A timing decoupling type multi-element carbon capture method and system

Abstract

This invention relates to the field of low-carbon energy system control technology, and particularly to a time-decoupled, multi-element carbon capture synergistic flexible control method and system. The method includes: constructing a dynamic load model for modular direct air capture using a time-decoupling approach, achieving real-time response reduction characteristics in the adsorption stage and batch constraint translation characteristics in the regeneration stage; constructing a continuous, flexible, and adjustable load model for the regeneration tower based on decoupling technology for post-combustion carbon capture solvent storage; establishing a multi-level synergistic control strategy based on green electricity supply gradients to construct a dynamic priority order for direct air capture and post-combustion carbon capture; and establishing a full-cycle synergistic optimization model considering carbon assets, with the goal of minimizing the system's net cost parameters, to solve the global operation strategy for modular direct air capture and post-combustion carbon capture. This invention effectively solves the problem of how to transform the carbon capture process into a flexibly adjustable load and achieve synergistic optimization with green electricity.

Description

Technical Field

[0001] This invention relates to the field of low-carbon energy system control technology, and in particular to a time-decoupled multi-element carbon capture and coordinated flexible control method and system. Background Technology

[0002] To achieve the "dual carbon" goal, carbon capture, utilization, and storage (CCUS) technology has become a key pathway. Currently, there are two main types of carbon capture technologies: post-combustion carbon capture (PCC) technology mainly targets high-concentration emission sources (such as power plant flue gas) and separates carbon dioxide through chemical solvents; direct air capture (DAC) technology directly captures low-concentration carbon dioxide from the atmospheric environment.

[0003] The two types of technologies mentioned above face two major systemic bottlenecks in practical applications: First, DAC technology has extremely high unit capture energy consumption due to the need to process a large amount of ambient air. Existing solutions require continuous operation of the equipment to ensure capture efficiency. If traditional high-carbon emission electric power is used, its net carbon removal benefit throughout its entire life cycle will be greatly reduced, and it may even produce a negative emission reduction effect. Second, the conventional PCC system has a rigid load characteristic due to its strong coupling with industrial processes. In order to match the continuous operation requirements of power plants, the PCC system must keep the absorption tower and regeneration tower operating synchronously, making it an uninterrupted rigid load. This rigid operating characteristic makes the system unable to respond to the output characteristics of fluctuating renewable energy sources. It is difficult to absorb intermittent green electricity resources, and it is also unable to actively reduce the load when green electricity is insufficient.

[0004] A deeper technical contradiction lies in the fact that the high energy consumption of DACs (Deposit Capture Capture) requires them to operate in conjunction with green electricity to achieve net emission reduction value, while the rigid load characteristics of PCCs (Purpose Capture Control) limit the overall system's flexible adjustment capabilities. Existing technologies have not yet solved the problem of flexible transformation of carbon capture loads, making it difficult to achieve spatiotemporal matching between carbon capture resources and fluctuating renewable energy sources.

[0005] The information disclosed in this background section is intended only to enhance the understanding of the general background of this disclosure and should not be construed as an admission or in any way implying that the information constitutes prior art known to those skilled in the art. Summary of the Invention

[0006] This invention provides a time-decoupled multi-element carbon capture synergistic flexible control method and system, which can effectively solve the problems in the background technology.

[0007] To achieve the above objectives, the technical solution adopted by the present invention is as follows:

[0008] A time-decoupled multi-element carbon capture synergistic flexible control method, the method comprising:

[0009] A modular direct air capture dynamic load model is constructed by using a time-series decoupling method to achieve real-time response reduction characteristics in the adsorption stage and batch constraint translation characteristics in the regeneration stage.

[0010] A continuous, flexible, and adjustable load model for the regeneration tower is constructed based on the decoupling technology of post-combustion carbon capture solvent storage, wherein the adjustment of the regeneration tower is constrained by the liquid level state of the solvent storage tank.

[0011] A multi-level coordinated control strategy based on green electricity supply gradient is established to construct a dynamic priority order for direct air capture and post-combustion carbon capture.

[0012] With the goal of minimizing the system's net cost parameters, a system full-cycle collaborative optimization model considering carbon assets is established to solve the global operation strategy of the modular direct air capture and post-combustion carbon capture.

[0013] Furthermore, a dynamic load model for modular direct air capture is constructed, including:

[0014] The modular direct air capture is divided into two independent adsorption and regeneration stages.

[0015] A nonlinear fan power model is established for the adsorption stage, which allows for real-time load reduction by interrupting fan operation;

[0016] A state transition model controlled by the adsorbent saturation threshold is established for the regeneration stage, and configured as a transferable load.

[0017] Furthermore, a continuous, flexible, and adjustable load model for the regeneration tower is constructed, including:

[0018] The solvent storage decoupling of the carbon capture after combustion is defined as the rigid load of the absorption tower and the flexible load of the regeneration tower;

[0019] Establish a linear control relationship between the power of the regeneration tower and the rich liquid flow rate;

[0020] Set the dynamic equation for the solvent storage tank level and its capacity constraints.

[0021] Furthermore, a dynamic priority order is constructed, including:

[0022] The first priority is to ensure the continuous operation of the absorption tower under rigid load;

[0023] The second priority is to forcibly activate the flexible load of the regeneration tower when the tank level reaches its limit;

[0024] The third priority is to allocate the green electricity surplus to accelerate the direct air capture and regeneration stage or the regeneration tower.

[0025] The fourth priority is to start the fan in the direct air capture and adsorption stage.

[0026] Furthermore, when the green electricity meets the mandatory regeneration buffer requirement but is insufficient for the regeneration stage power, the direct air capture adsorption stage is executed first until the adsorbent is saturated.

