Efficient deoxygenation system and optimized control method thereof

Abstract

This application relates to the field of boiler feedwater deoxygenation technology, and in particular to a high-efficiency deoxygenation system and its optimized control method. It includes: establishing an operational control model with a temperature control structure; pre-setting multiple deoxygenation cycles, and setting control sub-models for each deoxygenation cycle based on unit operating data and the operational control model; acquiring monitoring data of the deaerator according to preset correction time nodes, and determining whether to generate correction instructions for the control sub-model based on the monitoring data; by adding a temperature control structure and operational control model, dynamically controlling the internal operating temperature of the deaerator using a temperature auxiliary bypass and temperature adjustment loop, ensuring that the deaerator can quickly reach and maintain the optimal deoxygenation temperature under various operating conditions; and by adding an auxiliary unit (i.e., a heating device), executing a switching sub-strategy during operating condition switching to quickly compensate for temperature deviations caused by different operating condition switching, ensuring continuous and stable deoxygenation effect.

Description

Technical Field

[0001] This application relates to the field of boiler feedwater deoxygenation technology, and in particular to a high-efficiency deoxygenation system and its optimized control method. Background Technology

[0002] Currently, deaerators remove dissolved oxygen by heating feedwater to saturation, making them a core component for ensuring feedwater quality. Existing deaeration systems are typically designed and operated under rated conditions, and their efficiency is highly dependent on stable condensate inlet temperature and load conditions. However, in actual operation, especially under low unit load, cold start-up, or when heat exchanger efficiency decreases, persistently low condensate temperatures often occur, leading to the following prominent problems with existing technology:

[0003] First, heating low-temperature condensate requires more and higher-grade steam, significantly increasing energy consumption. Furthermore, auxiliary heating devices often lack precise and coordinated control, leading to reduced energy efficiency and localized thermal stress. Second, fixed-structure deaerators are ill-suited to varying operating conditions, resulting in decreased mass and heat transfer efficiency and difficulty in consistently achieving adequate deaeration. Third, increasing the medium flow rate to compensate for heat load can easily induce fluid vibration in the pipeline, posing mechanical fatigue and safety hazards. Traditional systems lack effective vibration monitoring and proactive control measures. Additionally, system operation relies heavily on distributed instruments and manual experience, hindering early fault warnings and predictive maintenance, resulting in high maintenance costs and insufficient reliability. Summary of the Invention

[0004] The purpose of this application is to provide a high-efficiency deoxygenation system and its optimized control method to solve the above-mentioned technical problems, aiming to improve the deoxygenation efficiency of the deaerator for boiler feedwater and ensure the efficient operation of the unit.

[0005] In some embodiments of this application, by adding a temperature control structure and an operation regulation model, the operating temperature inside the deaerator is dynamically controlled using a temperature-assisted bypass and a temperature regulation loop. This ensures that the deaerator can quickly reach and maintain the optimal deoxygenation temperature under various operating conditions, thereby improving the deoxygenation efficiency of the deaerator for boiler feedwater and ensuring the efficient operation of the unit.

[0006] In some embodiments of this application, the deoxygenation efficiency is improved, and an auxiliary unit (i.e., a heating device) is added to execute a switching sub-strategy when switching operating conditions, which quickly compensates for the temperature deviation caused by the switching of different operating conditions, achieves a smooth transition, avoids drastic fluctuations in temperature and pressure, and ensures the continuous and stable deoxygenation effect.

[0007] In some embodiments of this application, an optimized control method for a high-efficiency deoxygenation system is provided, including: Establish an operation and control model for the temperature control structure; Multiple deoxygenation cycles are preset, and control sub-models for each deoxygenation cycle are set according to unit operating data and operating control models. The monitoring data of the deaerator is obtained according to the preset correction time node, and the correction instruction of the control sub-model is determined based on the monitoring data. The temperature control structure includes: a main steam circuit, a temperature auxiliary bypass, and a temperature adjustment circuit.

[0008] In some embodiments of this application, the operating control model of the temperature control structure includes: Multiple operating modes are set based on the unit's historical operating data; Establish a sequence of working condition modes A, A=(a1, a2, ..., ai, ..., an), where ai is the i-th working condition mode; n is the number of working condition modes; Based on the working condition mode sequence A, ai is sequentially set as the target mode; A target mode operation sub-model is defined, the operation sub-model including: control strategy and mode switching strategy; The operation sub-models for each working condition are set sequentially, and the operation control model is constructed based on all the operation sub-models.

