Concrete pipe pile steam curing temperature control energy-saving device and method

Abstract

This invention relates to the field of concrete product manufacturing technology, and discloses a temperature control and energy-saving device and method for steam curing concrete pipe piles. The method includes: acquiring the temperature at multiple points in the steam curing tank, sensor coordinates, and real-time steam temperature; extracting spatial temperature penalty feature values ​​and calculating dynamic condensation heat exchange efficiency; dynamically identifying system thermal state parameters based on historical heat input and temperature response, and reconstructing the dynamic net heat demand power for the next stage by combining spatial penalty feature values, reference pipeline flow velocity shear rate, and target temperature; constructing a target cost function including an adaptive valve damping penalty term based on heat exchange efficiency and demand power, and optimizing the solution to obtain the optimal instantaneous steam flow increment; and superimposing this increment onto the current flow generation control signal to adjust the valve opening. This invention achieves refined and intelligent management, effectively solving the problems of uneven heating and cooling, serious energy waste, and large temperature fluctuations.

Description

Technical Field

[0001] This invention belongs to the field of concrete product manufacturing technology, and in particular relates to a temperature control and energy-saving device and method for steam curing concrete pipe piles. Background Technology

[0002] The production of concrete pipe piles typically involves key processes such as centrifugal molding and steam curing, with steam curing being the core step in stimulating early strength and shortening the demolding cycle. Currently, the commonly used steam curing temperature control system in the industry mainly consists of a main steam pipeline, pneumatic or electric regulating valves, and several temperature sensors arranged within the curing tank. In existing conventional control logic, the system mostly relies on a preset "time-temperature" stepped process standard curve (usually including four stages: static stop, heating, constant temperature, and cooling), combined with traditional single-input single-output PID algorithms or simple on-off logic for automatic adjustment. Specifically, the system mainly collects the average temperature of a representative point or a limited number of temperature measuring points within the curing tank as feedback, comparing it with the preset target temperature for the current stage: when the measured temperature is lower than the set value, the controller outputs a command to open the steam valve; when the temperature reaches or slightly exceeds the set value, the valve is closed or completely shut off.

[0003] However, the aforementioned existing technologies face numerous insurmountable challenges in practical large-scale industrial production applications. Firstly, pipe pile steam curing tanks are typically large in volume and filled with a large number of stacked pipe piles and steel molds, constituting a typical high-inertia, highly nonlinear thermodynamic system. Simply relying on local temperature feedback for valve opening and closing cannot address the three-dimensional heat gradient formed by steam diffusion within the complex geometric space, leading to severe uneven heating within the tank. Secondly, traditional temperature control methods treat the entire steam curing system as a simple passive heat receiver, failing to consider the dynamic evolution of the pipe pile's heat absorption capacity at different curing stages and the complex thermodynamic changes within the system. This crude "add steam when cold, cut off steam when hot" strategy often results in severe temperature overshoot and ineffective steam venting during the heating and isothermal phases. Simultaneously, the lack of feedforward physical compensation in flow regulation easily causes drastic local temperature fluctuations within the tank, resulting not only in significant energy consumption and waste but also inducing thermal stress microcracks on the pipe pile surface, making it difficult to guarantee the final product quality. Summary of the Invention

[0004] The purpose of this invention is to provide a temperature control and energy-saving device and method for steam curing concrete pipe piles, aiming to solve the above-mentioned problems.

[0005] This invention is implemented as follows: a method for energy-saving temperature control during steam curing of concrete pipe piles, comprising the following steps: Step S10: acquiring multi-point temperature data, sensor spatial coordinates, and real-time steam temperature within the steam curing tank; extracting spatial temperature penalty feature values ​​characterizing the degree of spatial unevenness; and calculating the dynamic condensation heat transfer efficiency; Step S20: dynamically identifying system thermal state parameters based on historical system heat input and temperature response; and reconstructing the dynamic net heat demand power for the next stage of the system by combining the spatial temperature penalty feature values, the reference pipeline flow velocity shear rate, and the target set temperature; Step S30: constructing a target cost function including an adaptive valve damping penalty term based on the dynamic condensation heat transfer efficiency and the dynamic net heat demand power; and obtaining the optimal instantaneous steam flow increment based on the optimization solution; Step S40: superimposing the optimal instantaneous steam flow increment onto the current actual instantaneous steam inlet flow to generate a control signal to adjust the steam valve opening.