[0027] Furthermore, the dynamic equation for the solvent storage tank level includes:

[0028] ;

[0029] in, The rich liquid flow rate fed into the regeneration tower is an adjustable control variable. The volume of the rich liquid tank; This refers to the volume of the lean liquid in the tank. The flow rate of the rich liquid flowing out of the absorption tower. is the discrete time step.

[0030] Furthermore, the system net cost parameters include:

[0031] The power supply cost is calculated based on real-time grid electricity price parameters and purchased grid power parameters;

[0032] Equipment wear parameters related to the number of equipment start-ups and shutdowns and operating time;

[0033] The technical benefit value of carbon assets is calculated using the carbon capture amount and the grid carbon emission factor.

[0034] Furthermore, the calculation model for the carbon asset returns includes:

[0035] ;

[0036] in, For carbon asset returns; For carbon price; and These are the capture amounts for PCC and DAC, respectively; To purchase grid power; is the real-time carbon emission factor of the power grid, and T is the carbon asset revenue accounting period.

[0037] A time-decoupled multi-element carbon capture synergistic flexible control system, the system comprising:

[0038] The dynamic load module constructs a modular dynamic load model for direct air capture through time-series decoupling, realizing the real-time response reduction characteristics of the adsorption stage and the batch constraint translation characteristics of the regeneration stage.

[0039] The flexible adjustment module is based on the decoupling technology of post-combustion carbon capture solvent storage to construct a continuous flexible and adjustable load model for the regeneration tower, wherein the adjustment of the regeneration tower is constrained by the liquid level state of the solvent storage tank.

[0040] The priority module establishes a multi-level collaborative control strategy based on the green energy supply gradient, and constructs a dynamic priority order for direct air capture and post-combustion carbon capture.

[0041] The strategy generation module aims to minimize the system's net cost parameters, establishes a system-wide collaborative optimization model that takes carbon assets into account, and solves the global operation strategy for modular direct air capture and post-combustion carbon capture.

[0042] Furthermore, the dynamic load module includes:

[0043] The modular direct air capture system is divided into two independent stages: an adsorption stage and a regeneration stage.

[0044] The load reduction unit establishes a nonlinear fan power model for the adsorption stage, allowing real-time load reduction to be achieved by interrupting fan operation.

[0045] The translational load unit establishes a state transition model for the regeneration stage that is controlled by the adsorbent saturation threshold and is configured as a translational load.

[0046] The technical solution of this invention can achieve the following technical effects:

[0047] By dynamically constructing a time-series decoupled load model for direct air capture, adsorption interruption operation and regeneration shift start-up are achieved. Simultaneously, a solvent storage decoupled flexible model for post-combustion carbon capture is designed to separate the rigid load of the absorption tower from the continuously adjustable characteristics of the regeneration tower. Subsequently, a four-level collaborative control mechanism based on green electricity supply gradient is established, dynamically allocating the load sequence according to the order of flue gas safety assurance, forced regeneration of storage tanks, surplus power allocation, and adsorption replenishment. Finally, through a full-cycle collaborative optimization engine, grid interaction parameters and carbon asset value are integrated to solve the globally optimal strategy, including equipment loss, operating costs, and environmental benefits, with the goal of minimizing net economic costs. This effectively solves the problem of how to transform the carbon capture process into a flexibly adjustable load and achieve collaborative optimization with green electricity.

[0048] The above description is only an overview of the technical solution of this application. In order to better understand the technical means of this application and to implement it in accordance with the contents of the specification, and to make the above and other objects, features and advantages of this application more obvious and understandable, specific embodiments of this application are given below. Attached Figure Description

[0049] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments recorded in the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0050] Figure 1 This is a flowchart illustrating a time-decoupled, multi-element carbon capture synergistic flexible control method.

[0051] Figure 2 Flowchart for flexible collaborative operation of DAC and PCC technologies;

[0052] Figure 3 A schematic diagram illustrating the priority settings for modular decoupling of DAC and PCC system operation;

[0053] Figure 4 A schematic diagram illustrating the green electricity priority for the flexible collaborative operation of DAC and PCC technologies. Detailed Implementation

[0054] The technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings of the embodiments of the present invention. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments.

[0055] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention pertains. The terminology used in this specification is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. The term "and / or" as used herein includes any and all combinations of one or more of the associated listed items.

[0056] Example 1;

[0057] like Figure 1 and Figure 2 As shown, this application provides a time-decoupled multi-element carbon capture synergistic flexible control method, the method comprising:

[0058] S10: A modular direct air capture dynamic load model is constructed through time-series decoupling to achieve real-time response reduction characteristics in the adsorption stage and batch constraint translation characteristics in the regeneration stage.

[0059] S20: A continuous, flexible, and adjustable load model for the regeneration tower is constructed based on the decoupling technology of post-combustion carbon capture solvent storage, wherein the adjustment of the regeneration tower is constrained by the liquid level state of the solvent storage tank.

[0060] S30: Establish a multi-level coordinated control strategy based on green electricity supply gradient to build a dynamic priority order for direct air capture and post-combustion carbon capture.

[0061] S40: With the goal of minimizing the system's net cost parameters, establish a system full-cycle collaborative optimization model that takes carbon assets into account, and solve the global operation strategy of modular direct air capture and post-combustion carbon capture.