[0009] In some embodiments of this application, the running sub-model for setting the target mode includes: Select the operating steam source; Set multiple steam source temperature ranges; Set the primary control parameters for each gas source temperature range; The primary control parameters include: the valve opening degree of the main steam circuit and the desuperheating parameters of the temperature auxiliary bypass; Set multiple inlet water temperature ranges; Set the secondary control parameters for each inlet water temperature range; The secondary control parameters include: the valve opening degree of the temperature auxiliary bypass and the circulating water volume of the temperature control circuit; The control strategy for the target mode is set based on the primary control parameters and the secondary control parameters.

[0010] In some embodiments of this application, the running sub-model for setting the target mode further includes: Based on the working condition mode sequence A, ai is sequentially set as the evaluation mode; The duration of fluctuations when switching between the target mode and the evaluation mode; The evaluation mode is set according to the switching fluctuation duration to determine the switching sub-strategy for the target mode; Generate sub-strategies for switching between each operating mode and the target mode in sequence; Construct a mode switching strategy for the target mode based on all switching example strategies.

[0011] In some embodiments of the present application, the control sub-model for setting each deaeration cycle includes: Obtain the unit operation data of the current deaeration cycle and generate the operation mode of the current deaeration cycle; Select the execution regulation strategy for the current deaeration cycle according to the operation mode; Obtain the historical operation mode of the previous deaeration cycle; Set the execution switching strategy for the current deaeration cycle according to the historical operation mode; Establish the correction time axis of the current deaeration cycle, and the correction time axis includes multiple correction time nodes; Construct the control sub-model of the current deaeration cycle, and the control sub-model includes: correction time axis, execution switching strategy and execution regulation strategy.

[0012] In some embodiments of the present application, the judgment of whether to generate a correction instruction for the control sub-model includes: Obtain the outlet water temperature of the deaerator at the current correction time node; Generate a deaeration deviation value f according to the outlet water temperature; Preset a first deaeration deviation value threshold F1 and a second deaeration deviation value threshold F2, and F1 < F2; If f > F1, no correction instruction is generated at the current correction time node; If F1 < f < F2, a first-level correction instruction is generated at the current correction time node; If f > F2, obtain the unit operation data at the current correction time, and judge whether to generate a correction instruction according to the unit operation data.

[0013] In some embodiments of the present application, the judgment of whether to generate a correction instruction according to the unit operation data includes: Generate the working condition fluctuation value k at the current correction time node k = (si - s'i) 2 ; where θ is the number of working condition characteristic indexes; si is the real-time reference value of the i-th working condition characteristic index at the current correction time node; s'i is the expected reference value of the i-th working condition characteristic index within the current deaeration cycle; Preset a working condition fluctuation value threshold K1; If k < K1, a second-level correction instruction for the control sub-model is generated at the current correction time node; If k > K1, a switching correction instruction is generated at the current correction time node.

[0014] In some embodiments of the present application, an efficient deaeration system is provided, including: A deaerator for treating boiler feed water; The temperature control structure includes: a main steam circuit, a temperature auxiliary bypass, and a temperature regulation circuit; The temperature control structure is connected to the deaerator; The temperature control structure is used to control the operating temperature of the deaerator; The monitoring unit is used to acquire unit operating data; An auxiliary unit, located inside the deaerator, is used to control the operating temperature of the deaerator according to the execution switching strategy and the first-level correction command. The central control unit is used to establish the operation and control model of the temperature control structure; The central control unit includes: The first processing module is used to preset multiple deoxygenation cycles; The first processing module is also used to set control sub-models for each deoxygenation cycle based on unit operating data and operating control model; The second processing module is used to acquire monitoring data of the deaerator according to a preset correction time node; The second processing module is also used to determine whether to generate a correction instruction for the control sub-model based on the monitoring data.