[0006] A further technical solution, in step S10, the process of extracting the spatial temperature penalty feature value includes: calculating the temperature deviation feature between the actual temperature of each temperature measuring point and the average temperature of the steam incubation tank; constructing a distance attenuation weight function by combining the spatial distance from each temperature measuring point to the nearest effective steam injection hole, wherein the distance attenuation weight function monotonically decreases as the spatial distance increases; weighting and fusing the temperature deviation feature with the corresponding distance attenuation weight function to obtain the spatial temperature penalty feature value; the spatial temperature penalty feature value is positively correlated with the dispersion of the temperature deviation feature.

[0007] A further technical solution, in step S10, the process of calculating the dynamic condensation heat transfer efficiency includes: obtaining the maximum steam condensation efficiency of the system under ideal conditions as a benchmark value; establishing a heat conduction driving term based on the difference between the real-time steam temperature at the steam inlet and the average temperature of the steam curing tank; establishing a heat transfer attenuation resistance term based on the space temperature penalty characteristic value; and generating the dynamic condensation heat transfer efficiency by performing a nonlinear mapping based on the benchmark value, the heat conduction driving term, and the heat transfer attenuation resistance term; wherein the value of the dynamic condensation heat transfer efficiency is positively correlated with the heat conduction driving term and negatively correlated with the heat transfer attenuation resistance term.

[0008] In a further technical solution, in step S20, the system thermal state parameters include the system equivalent comprehensive specific heat capacity and the net hydration heat release power. The dynamic identification process includes: system equivalent comprehensive specific heat capacity identification: based on the energy conservation relationship between the accumulated effective heat input of steam within a set historical sliding time window and the actual temperature rise of the steam curing tank within that window, the system equivalent comprehensive specific heat capacity at the current moment is dynamically estimated; reverse calculation of net hydration heat release power: a system thermal state observer is constructed, and based on the currently calculated system equivalent comprehensive specific heat capacity and the actual temperature rise rate at the previous moment, the total sensible heat demand of the system is calculated; the effective condensation heat of steam actually input at the previous moment is removed from the total sensible heat demand, and the difference between the two is taken as the net hydration heat release power spontaneously released by the pipe pile hydration reaction.

[0009] A further technical solution, in step S20, the process of reconstructing the dynamic net heat demand power of the system in the next stage includes: calculating the basic sensible heat power requirement required for the system to follow the standard process curve based on the process target set temperature of the next control cycle, the equivalent total mass of the steam curing tank, and the identified equivalent comprehensive specific heat capacity of the system; subtracting the identified net hydration heat release power from the basic sensible heat power requirement to obtain the basic net heat demand; introducing the reference pipeline flow velocity shear rate characterizing the steam injection kinetic energy and the spatial temperature penalty characteristic value to construct a dynamic heat compensation term for smoothing local thermal gradients and fluid disturbance dissipation; and superimposing and fusing the basic net heat demand with the dynamic heat compensation term to reconstruct the dynamic net heat demand power of the system in the next stage.

[0010] In a further technical solution, step S30, the process of generating the adaptive valve damping penalty term includes: extracting the current spatial temperature penalty feature value and the average temperature of the steam curing tank as feature variables, and evaluating the spatial temperature non-uniformity in the tank; constructing a damping amplification mapping relationship with the spatial temperature non-uniformity as the independent variable, and combining it with the physical flow parameters of the steam pipeline network to generate the adaptive valve damping penalty term; the strength of the adaptive valve damping penalty term increases adaptively with the aggravation of the spatial temperature non-uniformity, and is used to limit the drastic changes in the steam valve opening when the temperature gradient is large.