[0062] Specifically, this solution is applied to low-carbon energy systems that simultaneously configure direct air capture (DAC) and post-combustion carbon capture (PCC), such as park or power plant systems that incorporate renewable energy sources like wind and solar and can interact with the grid. Firstly, on the DAC side, the existing device is divided into two independent, controlled stages—adsorption and regeneration—based on its operating mechanism, forming a periodically repeatable operating unit. In the adsorption stage, a fan drives air through a solid adsorbent bed to accumulate carbon dioxide load. Preferably, this stage is defined as a real-time responsive load reduction system, where the control system continuously adjusts the fan's power, reduces its output, or temporarily shuts it down based on available green electricity and electricity prices. When green electricity is insufficient or electricity prices rise, the adsorption operation can be interrupted, and the adsorbed carbon dioxide remains in the adsorbent pores. The adsorption phase does not require immediate regeneration, thus enabling rapid start-up and shutdown and reduction capabilities. The regeneration phase is preferably defined as a batch-constrained, shiftable load, i.e., setting an adsorbent saturation threshold. Regeneration is only permitted when the adsorbent load reaches the threshold. Once initiated, regeneration must be continuously executed at approximately rated demand for a preset duration until completion. For example, it may require simultaneous heat supply and vacuum work to desorb carbon dioxide, but its start time can be shifted within the scheduling cycle. The control system prioritizes triggering regeneration during periods of abundant green electricity or low electricity prices to avoid high-energy-consuming operations during periods of high carbon electricity or high electricity prices. Furthermore, considering the fixed-energy-consumption batch characteristics of DAC regeneration—that is, regardless of the load on the adsorbent—once regeneration is initiated, it typically operates at rated conditions, preferably through... The batch mechanism links the number of regeneration cycles to the amount of carbon dioxide released per regeneration cycle, making the capture capacity dependent on the load level at the start of regeneration. This guides the system to initiate regeneration as close to the load threshold as possible to improve capture efficiency per unit energy consumption. Secondly, on the PCC side, addressing the rigid load issue caused by the need for synchronous and continuous operation of the traditional PCC absorber and regeneration towers, a solvent storage decoupling technology is preferred. Rich and lean liquid tanks are configured between absorption and regeneration, relaxing the absorption and regeneration processes into two separable processes. The absorber must operate in accordance with the flue gas flow rate to ensure that the flue gas is not directly discharged; therefore, the absorber is preferably treated as a rigid link under safety constraints, maintaining a stable processing capacity matched to the flue gas side. Its energy consumption mainly comes from blower purging, etc. A relatively stable auxiliary power is assigned the highest priority in the scheduling logic. The regeneration tower achieves continuous and flexible adjustment by regulating the flow rate of the rich liquid fed into the regeneration tower from the rich liquid tank. The regeneration tower load is preferably modeled as a continuously adjustable load that varies with the amount of rich liquid processed. Its adjustable boundary is constrained by the liquid level status and upper and lower capacity limits of the rich liquid tank or lean liquid tank. When green electricity is insufficient, the system allows regeneration to be temporarily suspended. The rich liquid generated by the absorption tower is preferentially stored in the rich liquid tank, and the lean liquid tank provides the existing solvent to support the continuous operation of the absorption tower. When the liquid level of the rich liquid tank approaches the upper limit alarm value, in order to avoid overflow or absorption limitation, the control system triggers forced regeneration to release the tank capacity. Thus, without sacrificing flue gas safety and compliance, the originally uninterrupted regeneration load is transformed into an adjustable continuous load constrained by the liquid level.Then, based on the above-mentioned DAC timing decoupling and PCC storage decoupling, a clear dynamic priority order is preferably established and executed in real-time: the first priority ensures the operation of the PCC absorption tower to ensure that flue gas is not directly discharged; the second priority is to forcibly start or increase the load of the PCC regeneration tower to buffer when the rich liquid tank level approaches the upper limit; the third priority is to allocate the surplus power to the PCC regeneration tower acceleration or DAC regeneration task when the regenerable output exceeds the base load and there is surplus power, depending on the risk level of the rich liquid tank and the saturation state of the DAC adsorbent, so as to complete the high-energy-consumption analysis within the green electricity window; the fourth priority is to start or increase the DAC adsorption fan for air capture replenishment when there is still surplus power or when the electricity price is in a low period and it does not affect the aforementioned safety and buffer constraints; among which, a further preferred provision is: when the green electricity level only meets the second priority but is insufficient to support the fixed power required for DAC regeneration, the system allows only DAC adsorption to be performed to accumulate. The load is loaded and adsorption stops after reaching the saturation threshold, waiting for the next green electricity window before restarting regeneration, thus achieving a time-series synergy of first storing carbon and then regenerating low-carbon energy. Finally, to coordinate electricity price fluctuations, changes in the carbon emission factor of grid-purchased electricity, equipment depreciation, and carbon asset value on a longer time scale, a comprehensive lifecycle synergistic optimization solution process considering carbon assets is preferred: Under the premise of satisfying system power balance constraints, DAC regeneration continuous execution constraints, PCC tank liquid level upper and lower limits constraints, and absorption safety constraints, with the goal of minimizing the total net economic cost of the system, the process comprehensively considers electricity purchase costs, equipment depreciation and material loss costs, and carbon asset revenue. The preferred method is to deduct the indirect carbon emissions caused by grid-purchased electricity from the total capture volume and multiply it by the carbon price to include the revenue. The output is the start-up, shutdown, and shift arrangements of DAC adsorption and regeneration, the continuous adjustment trajectory of the PCC regeneration tower, and the electricity purchase strategy for interaction with the grid throughout the entire scheduling cycle, thereby obtaining a global operation strategy that balances environmental benefits and economics.