[0015] In some embodiments of this application, the central control unit further includes: The third processing module is used to set multiple operating modes based on the unit's historical operating data; Establish a sequence of working condition modes A, A=(a1, a2, ..., ai, ..., an), where ai is the i-th working condition mode; n is the number of working condition modes; Based on the working condition mode sequence A, ai is sequentially set as the target mode; A target mode operation sub-model is defined, the operation sub-model including: control strategy and mode switching strategy; The operation sub-models for each working condition are set sequentially, and the operation control model is constructed based on all the operation sub-models; The sub-model for setting the target mode includes: Select the operating steam source; Set multiple steam source temperature ranges; Set the primary control parameters for each gas source temperature range; The primary control parameters include: the valve opening degree of the main steam circuit and the desuperheating parameters of the temperature auxiliary bypass; Set multiple inlet water temperature ranges; Set the secondary control parameters for each inlet water temperature range; The secondary control parameters include: the valve opening degree of the temperature auxiliary bypass and the circulating water volume of the temperature control circuit; The control strategy for the target mode is set based on the primary control parameters and the secondary control parameters; Based on the working condition mode sequence A, ai is sequentially set as the evaluation mode; The duration of fluctuations when switching between the target mode and the evaluation mode; The evaluation mode is set according to the switching fluctuation duration to determine the switching sub-strategy for the target mode; Generate sub-strategies for switching between each operating mode and the target mode in sequence; Construct a mode switching strategy for the target mode based on all switching example strategies.

[0016] In some embodiments of this application, the first processing module is further configured to: Acquire the unit operating data for the current deoxygenation cycle and generate the operating mode for the current deoxygenation cycle; Select the execution control strategy for the current deoxygenation cycle based on the operating mode; Obtain the historical operating mode of the previous deoxygenation cycle; The execution switching strategy for the current deoxygenation cycle is set based on historical operating patterns; Establish a corrected time axis for the current deoxygenation cycle, which includes multiple corrected time nodes; Construct a control sub-model for the current deoxygenation cycle. The control sub-model includes: correcting the time axis, executing a switching strategy, and executing a regulation strategy.

[0017] Compared with the prior art, the advantages of the high-efficiency deoxygenation system and its optimized control method described in this application are as follows: By adding a temperature control structure and operation regulation model, the operating temperature inside the deaerator is dynamically controlled using a temperature-assisted bypass and temperature regulation loop. This ensures that the deaerator can quickly reach and maintain the optimal deoxygenation temperature under various operating conditions, thereby improving the deoxygenation efficiency of the deaerator for boiler feedwater and ensuring the efficient operation of the unit.

[0018] To improve deoxygenation efficiency, an auxiliary unit (i.e., a heating device) is added to execute a switching sub-strategy when switching operating conditions. This quickly compensates for temperature deviations caused by switching between different operating conditions, achieving a smooth transition, avoiding drastic fluctuations in temperature and pressure, and ensuring continuous and stable deoxygenation performance. Attached Figure Description

[0019] Figure 1 This is a schematic diagram of the structure of an optimized control method for a high-efficiency deoxygenation system in a preferred embodiment of this application. Detailed Implementation

[0020] The specific embodiments of this application will be described in further detail below with reference to the accompanying drawings and examples. The following examples are used to illustrate this application, but are not intended to limit the scope of this application.

[0021] In the description of this application, it should be understood that the terms "center", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are only for the convenience of describing this application and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this application.

[0022] The terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Therefore, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of this application, unless otherwise stated, "a plurality of" means two or more.

[0023] In the description of this application, it should be noted that, unless otherwise expressly specified and limited, the terms "installation," "connection," and "linking" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection between two components. Those skilled in the art can understand the specific meaning of the above terms in this application based on the specific circumstances.

[0024] like Figure 1 As shown in the preferred embodiment of this application, an optimized control method for a high-efficiency deoxygenation system includes: S101: Establish an operational control model for the temperature control structure; S102: Multiple deoxygenation cycles are preset, and control sub-models for each deoxygenation cycle are set according to unit operation data and operation control model; S103: Obtain the monitoring data of the deaerator according to the preset correction time node, and determine whether to generate the correction instruction of the control sub-model based on the monitoring data; The temperature control structure includes: a main steam circuit, a temperature auxiliary bypass, and a temperature adjustment circuit.

[0025] Specifically, the main steam line can receive main extraction steam or standby steam from the turbine unit (such as steam from the auxiliary steam header). The temperature auxiliary bypass is connected in parallel to the main heating steam line and includes a desuperheater, a fine-tuning steam valve, and shut-off valves before and after it. It is used to desuperheat the steam in the main steam line. The temperature control circuit draws a stream of hot water from the bottom of the deaerator tank and mixes it into the main condensate inlet pipe via a small pump and regulating valve.

