains, the underlying electrical data of the solid-state transformer directly supplying power to the water electrolysis hydrogen production unit is collected in real-time and at high frequency. Electrical characteristic parameters characterizing the transient rate of change of the solid-state transformer's output energy are extracted from this underlying electrical data and used as the feedforward trigger source for the entire control system, thus avoiding the time lag of traditional chemical fluid sensors. Delay prediction step: The electrical characteristic parameters are monitored in real-time. When the instantaneous drop amplitude or change slope of the electrical characteristic parameters meets the preset load reduction trigger condition, a pre-established cross-domain electrical and fluid coupling model is activated. This model comprehensively considers the physical spatial distance of the hydrogen distribution network, the gas capacity of the buffer tank, and the gas resistance of the pipeline. Based on this, it accurately calculates the dynamic pneumatic transmission delay time necessary for the fluid pressure trough formed by the sudden drop in hydrogen production due to the load reduction of the solid-state transformer to be physically transmitted from the outlet of the water electrolysis hydrogen production unit to the inlet of the Fischer-Tropsch reactor. Phase compensation step: The dynamic pneumatic transmission delay time is used as the reference lead amount on the time control axis. Combined with the mechanical dead zone and valve core action response characteristics of the carbon monoxide intake regulating valve, a dynamic advance phase compensation time for the carbon monoxide intake regulating valve is calculated. This advance phase compensation time is used to characterize the time difference that the carbon monoxide valve must perform the shut-off action in advance to compensate for the fluid delay. Phase lock execution step: During the advance phase compensation time before the pressure trough actually reaches the inlet of the Fischer-Tropsch reactor along the pipeline, the conventional hydrogen fluid detection feedback loop is forcibly bypassed at the physical control level. A nonlinear feedforward shut-off command is directly issued to the carbon monoxide intake regulating valve, forcing the carbon monoxide intake flow curve to accurately follow the predicted hydrogen flow decay curve in time phase. This ensures that during the entire transient impact cycle of source-end unloading, the real-time dynamic carbon-hydrogen ratio of hydrogen and carbon monoxide input to the Fischer-Tropsch reactor is strictly locked above the preset safety threshold to prevent catalyst carbon buildup and waste.

2. The control method according to claim 1, characterized in that, In the state perception step, the extracted electrical characteristic parameter is the first time derivative of the active power output of the solid-state transformer; the preset load reduction trigger condition is that the first time derivative is less than the preset negative sudden drop threshold. When this condition is met, the trigger control system immediately switches from steady-state closed-loop mode to transient feedforward phase-locked mode.

3. The control method according to claim 1, characterized in that, In the delay prediction step, the pre-established electrical and fluid coupling model integrates the physical gas capacity parameters and physical gas resistance parameters in the hydrogen buffer distribution branch; the process of calculating the aerodynamic transmission delay time is to convert the spatial distribution attenuation, which is difficult to measure in fluid dynamics, into dynamic time-domain compensation parameters on the cross-physical domain controller execution reference through a clock synchronization mechanism.

4. The control method according to claim 1, characterized in that, The specific control logic of the phase-locked execution step is as follows: using the predicted hydrogen flow rate decay curve as the reference phase signal and the mechanical displacement action of the valve core of the carbon monoxide intake regulating valve as the tracking signal; within the advance phase compensation time, controlling the carbon monoxide intake regulating valve to perform nonlinear shutdown at the adaptive spatial damping rate calculated by dynamic inversion, thereby realizing dynamic phase locking of the two synthesis gas flow rate decline curves in the time dimension.

5. The control method according to claim 1, characterized in that, The preset safety threshold is set to a real-time dynamic carbon-hydrogen ratio of not less than 1.8 to 1; during the entire transient adjustment cycle of the phase-locked execution step, the system executes the underlying hard clamping logic in parallel: when the calculated local transient carbon-hydrogen ratio approaches the preset safety threshold, the carbon monoxide intake is forcibly cut off to ensure that the catalyst in the reactor does not undergo irreversible carbon deposition.

6. The control method according to any one of claims 1 to 5, characterized in that, It also includes an anti-disturbance recovery step: when the first time derivative of the active power of the solid-state transformer is detected to be greater than the preset positive recovery threshold, the control system enters the power ramp-up period; during the power ramp-up period, an asymmetric phase shift compensation strategy based on stoichiometric boundary constraints is initiated; the opening phase of the carbon monoxide intake regulating valve is controlled to lag behind the recovery phase of the hydrogen pressure, and this lag is determined by the real-time reverse clamping of the transient thermodynamic anti-carbon deposition threshold to ensure that the hydrogen-rich state is maintained throughout the process of the system recovering to steady state.

7. A dynamic phase-locked control system for the C-H ratio of SAF syngas to cope with source-end power fluctuations, characterized in that, Includes: electrical power supply assembly, including solid-state transformer and water electrolysis hydrogen production unit; fluid gas supply assembly, including hydrogen buffer distribution branch and carbon monoxide supply branch; Fischer-Tropsch reactor; The flow actuator includes a first high-speed regulating valve and a second high-speed regulating valve respectively disposed on the hydrogen buffer distribution branch and the carbon monoxide supply branch; a cross-domain phase-locked controller, which is communicatively connected to the underlying main control board of the solid-state transformer and electrically connected to the second high-speed regulating valve; the cross-domain phase-locked controller has an embedded microprocessor configured to execute the control method as described in any one of claims 1 to 6.

8. A computer-readable storage medium having a computer program stored thereon, characterized in that, When the program is executed by the processor, it implements the steps of the control method as described in any one of claims 1 to 6.

9. An electronic device comprising a memory and a processor, characterized in that, The memory stores a computer program, and when the processor executes the program, it implements the steps of the control method as described in any one of claims 1 to 6.

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