[0063] Through the technical solution of this invention, a time-series decoupled load model for direct air capture is dynamically constructed to achieve adsorption interruption operation and regeneration shift start-up; a solvent storage decoupled flexible model for post-combustion carbon capture is designed simultaneously to separate the rigid load of the absorption tower from the continuously adjustable characteristics of the regeneration tower; then, a four-level collaborative control mechanism based on green electricity supply gradient is established to dynamically allocate the load sequence according to the order of flue gas safety assurance, forced regeneration of storage tanks, surplus power allocation, and adsorption replenishment; finally, through a full-cycle collaborative optimization engine, grid interaction parameters and carbon asset value are integrated to solve the globally optimal strategy including equipment loss, operating costs, and environmental benefits with the goal of minimizing net economic cost, effectively solving the problem of how to transform the carbon capture process into a flexibly adjustable flexible load and achieve collaborative optimization with green electricity.

[0064] Furthermore, constructing a modular direct air capture dynamic load model includes:

[0065] Modular direct air capture is divided into two independent adsorption and regeneration stages.

[0066] A nonlinear fan power model is established for the adsorption stage, which allows for real-time load reduction by interrupting fan operation.

[0067] A state transition model for the regeneration stage, controlled by the adsorbent saturation threshold, is established and configured as a transferable load.

[0068] As a preferred embodiment of the above, the description boundary is first taken as one operating cycle of a single direct air capture device. In the adsorption stage, the controlled object is the fan that drives the ambient air through the adsorbent bed and its auxiliary ventilation components. The carbon dioxide load on the adsorbent gradually accumulates with the adsorption operation. By collecting operating information such as fan speed or frequency, air volume, pressure difference, and adsorbent load status, a nonlinear mapping relationship between fan power and adsorption air volume is established, and this adsorption stage is defined as a load that can be reduced: when the output of renewable energy decreases, the upper-level dispatch issues a power rationing order, or the power supply is insufficient, it is allowed to directly reduce the load or even interrupt operation by reducing the fan speed, shutting down the fan, or maintaining minimum ventilation. The adsorption stage is designed to allow interruption without losing the operating logic of the captured carbon dioxide. That is, during the fan shutdown, the carbon dioxide adsorbed in the pores of the adsorbent remains on the adsorbent and is not required to be executed continuously and synchronously with the regeneration stage. This allows the adsorption stage to achieve response reduction on a minute-level or even shorter time scale, just like an interruptible controllable power load, thereby supporting the system's real-time tracking of green electricity fluctuations. In the regeneration stage, the regeneration process is preferably described as The process is constrained by the adsorbent saturation threshold: When the adsorbent load reaches the preset threshold, the device is allowed to switch from the adsorption state to the regeneration state. In the regeneration state, heat energy and vacuum work are required to decompose and release carbon dioxide. Once regeneration is started, it is preferably set to continue until completion within a preset continuous period and cannot be interrupted at will to ensure sufficient decomposition and stable equipment operation. However, its start time is not forcibly synchronized with the adsorption stage, but is allowed to shift within the scheduling cycle. That is, the control system can select an appropriate start time to trigger regeneration based on the sufficiency of green electricity or the off-peak electricity price window, thereby configuring the regeneration stage as a batch-constrained but shiftable load type. Furthermore, regeneration has a fixed energy consumption batch characteristic. It is preferable to manage regeneration as a discrete batch task in the regeneration scheduling strategy: each regeneration trigger corresponds to one batch execution. During the regeneration period, it operates at approximately the rated demand. The amount of carbon dioxide released in the batch is related to the load level in the adsorbent when regeneration is triggered. Therefore, without violating the saturation threshold condition, it is preferable to schedule the regeneration trigger when the adsorbent is close to the saturation threshold and green electricity is sufficient to improve the net capture efficiency per unit energy consumption.

[0069] Furthermore, constructing a continuous, flexible, and adjustable load model for the regeneration tower includes:

[0070] The decoupling of solvent storage for carbon capture after combustion is defined as the rigid load of the absorber and the flexible load of the regeneration tower.

[0071] Establish a linear control relationship between the power of the regeneration tower and the rich liquid flow rate;

[0072] Set the dynamic equation for the solvent storage tank level and its capacity constraints.

[0073] As a preferred embodiment of the above, post-combustion carbon capture preferably includes a rich liquor storage tank and a lean liquor storage tank, arranged between the absorption tower and the regeneration tower. The absorption tower preferably continues to operate according to the safety and compliance requirements for flue gas treatment, and its processing capacity varies with the flue gas flow rate but is not primarily regulated by electrical power. In terms of control strategy, it is defined as a rigid link that must be prioritized: when flue gas enters the absorption tower and forms a rich liquor that flows out of the absorption tower, this rich liquor preferentially enters the rich liquor storage tank for temporary storage. Correspondingly, the lean liquor storage tank provides a source of circulating solvent for the absorption tower, so that when the regeneration tower is slowed down or its load reduced, the absorption process can still maintain continuous capture relying on the lean liquor storage, fundamentally relaxing the absorption process to the point of regeneration. A rigid constraint requiring synchronization is required. Based on the above decoupling structure, a linear control relationship between the regeneration tower power and the rich liquid flow rate is further established on the regeneration side. Preferably, the adjustable control quantity of the regeneration tower is set to the rich liquid flow rate fed into the regeneration tower from the rich liquid storage tank. Accordingly, the operating power of the regeneration tower is defined as an adjustable load that continuously changes with the rich liquid flow rate. That is, in operation control, the smooth increase and decrease of the regeneration tower power is achieved by continuously adjusting the rich liquid inlet flow rate: when green electricity is abundant or the electricity price is favorable, the rich liquid inlet flow rate is increased to enhance the regeneration treatment intensity, thereby increasing the regeneration tower power and accelerating the consumption of rich liquid; when green electricity is insufficient or the system load needs to be reduced, the rich liquid inlet flow rate is reduced to decrease the regeneration tower power. Correspondingly, the flow rate of the rich solution entering the tower can be reduced to near the minimum operating level if necessary to achieve near-pause regeneration, thereby enabling the regeneration tower to have continuous, flexible, and adjustable characteristics without changing the continuous operation of the absorber. To ensure that this flexible adjustment can be implemented stably in the long term without causing tank overflow or absorption supply interruption, it is preferable to set a dynamic equation for the solvent storage tank level and its capacity constraint: the level of the rich solution storage tank changes dynamically with the difference between the amount of rich solution flowing into the absorber and the amount of rich solution flowing out of the regeneration tower, while the level of the lean solution storage tank is related to the difference between the lean solution returned after regeneration and the lean solution consumed by the absorber. In the control and optimization process, it is preferable to set upper and lower limit boundaries for the rich solution storage tank and the lean solution storage tank respectively. The upper limit of the rich liquid storage tank is used to prevent the accumulation of rich liquid from causing the tank to become full, which in turn restricts the operation of the absorption tower. The lower limit of the lean liquid storage tank is used to prevent the absorption tower from being interrupted due to insufficient lean liquid. More preferably, when the liquid level of the rich liquid storage tank approaches the upper limit alarm threshold, the control strategy triggers the regeneration tower to force regeneration or ensure minimum regeneration operation. Even if the green electricity is insufficient, the storage tank capacity is released by maintaining the necessary rich liquid inlet flow to ensure that the absorption tower can continuously treat flue gas without the risk of direct discharge. When the liquid level of the rich liquid storage tank is in the safe range and green electricity is scarce, the regeneration tower is allowed to reduce its load or temporarily suspend operation, so that the rich liquid is preferentially stored in the storage tank and the lean liquid is supported by the lean liquid storage tank to support the continuous absorption process.