[0026] Specifically, by adding a temperature control structure and an operation regulation model, the internal operating water temperature of the deaerator can be adjusted in multiple dimensions.

[0027] In a preferred embodiment of this application, the operation and control model of the temperature control structure includes: Multiple operating modes are set based on the unit's historical operating data; Establish a sequence of working condition modes A, A=(a1, a2, ..., ai, ..., an), where ai is the i-th working condition mode; n is the number of working condition modes; Based on the working condition mode sequence A, ai is sequentially set as the target mode; The target mode is defined as the operating sub-model, which includes: control strategy and mode switching strategy; The operation sub-models for each working condition are set sequentially, and the operation control model is constructed based on all the operation sub-models.

[0028] Specifically, historical operating data is generated by monitoring the historical operating status of the unit, and multiple operating condition characteristic indicators are set based on the historical operating data. These operating condition characteristic indicators include, but are not limited to, parameters related to the steam turbine unit such as heating steam extraction rate, condensate flow rate, feedwater pump speed, and power generation coal consumption. All operating condition characteristic indicators are quantified to ensure that the reference values ​​of each operating condition characteristic indicator are within the same range. Based on all operating condition characteristic indicators, multiple typical operating conditions (such as pure condensing, extraction condensing, and low-pressure cylinder zero-output mode) are generated, thereby establishing multiple operating condition modes. Each operating condition mode represents a typical operating condition.

[0029] Specifically, historical operating data includes parameters such as turbine unit operating condition records, operating gas source monitoring data, historical data of valve opening on the main steam line, desuperheating control data of the temperature auxiliary bypass, and historical data of boiler feedwater.

[0030] Specifically, the operational sub-model of the target mode is defined, including: Select the operating steam source; Set multiple steam source temperature ranges; Set the primary control parameters for each gas source temperature range; The primary control parameters include: the valve opening degree of the main steam line and the desuperheating parameters of the temperature auxiliary bypass; Set multiple inlet water temperature ranges; Set the secondary control parameters for each inlet water temperature range; Secondary control parameters include: the valve opening degree of the temperature auxiliary bypass and the circulating water volume of the temperature control loop; The control strategy for the target mode is set based on the primary control parameters and the secondary control parameters.

[0031] Specifically, the operating steam source refers to the structure that provides steam to the main steam circuit (including but not limited to main extraction steam or backup steam source, such as auxiliary steam header steam, etc.). By analyzing the historical monitoring data of the target mode, a suitable operating steam source is selected.

[0032] Specifically, the temperature range of the steam source in the target mode is generated based on historical operating data, and the temperature range is divided into multiple steam source temperature intervals. The valve opening and desuperheating parameters (i.e., the desuperheating valve opening of the temperature auxiliary bypass) in each steam source temperature interval are dynamically set based on historical operating data, so as to ensure that the steam entering the deaerator for the first time can enable the boiler feedwater to quickly reach and maintain the optimal deaeration temperature.

[0033] Specifically, based on historical operating data, the historical temperature range of boiler feedwater in the target mode is generated, and the historical temperature range is divided into multiple inlet water temperature intervals (i.e., the temperature at which boiler feedwater enters the deaerator). Based on historical operating data, the valve opening of the temperature auxiliary bypass corresponding to each inlet water temperature interval and the circulating water volume of the temperature control circuit are dynamically set, so that the steam entering the deaerator for the first time can keep the boiler feedwater temperature stable.

[0034] Specifically, by setting primary and secondary control parameters, when the turbine unit is in the target mode, the operating parameters of the temperature control structure are dynamically adjusted by monitoring the real-time steam source temperature and boiler feedwater temperature.

[0035] Specifically, the operational sub-model for setting the target mode also includes: Based on the working condition mode sequence A, ai is sequentially set as the evaluation mode; The duration of fluctuations when switching between the target mode and the evaluation mode; The evaluation mode is set according to the switching fluctuation duration to determine the switching sub-strategy for the target mode; Generate sub-strategies for switching between each operating mode and the target mode in sequence; Construct a mode switching strategy for the target mode based on all switching example strategies.

[0036] Specifically, the switching sub-strategy includes the auxiliary unit's continuous operating time being the same as the switching fluctuation time (the switching fluctuation time refers to the time when the turbine unit switches from the target mode to the evaluation mode, and the temperature control unit cannot maintain stable heating).

[0037] Specifically, the auxiliary unit is a heating device located inside the deaerator. When the turbine unit switches operating conditions, the auxiliary unit actively heats the water inside the deaerator to ensure a stable water temperature.

[0038] It is understandable that in the above embodiments, by adding a temperature control structure and an operation regulation model, the operating temperature inside the deaerator is dynamically controlled using a temperature-assisted bypass and a temperature regulation loop, ensuring that the deaerator can quickly reach and maintain the optimal deoxygenation temperature under various operating conditions, thereby improving the deoxygenation efficiency of the deaerator for boiler feedwater and ensuring the efficient operation of the unit.

[0039] The preferred embodiment of this application sets up a control sub-model for each deoxygenation cycle, including: Acquire the unit operating data for the current deoxygenation cycle and generate the operating mode for the current deoxygenation cycle; Select the execution control strategy for the current deoxygenation cycle based on the operating mode; Obtain the historical operating mode of the previous deoxygenation cycle; The execution switching strategy for the current deoxygenation cycle is set based on historical operating patterns; Establish a corrected timeline for the current deoxygenation cycle, which includes multiple corrected time nodes; Construct a control sub-model for the current deoxygenation cycle. The control sub-model includes: correcting the time axis, executing the switching strategy, and executing the regulation strategy.

[0040] Specifically, the historical operating mode is the operating condition mode corresponding to the control sub-model of the previous deoxygenation cycle.

[0041] Specifically, the control strategy for the operating mode corresponding to the set operating mode is the execution control strategy, and the switching sub-strategy corresponding to the switch from the historical operating mode to the current operating mode is the execution switching strategy.

[0042] Specifically, the duration of a single deaeration cycle can be set according to the operating condition switching frequency of the turbine unit. The higher the operating condition switching frequency, the shorter the duration of the corresponding single deaeration cycle.

[0043] Specifically, the correction time node can be set according to the operating stability of the turbine unit. The higher the stability, the shorter the time interval between adjacent correction time nodes, so as to provide timely early warning and adaptation to the operating condition fluctuations of the turbine unit and ensure the efficient deoxygenation of the deaerator.

[0044] In a preferred embodiment of this application, determining whether to generate a correction instruction for the control sub-model includes: Obtain the outlet water temperature of the deaerator at the current correction time point; The deoxygenation deviation value f is generated based on the outlet water temperature; A first deoxygenation deviation threshold F1 and a second deoxygenation deviation threshold F2 are preset, and F1 <F2; If f > F1, no correction instruction will be generated at the current correction time node; If F1 < f < F2, a first-level correction instruction is generated at the current correction time node; If f > F2, the unit operation data at the current correction time is obtained, and it is determined whether to generate a correction instruction based on the unit operation data.

[0045] Specifically, according to the deaeration deviation value of the difference between the real-time outlet water temperature of the deaerator (i.e., the temperature of the boiler feed water deaerated by the deaerator) and the expected outlet water temperature (i.e., the outlet water temperature corresponding to the optimal deaeration state of the deaerator), the greater the difference, the greater the corresponding deaeration deviation value, and the mapping relationship between the two can be set according to historical parameters.

[0046] Specifically, the first deaeration deviation value threshold and the second deaeration deviation value threshold can be set according to historical parameters. When the real-time deaeration deviation value is greater than the preset first deaeration deviation value threshold, it indicates that there is temperature fluctuation inside the current deaerator, and the operation parameters of the auxiliary unit need to be adjusted according to the first-level correction instruction.

[0047] Specifically, determining whether to generate a correction instruction based on the unit operation data includes: Generating the working condition fluctuation value k at the current correction time node k = (si - s'i) 2 ; where θ is the number of working condition characteristic indicators; si is the real-time reference value of the i-th working condition characteristic indicator at the current correction time node; s'i is the expected reference value of the i-th working condition characteristic indicator within the current deaeration cycle; Presetting the working condition fluctuation value threshold K1; If k < K1, a second-level correction instruction for the control sub-model is generated at the current correction time node; If k > K1, a switching correction instruction is generated at the current correction time node.

[0048] Specifically, the working condition characteristic indicators include but are not limited to: extraction steam flow for heating, condensate flow, feed pump speed, power generation coal consumption, and other parameters related to the steam turbine unit. By quantifying each working condition characteristic indicator, the reference values of each working condition characteristic indicator are within the same value range.