[0074] Furthermore, such as Figure 3 and Figure 4 As shown, a dynamic priority order is constructed, including:

[0075] The first priority is to ensure the continuous operation of the absorption tower under rigid load;

[0076] The second priority is to forcibly activate the flexible load of the regeneration tower when the tank level reaches its limit.

[0077] The third priority is to allocate surplus green electricity to accelerate the direct air capture and regeneration stage or regeneration tower.

[0078] The fourth priority is to start the direct air capture and adsorption stage fan.

[0079] As a preferred embodiment of the above, the highest priority is used to ensure the continuous operation of the absorber under rigid load. That is, the control strategy preferably treats the absorber as the safety baseline for preventing direct emissions of flue gas, prioritizing the allocation of necessary operating resources and maintaining stable processing matching the flue gas flow rate under any power conditions. The rich liquor generated from absorption preferentially enters the rich liquor storage tank, while the lean liquor is supplied to the absorber from the lean liquor storage tank, thereby ensuring that the absorption process is not interrupted by downstream regeneration fluctuations. The second priority is used to forcibly activate the flexible load of the regeneration tower when the tank level reaches or approaches its limit. A preferred approach is to set a warning threshold and a limit threshold for the rich liquor storage tank level. When the rich liquor continues to accumulate and causes the level to approach the upper limit, the system... Even when the system is experiencing a shortage of green electricity or needs to reduce load, it triggers the regeneration tower to enter forced regeneration or minimum guaranteed regeneration operation. This is achieved by increasing or maintaining a certain rich liquid inflow rate to release tank capacity, avoiding the risk of the rich liquid tank becoming full and forcing the absorption tower to reduce load. This makes the liquid level safety boundary a hard trigger condition for priority switching. The third priority is used to allocate green electricity surplus to the direct air capture regeneration stage or to accelerate the regeneration tower. Ideally, after satisfying the first two constraints, it is determined in real time whether the renewable energy output exceeds the system's base load to form a usable surplus. If a surplus exists, it is prioritized for two types of high-value energy use: one is to accelerate the regeneration tower, i.e., increase... The first priority is to increase the flow rate of the rich liquid entering the tower and increase the regeneration intensity to accelerate the consumption of rich liquid and replenish lean liquid, especially when the rich liquid level is high but has not triggered forced regeneration, to prevent subsequent overshooting. The second priority is to start or arrange the regeneration task of direct air capture. Regeneration is a high-energy-consuming operation that needs to be completed continuously and whose start time can be shifted. When the adsorbent saturation has reached the regeneration threshold and the current surplus is sufficient to cover the fixed energy consumption window required for regeneration, it is preferable to trigger direct air capture regeneration and run it continuously until completion, so as to arrange the regeneration during the green electricity surplus period to achieve the net emission reduction advantage. In the third priority internal ranking, it is preferable to prioritize the risk level of the rich liquid storage tank and direct air capture. Dynamic selection is made based on the saturation state of air capture: for example, when the rich liquid level approaches the warning threshold, the regeneration tower is accelerated first; when the rich liquid is in the safe zone and the adsorbent is saturated and ready for regeneration, direct air capture regeneration is prioritized to achieve a coordinated allocation of risk-oriented and energy consumption window-oriented approaches; the fourth priority is used to start the fan in the direct air capture adsorption stage, that is, only when the first three priorities have been met and there is still residual green electricity or the operation window is suitable, the adsorption fan power is started or increased for air capture replenishment, and this adsorption stage can be interrupted at any time to achieve real-time load reduction, so it is placed last to ensure that it does not compete with absorption safety, liquid level boundary and high energy consumption regeneration window for resources.

[0080] Furthermore, when green electricity meets the mandatory regeneration buffer requirement but is insufficient for the regeneration stage power, the direct air capture and adsorption stage is prioritized until the adsorbent is saturated.

[0081] As a preferred embodiment of the above, the available green electricity power level, the liquid level of the carbon capture rich liquid storage tank after combustion and its alarm threshold or limit threshold, the minimum guaranteed regeneration intensity currently required by the regeneration tower to release the storage tank capacity and avoid limiting the absorption side, and the rated energy demand window for the direct air capture regeneration stage, which must be continuously met once started; when it is determined that the available green electricity power, after deducting the rigid load of the absorption tower, can cover the minimum forced regeneration power or minimum operating intensity required by the regeneration tower when the liquid level is close to the limit, but at the same time cannot cover the continuous rated power demand required for the direct air capture regeneration stage, the control strategy does not trigger direct air capture regeneration, but switches to adsorption-preferred filling. Operating status: Under the premise of ensuring continuous operation of the absorption tower and maintaining the minimum treatment intensity required for forced regeneration buffer in the regeneration tower, such as by maintaining a certain rich liquid inlet flow rate to slow down the upward trend of the rich liquid tank, the remaining green electricity is preferentially allocated to the direct air capture adsorption stage fan, so that the adsorption stage operates at adjustable power and continuously accumulates adsorbent load; the adsorption stage is configured as a load that can be reduced at any time and can be interrupted at any time. Therefore, when the green electricity is only moderately insufficient and does not meet the continuous regeneration window, carbon dioxide can still be temporarily stored in the pores of the adsorbent through adsorption, realizing the time-series decoupling benefits of storing carbon first and then regenerating at the opportune time, and avoiding the interruption of the regeneration process or the use of high-carbon electricity due to accidental triggering of regeneration under the condition of insufficient green electricity.

[0082] Furthermore, the dynamic equation for the solvent storage tank level includes:

[0083] ;

[0084] in, The rich liquid flow rate fed into the regeneration tower is an adjustable control variable. The volume of the rich liquid tank; This refers to the volume of the lean liquid in the tank. The flow rate of the rich liquid flowing out of the absorption tower. is the discrete time step.

[0085] In a preferred embodiment, the change in the volume of the rich liquid in the tank over time is determined by two flow rate differences: one is the rich liquid flow rate generated and discharged during the continuous operation of the absorber, which is preferably determined by the flue gas flow rate and absorption conditions, and is usually used as an externally given or measurable input quantity, representing the inflow into the rich liquid tank; the other is the rich liquid flow rate fed from the rich liquid tank into the regeneration tower for analytical processing, which is set as an adjustable control variable, representing the outflow from the rich liquid tank. The control system can continuously change the processing intensity and power level of the regeneration tower by adjusting this flow rate. Correspondingly, the change in the liquid volume of the lean solution tank is complementary to the two flow rates mentioned above. That is, the regeneration tower processes the rich solution and recycles the lean solution, which is equivalent to the inflow into the lean solution tank, while the absorption tower takes solvent from the lean solution tank for absorption and circulation, which is equivalent to the outflow from the lean solution tank. Therefore, the change in the liquid volume of the lean solution tank over time can be characterized by the difference between the flow rate of the rich solution fed into the regeneration tower and the flow rate of the rich solution flowing out of the absorption tower. This forms a pair of mutually coupled and opposite-directed descriptions of liquid level dynamics: when the treatment intensity on the regeneration side increases, the liquid level in the rich solution tank decreases, and the liquid level in the lean solution tank increases. When the regeneration side reduces or temporarily suspends its load, the level in the rich liquid tank rises and the level in the lean liquid tank falls, while the absorber can still maintain continuous collection for a certain period of time by relying on the remaining amount in the lean liquid tank. More preferably, the liquid storage volume status is used as a real-time status input. During each scheduling period, based on the current rich liquid flow rate generated by the absorber and the currently set rich liquid flow rate fed into the regeneration tower, the liquid storage volume status of the rich liquid tank and the lean liquid tank is updated and compared with their respective upper and lower capacity limits. When the volume of the rich liquid tank continues to rise and approaches the upper limit, it is preferable to increase the flow rate to the regeneration tower. The rich liquid flow rate is increased to accelerate the consumption of rich liquid and release the capacity of the rich liquid tank. When the volume of the lean liquid tank decreases and approaches the lower limit, it is preferable to also increase the rich liquid flow rate fed into the regeneration tower to accelerate the replenishment of lean liquid, or coordinate the absorption conditions without affecting the safety of flue gas, so that the lean liquid tank will not affect the continuous operation of the absorption tower due to insufficient liquid supply. Conversely, when green electricity is insufficient and load reduction is required, and the rich liquid tank is still in the safe range, it is preferable to reduce the rich liquid flow rate fed into the regeneration tower to reduce the power of the regeneration tower, so that the rich liquid is temporarily stored in the rich liquid tank and the lean liquid supports the continuous operation of the absorption tower.

[0086] Furthermore, the system net cost parameters include:

[0087] The power supply cost is calculated based on real-time grid electricity price parameters and purchased grid power parameters;

[0088] Equipment wear parameters related to the number of equipment start-ups and shutdowns and operating time;

[0089] The technical benefit value of carbon assets is calculated using carbon capture volume and grid carbon emission factor.