[0049] Specifically, the expected reference value refers to the reference value of each working condition characteristic indicator in the working condition mode corresponding to the execution control strategy set in the current deaeration cycle.

[0050] Specifically, the working condition fluctuation value threshold can be set according to historical parameters. When the real-time working condition fluctuation value is greater than the preset working condition fluctuation value threshold, the control sub-model within the current deaeration cycle needs to be updated according to the switching correction instruction.

[0051] Specifically, the secondary correction instruction optimizes and adjusts the control parameters within the current control sub-model.

[0052] It is understood that in the above embodiments, by adding an auxiliary unit (i.e. a heating device), a switching sub-strategy is executed when switching operating conditions, which quickly compensates for the temperature deviation caused by the switching of different operating conditions, achieves a smooth transition, avoids drastic fluctuations in temperature and pressure, and ensures the continuous and stable deoxygenation effect.

[0053] In another preferred embodiment of the optimized control method for a high-efficiency deoxygenation system based on any of the above preferred embodiments, this preferred embodiment provides a high-efficiency deoxygenation system, comprising: Deaerators are used to treat boiler feedwater; The temperature control structure includes: a main steam circuit, a temperature auxiliary bypass, and a temperature regulation circuit; The temperature control structure is connected to the deaerator; The temperature control structure is used to control the operating temperature of the deaerator; The monitoring unit is used to acquire unit operating data; The auxiliary unit is located inside the deaerator. The auxiliary unit is used to control the operating temperature of the deaerator according to the execution switching strategy and the first-level correction command. The central control unit is used to establish the operation and control model of the temperature control structure; The central control unit includes: The first processing module is used to preset multiple deoxygenation cycles; The first processing module is also used to set the control sub-model for each deoxygenation cycle based on the unit operation data and the operation control model; The second processing module is used to acquire monitoring data of the deaerator according to a preset correction time node; The second processing module is also used to determine whether to generate a correction instruction for the control sub-model based on the monitoring data.

[0054] Specifically, the auxiliary unit is preferably a heating device, which is installed inside the deaerator and is used to fine-tune the temperature inside the deaerator.

[0055] Specifically, the main steam line can receive main extraction steam or standby steam from the turbine unit (such as steam from the auxiliary steam header). The temperature auxiliary bypass is connected in parallel to the main heating steam line and includes a desuperheater, a fine-tuning steam valve, and shut-off valves before and after it. It is used to desuperheat the steam in the main steam line. The temperature control circuit draws a stream of hot water from the bottom of the deaerator tank and mixes it into the main condensate inlet pipe via a small pump and regulating valve.

[0056] In a preferred embodiment of this application, the central control unit further includes: The third processing module is used to set multiple operating modes based on the unit's historical operating data; Establish a sequence of working condition modes A, A=(a1, a2, ..., ai, ..., an), where ai is the i-th working condition mode; n is the number of working condition modes; Based on the working condition mode sequence A, ai is sequentially set as the target mode; The target mode is defined as the operating sub-model, which includes: control strategy and mode switching strategy; The operation sub-models for each working condition are set sequentially, and the operation control model is constructed based on all the operation sub-models; The sub-model for setting the target mode includes: Select the operating steam source; Set multiple steam source temperature ranges; Set the primary control parameters for each gas source temperature range; The primary control parameters include: the valve opening degree of the main steam line and the desuperheating parameters of the temperature auxiliary bypass; Set multiple inlet water temperature ranges; Set the secondary control parameters for each inlet water temperature range; Secondary control parameters include: the valve opening degree of the temperature auxiliary bypass and the circulating water volume of the temperature control loop; The control strategy for the target mode is set based on the primary control parameters and the secondary control parameters; Based on the working condition mode sequence A, ai is sequentially set as the evaluation mode; The duration of fluctuations when switching between the target mode and the evaluation mode; The evaluation mode is set according to the switching fluctuation duration to determine the switching sub-strategy for the target mode; Generate sub-strategies for switching between each operating mode and the target mode in sequence; Construct a mode switching strategy for the target mode based on all switching example strategies.