[0090] As a preferred embodiment of the above, the power supply cost is preferably determined by the real-time electricity price parameters of the power grid and the power purchased from the grid. The control system collects the real-time electricity price of the power grid at each time period as the current electricity unit price input, and records the power level purchased from the power grid as the current power purchased from the grid, and forms the current electricity expenditure accordingly. In particular, when the system has green electricity output, it is preferable to first use green electricity to meet the rigid load of the absorption tower and the buffer demand of forced regeneration, and then decide whether to purchase grid electricity to support the continuous operation of the direct air capture and regeneration stage or to increase the processing intensity of the regeneration tower based on the remaining green electricity and the electricity price level. Thus, the power purchased from the grid becomes a key quantity that changes with decisions such as whether to start high-energy regeneration, whether to speed up regeneration, and whether to reduce adsorption. The equipment loss parameters are preferably related to the number of equipment start-ups and shutdowns and the running time to reflect the impact of frequent start-ups and shutdowns and long-term operation on equipment life and maintenance costs. The number of start-ups and shutdowns is preferably counted separately for the start-ups of the direct air capture and regeneration stage and the start-ups and shutdowns of the fans in the adsorption stage, and can also be counted simultaneously for the regeneration tower from low load. The number of state switching times when switching to forced regeneration or accelerated operation is optimized, and the operating time is preferably accumulated by summarizing the actual operating time of the fan during the adsorption stage, the continuous operating time during the direct air capture and regeneration stage, and the operating time of the regeneration tower at various load levels. These statistics are then mapped to indicators of equipment depreciation, maintenance, or material loss to avoid non-optimal solutions that prioritize short-term electricity cost minimization, leading to excessive start-ups and shutdowns and increased losses. The carbon asset technology benefit value is preferably calculated using carbon capture volume and grid carbon emission factor: the control system records the carbon capture volume after combustion and the capture volume of direct air capture at each time period, and simultaneously obtains the grid carbon emission factor as a characterization of the indirect emission intensity of grid-purchased electricity. The net emission reduction contribution is then formed by deducting the indirect emission impact of grid-purchased electricity from the total emission reduction benefit from capture. Combined with carbon price or carbon asset pricing rules, a quantifiable technology benefit value is obtained. This ensures that when green electricity is insufficient and grid-purchased electricity is necessary to support regeneration, the system will automatically assess whether the purchased grid-purchased electricity will offset the capture benefit, avoiding operating strategies where net emission reduction is negative or benefits are diluted.

[0091] Furthermore, the calculation models for carbon asset returns include:

[0092] ;

[0093] in, For carbon asset returns; For carbon price; and These are the capture amounts for PCC and DAC, respectively; To purchase grid power; is the real-time carbon emission factor of the power grid, and T is the carbon asset revenue accounting period.

[0094] As a preferred embodiment of the above, the capture amounts of PCC and DAC are statistically analyzed at a preset time granularity within the scheduling cycle. The PCC capture amount preferably originates from the cumulative carbon dioxide release generated during the regeneration tower's treatment of the rich liquor, and the DAC capture amount preferably originates from the cumulative carbon dioxide released after the regeneration stage. Both constitute the total carbon capture amount for the current period and are converted into positive carbon asset revenue at the carbon price. Simultaneously, the purchased grid power is considered a representation of the electricity intensity purchased from the grid in the current period, preferably obtained from an energy management system or electricity meter. The real-time carbon emission factor of the grid is also simultaneously acquired as a representation of the unit indirect emission intensity of purchased grid power. Both are used to calculate the indirect carbon emissions from purchased grid power and are converted into a deduction item for carbon asset revenue at the same carbon price, thereby forming a system where the more carbon captured, the more revenue generated. The system exhibits a linkage where greater benefits lead to greater grid purchases and higher grid carbon emissions, resulting in greater offsets. More preferably, to ensure the revenue model can be directly used for online control and rolling optimization, the system executes a closed loop of data acquisition, revenue updates, and strategy feedback within each scheduling period: it collects the current PCC and DAC capture volumes, purchased grid power, and the grid's real-time carbon emission factor; updates the current carbon asset revenue and inputs it as part of the net cost into the optimizer. This ensures that, under the premise of satisfying the continuous operation of the absorption tower, the tank level boundary, and the DAC regeneration continuity constraints, the optimizer tends to schedule high-energy-consumption regeneration during periods of green electricity surplus or lower grid carbon emission factors. This reduces the situation where DAC regeneration is forcibly started through grid purchases during high-carbon grid periods, thus aligning with the goal that DAC must work in conjunction with green electricity to achieve net emission reduction value.

[0095] Example 2;

[0096] Based on the same inventive concept as the time-decoupled multi-element carbon capture synergistic flexible control method in the foregoing embodiments, the present invention also provides a time-decoupled multi-element carbon capture synergistic flexible control system, the system comprising:

[0097] The dynamic load module constructs a modular dynamic load model for direct air capture through time-series decoupling, realizing the real-time response reduction characteristics of the adsorption stage and the batch constraint translation characteristics of the regeneration stage.

[0098] The flexible adjustment module is based on the decoupling technology of post-combustion carbon capture solvent storage to construct a continuous flexible and adjustable load model for the regeneration tower, wherein the adjustment of the regeneration tower is constrained by the liquid level state of the solvent storage tank.

[0099] The priority module establishes a multi-level collaborative control strategy based on the green energy supply gradient, and constructs a dynamic priority order for direct air capture and post-combustion carbon capture.

[0100] The strategy generation module aims to minimize the system's net cost parameters, establishes a system-wide collaborative optimization model that takes carbon assets into account, and solves the global operation strategy for modular direct air capture and post-combustion carbon capture.

[0101] The adjustment system described above in this invention can effectively realize a time-decoupled multi-element carbon capture synergistic flexible control method, and the technical effects it can achieve are as described in the above embodiments, and will not be repeated here.

[0102] Furthermore, the dynamic load module includes:

[0103] The modular direct air capture system is divided into two independent stages: an adsorption stage and a regeneration stage.

[0104] The load reduction unit establishes a nonlinear fan power model for the adsorption stage, allowing real-time load reduction to be achieved by interrupting fan operation.

[0105] The translational load unit establishes a state transition model for the regeneration stage that is controlled by the adsorbent saturation threshold and is configured as a translational load.