[0057] In a preferred embodiment of this application, the first processing module is further configured to: Acquire the unit operating data for the current deoxygenation cycle and generate the operating mode for the current deoxygenation cycle; Select the execution control strategy for the current deoxygenation cycle based on the operating mode; Obtain the historical operating mode of the previous deoxygenation cycle; The execution switching strategy for the current deoxygenation cycle is set based on historical operating patterns; Establish a corrected timeline for the current deoxygenation cycle, which includes multiple corrected time nodes; Construct a control sub-model for the current deoxygenation cycle. The control sub-model includes: correcting the time axis and executing the switching. According to the first concept of this application, by adding a temperature control structure and an operation control model, the operating temperature inside the deaerator is dynamically controlled by using a temperature-assisted bypass and a temperature adjustment loop, so as to ensure that the deaerator can quickly reach and maintain the optimal deoxygenation temperature under various operating conditions, thereby improving the deoxygenation efficiency of the deaerator for boiler feedwater and ensuring the efficient operation of the unit.

[0058] According to the second concept of this application, by adding an auxiliary unit (i.e. a heating device), a switching sub-strategy is executed when switching operating conditions, which quickly compensates for the temperature deviation caused by the switching of different operating conditions, achieves a smooth transition, avoids drastic fluctuations in temperature and pressure, and ensures the continuous and stable deoxygenation effect.

[0059] The above description is only a preferred embodiment of this application. It should be noted that for those skilled in the art, several improvements and substitutions can be made without departing from the technical principles of this application, and these improvements and substitutions should also be considered within the scope of protection of this application.

Claims

1. An optimized control method for a high-efficiency deoxygenation system, characterized in that, It includes: Establish an operation regulation model for the temperature control structure; Preset multiple deaeration cycles, and set the control sub-model for each deaeration cycle according to the unit operation data and the operation regulation model; Obtain the monitoring data of the deaerator according to the preset correction time node, and judge whether to generate a correction instruction for the control sub-model according to the monitoring data; Among them, the temperature control structure includes: a main steam path, a temperature auxiliary bypass, and a temperature regulation loop.

2. The optimized control method for the high-efficiency deoxygenation system as described in claim 1, characterized in that, The operation regulation model of the temperature control structure includes: Set multiple working condition modes according to the unit historical operation data; Establish a working condition mode sequence A, A=(a1, a2…ai…an), where ai is the i-th working condition mode; n is the number of working condition modes; Set ai as the target mode in sequence according to the working condition mode sequence A; Set the operation sub-model of the target mode, and the operation sub-model includes: a regulation strategy and a mode switching strategy; Set the operation sub-models of each working condition mode in sequence, and construct an operation regulation model according to all the operation sub-models.

3. The optimized control method for the high-efficiency deoxygenation system as described in claim 2, characterized in that, The operation sub-model of the set target mode includes: Select an operating steam source; Set multiple steam source temperature ranges; Set the primary control parameters for each steam source temperature range; The primary control parameters include: the valve opening of the main steam path and the desuperheating parameters of the temperature auxiliary bypass; Set multiple inlet water temperature ranges; Set the secondary control parameters for each inlet water temperature range; The secondary control parameters include: the valve opening of the temperature auxiliary bypass and the circulating water volume of the temperature regulation loop; Set the regulation strategy of the target mode according to the primary control parameters and the secondary control parameters.

4. The optimized control method for the high-efficiency deoxygenation system as described in claim 3, characterized in that, The operation sub-model of the set target mode further includes: Set ai as the evaluation mode in sequence according to the working condition mode sequence A; Generate the switching fluctuation duration between the target mode and the evaluation mode; Set the switching sub-strategy of the evaluation mode to the target mode according to the switching fluctuation duration; Generate the switching sub-strategies of each working condition mode to the target mode in sequence; Construct the mode switching strategy of the target mode according to all the switching sub-strategies.

5. The optimized control method for the high-efficiency deoxygenation system as described in claim 4, characterized in that, The setting of the control sub-model for each deaeration cycle includes: Obtain the unit operation data of the current deaeration cycle, and generate the operation mode of the current deaeration cycle; Select the regulation strategy to be executed in the current deaeration cycle according to the operation mode; Obtain the historical operation mode of the previous deaeration cycle; Set the execution switching strategy of the current deaeration cycle according to the historical operation mode; Establish the correction time axis of the current deaeration cycle, and the correction time axis includes multiple correction time nodes; Construct the control sub-model of the current deaeration cycle, and the control sub-model includes: the correction time axis, the execution switching strategy, and the execution regulation strategy.

6. The optimized control method for the high-efficiency deoxygenation system as described in claim 5, characterized in that, The judgment of whether to generate a correction instruction for the control sub-model includes: Obtain the outlet water temperature of the deaerator at the current correction time node; Generate a deaeration deviation value f according to the outlet water temperature; Preset a first deaeration deviation value threshold F1 and a second deaeration deviation value threshold F2, and F1 < F2; If f > F1, no correction instruction is generated at the current correction time node; If F1 < f < F2, a primary correction instruction is generated at the current correction time node; If f > F2, obtain the unit operation data at the current correction time, and judge whether to generate a correction instruction according to the unit operation data.

7. The optimized control method for the high-efficiency deoxygenation system as described in claim 6, characterized in that, Judging whether to generate a correction instruction according to the unit operation data includes: Generating the working condition fluctuation value k at the current correction time node k=[ (si-s'i) 2 ]; Where, θ is the number of working condition characteristic indexes; si is the real-time reference value of the i-th working condition characteristic index at the current correction time node; s'i is the expected reference value of the i-th working condition characteristic index within the current deaeration cycle; Presetting the working condition fluctuation value threshold K1; If k < K1, a secondary correction instruction for the control sub-model is generated at the current correction time node; If k > K1, a switching correction instruction is generated at the current correction time node.

8. A high-efficiency deoxygenation system, employing the optimized control method for the high-efficiency deoxygenation system described in any one of claims 1-7, characterized in that, Including: A deaerator for treating boiler feed water; A temperature control structure including a main steam path, a temperature auxiliary bypass, and a temperature regulation loop; The temperature control structure is connected to the deaerator; The temperature control structure is used to control the operating temperature of the deaerator; A monitoring unit for obtaining unit operation data; An auxiliary unit is arranged inside the deaerator, and the auxiliary unit is used to control the operating temperature of the deaerator according to the execution switching strategy and the primary correction instruction; A central control unit for establishing an operation regulation model of the temperature control structure; The central control unit includes: A first processing module for presetting multiple deaeration cycles; The first processing module is further used to set the control sub-model of each deaeration cycle according to the unit operation data and the operation regulation model; A second processing module for obtaining the monitoring data of the deaerator according to the preset correction time node; The second processing module is further used to judge whether to generate a correction instruction for the control sub-model according to the monitoring data.

9. The high-efficiency deoxygenation system as described in claim 8, characterized in that, The central control unit further includes: A third processing module for setting multiple working condition modes according to the unit historical operation data; Establishing a working condition mode sequence A, A = (a1, a2…ai…an), where ai is the i-th working condition mode; n is the number of working condition modes; Sequentially setting ai as the target mode according to the working condition mode sequence A; Setting the operation sub-model of the target mode, and the operation sub-model includes: a regulation strategy and a mode switching strategy; Sequentially setting the operation sub-models of each working condition mode, and constructing an operation regulation model according to all the operation sub-models; Among them, setting the operation sub-model of the target mode includes: Selecting an operating steam source; Setting multiple steam source temperature ranges; Setting the primary control parameters of each gas source temperature range; The primary control parameters include: the valve opening of the main steam path and the desuperheating parameter of the temperature auxiliary bypass; Setting multiple inlet water temperature ranges; Setting the secondary control parameters of each inlet water temperature range; The secondary control parameters include: the valve opening of the temperature auxiliary bypass and the circulating water volume of the temperature regulation loop; Setting the regulation strategy of the target mode according to the primary control parameters and the secondary control parameters; Sequentially setting ai as the evaluation mode according to the working condition mode sequence A; Generating the switching fluctuation duration between the target mode and the evaluation mode; Setting the switching sub-strategy of the evaluation mode to the target mode according to the switching fluctuation duration; Sequentially generating the switching sub-strategies of each working condition mode to the target mode; Constructing the mode switching strategy of the target mode according to all the switching sub-strategies.

10. The high-efficiency deoxygenation system as described in claim 9, characterized in that, The first processing module is further used for: Obtaining the unit operation data of the current deaeration cycle and generating the operation mode of the current deaeration cycle; Selecting the execution regulation strategy of the current deaeration cycle according to the operation mode Obtain the historical operating mode of the previous deoxygenation cycle; The execution switching strategy for the current deoxygenation cycle is set based on historical operating patterns; Establish a corrected time axis for the current deoxygenation cycle, which includes multiple corrected time nodes; Construct a control sub-model for the current deoxygenation cycle. The control sub-model includes: correcting the time axis, executing a switching strategy, and executing a regulation strategy.

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