[0106] Similarly, the above-mentioned optimization schemes for the system can also achieve the optimization effects corresponding to the methods in Embodiment 1, which will not be repeated here.

[0107] Although this application has been described in conjunction with specific features and embodiments, it is obvious that various modifications and combinations can be made thereto without departing from the spirit and scope of this application. Accordingly, this specification and drawings are merely exemplary illustrations of the application as defined herein, and are to be considered as covering any and all modifications, variations, combinations, or equivalents within the scope of this application. Clearly, those skilled in the art can make various alterations and modifications to this application without departing from its scope. Thus, if such modifications and modifications fall within the scope of this application and its equivalents, this application intends to include such modifications and modifications.

Claims

1. A time-decoupled, multi-element carbon capture synergistic flexible control method, characterized in that, The method includes: A modular direct air capture dynamic load model is constructed by using a time-series decoupling method to achieve real-time response reduction characteristics in the adsorption stage and batch constraint translation characteristics in the regeneration stage. A continuous, flexible, and adjustable load model for the regeneration tower is constructed based on the decoupling technology of post-combustion carbon capture solvent storage, wherein the adjustment of the regeneration tower is constrained by the liquid level state of the solvent storage tank. A multi-level coordinated control strategy based on green electricity supply gradient is established to construct a dynamic priority order for direct air capture and post-combustion carbon capture. With the goal of minimizing the system's net cost parameters, a system full-cycle collaborative optimization model considering carbon assets is established to solve the global operation strategy of the modular direct air capture and post-combustion carbon capture.

2. The time-decoupled multi-element carbon capture synergistic flexible control method according to claim 1, characterized in that, Construct a modular dynamic load model for direct air capture, including: The modular direct air capture is divided into two independent adsorption and regeneration stages. A nonlinear fan power model is established for the adsorption stage, which allows for real-time load reduction by interrupting fan operation; A state transition model controlled by the adsorbent saturation threshold is established for the regeneration stage, and configured as a transferable load.

3. The time-decoupled multi-element carbon capture synergistic flexible control method according to claim 2, characterized in that, Constructing a continuous, flexible, and adjustable load model for the regeneration tower includes: The solvent storage decoupling of the carbon capture after combustion is defined as the rigid load of the absorption tower and the flexible load of the regeneration tower; Establish a linear control relationship between the power of the regeneration tower and the rich liquid flow rate; Set the dynamic equation for the solvent storage tank level and its capacity constraints.

4. The time-decoupled multi-element carbon capture synergistic flexible control method according to claim 3, characterized in that, Constructing a dynamic priority order includes: The first priority is to ensure the continuous operation of the absorption tower under rigid load; The second priority is to forcibly activate the flexible load of the regeneration tower when the tank level reaches its limit; The third priority is to allocate the green electricity surplus to accelerate the direct air capture and regeneration stage or the regeneration tower. The fourth priority is to start the fan in the direct air capture and adsorption stage.

5. The time-decoupled multi-element carbon capture synergistic flexible control method according to claim 4, characterized in that, When green electricity meets the mandatory regeneration buffer requirement but is insufficient for the regeneration stage power, the direct air capture adsorption stage is executed first until the adsorbent is saturated.

6. The time-decoupled multi-element carbon capture synergistic flexible control method according to claim 3, characterized in that, The dynamic equation for the solvent storage tank level includes: ； in, The rich liquid flow rate fed into the regeneration tower is an adjustable control variable. The volume of the rich liquid tank; This refers to the volume of the lean liquid in the tank. The flow rate of the rich liquid flowing out of the absorption tower. is the discrete time step.

7. The time-decoupled multi-element carbon capture synergistic flexible control method according to claim 1, characterized in that, The system net cost parameters include: The power supply cost is calculated based on real-time grid electricity price parameters and purchased grid power parameters; Equipment wear parameters related to the number of equipment start-ups and shutdowns and operating time; The technical benefit value of carbon assets is calculated using the carbon capture amount and the grid carbon emission factor.

8. The time-decoupled multi-element carbon capture synergistic flexible control method according to claim 7, characterized in that, The calculation models for carbon asset returns include: ； in, For carbon asset returns; For carbon price; and These are the capture amounts for PCC and DAC, respectively; To purchase grid power; is the real-time carbon emission factor of the power grid, and T is the carbon asset revenue accounting period.

9. A time-decoupled multi-element carbon capture synergistic flexible control system, characterized in that, The system includes: The dynamic load module constructs a modular dynamic load model for direct air capture through time-series decoupling, realizing the real-time response reduction characteristics of the adsorption stage and the batch constraint translation characteristics of the regeneration stage. The flexible adjustment module is based on the decoupling technology of post-combustion carbon capture solvent storage to construct a continuous flexible and adjustable load model for the regeneration tower, wherein the adjustment of the regeneration tower is constrained by the liquid level state of the solvent storage tank. The priority module establishes a multi-level collaborative control strategy based on the green energy supply gradient, and constructs a dynamic priority order for direct air capture and post-combustion carbon capture. The strategy generation module aims to minimize the system's net cost parameters, establishes a system-wide collaborative optimization model that takes carbon assets into account, and solves the global operation strategy for modular direct air capture and post-combustion carbon capture.

10. The time-decoupled multi-element carbon capture synergistic flexible control system according to claim 9, characterized in that, The dynamic load module includes: The modular direct air capture system is divided into two independent stages: an adsorption stage and a regeneration stage. The load reduction unit establishes a nonlinear fan power model for the adsorption stage, allowing real-time load reduction to be achieved by interrupting fan operation. The translational load unit establishes a state transition model for the regeneration stage that is controlled by the adsorbent saturation threshold and is configured as a translational load.

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