[0011] In a further technical solution, step S30, the process of obtaining the optimal instantaneous steam flow increment, includes: constructing a target cost function with the instantaneous steam flow increment as the decision variable. The target cost function is composed of two related parts: the first part is a heat tracking deviation evaluation term, which is used to characterize the deviation level between the actual expected heating power and the dynamic net heat demand power; the second part is a control action damping evaluation term, which is composed of the instantaneous steam flow increment and the adaptive valve damping penalty term; the target cost function is solved using an extreme value optimization algorithm to find the optimal solution that makes the partial derivative or gradient of the target cost function approach zero, thereby outputting the optimal instantaneous steam flow increment that takes into account both the accuracy of heat demand tracking and the smoothness of valve action.

[0012] In a further technical solution, in step S40, the instantaneous flow rate of the steam inlet actually measured at the current moment is arithmetically superimposed with the incremental value of the optimal instantaneous steam flow rate obtained by solving, and sent to the steam valve as the target control signal to be executed at the next moment.

[0013] A temperature control and energy-saving device for steam curing concrete pipe piles includes: a feature extraction and efficiency calculation module, used to acquire multi-point temperature data, sensor spatial coordinates, and real-time steam temperature in the steam curing tank, extract spatial temperature penalty feature values ​​characterizing the degree of spatial unevenness, and calculate the dynamic condensation heat transfer efficiency; a state identification and demand reconstruction module, used to dynamically identify the system's thermal state parameters based on the system's historical heat input and temperature response, and reconstruct the dynamic net heat demand power for the next stage of the system by combining the spatial temperature penalty feature values, the reference pipeline flow velocity shear rate, and the target set temperature; a cost optimization and increment generation module, used to construct a target cost function including an adaptive valve damping penalty term based on the dynamic condensation heat transfer efficiency and the dynamic net heat demand power, and obtain the optimal instantaneous steam flow increment based on the optimization solution; and a control output and closed-loop execution module, used to superimpose the optimal instantaneous steam flow increment onto the current actual instantaneous steam inlet flow to generate a control signal to adjust the steam valve opening.

[0014] Compared with the prior art, the beneficial effects of the present invention are as follows:

[0015] 1. By extracting distance-weighted spatial temperature penalty feature values ​​and performing dynamic heat compensation, the "uneven heating and cooling" phenomenon commonly found in large-volume steam curing tanks is effectively eliminated, fundamentally reducing the risk of microcracks in pipe piles caused by uneven thermal stress.

[0016] 2. Real-time identification of the system's dynamic specific heat capacity and precise feedforward deduction of the hydration heat release of the pipe pile itself completely breaks the traditional "add steam when it gets cold" lag control logic, effectively avoiding temperature overshoot and ineffective steam venting caused by blind steam supply.

[0017] 3. Abandoning cumbersome iterative algorithms, the analytical solution for the optimal steam flow increment is directly obtained based on the Jacobian gradient of the objective cost function; combined with an adaptive damping mechanism, the system achieves extremely fast response while effectively suppressing drastic valve fluctuations and extending equipment service life. Attached Figure Description

[0018] Figure 1 The flowchart of a temperature control and energy-saving method for steam curing of concrete pipe piles provided by the present invention is shown. Detailed Implementation

[0019] To make the objectives, technical solutions, and advantages of this invention clearer, the invention will be further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative and not intended to limit the invention.

[0020] The specific implementation of the present invention will be described in detail below with reference to specific embodiments.

[0021] like Figure 1 As shown, an embodiment of the present invention provides a temperature control and energy-saving device and method for steam curing concrete pipe piles, comprising the following steps:

[0022] Step S10: Acquire multi-point temperature data (and perform smoothing filtering to eliminate measurement noise), sensor spatial coordinates, and real-time steam temperature within the steam curing tank. Extract the spatial temperature penalty feature value characterizing the degree of spatial distribution non-uniformity and calculate the dynamic condensation heat transfer efficiency. The steam curing tank is a closed space used for the steam curing of concrete pipe piles, filled with steam to provide the temperature and humidity environment required for the hydration of the pipe piles. This tank is typically large, containing a large number of concrete pipe piles and steel molds to be cured. Multi-point temperature data refers to the set of temperature measurements collected in real time by multiple temperature sensors arranged at different locations within the steam curing tank. This data reflects the temperature distribution in different areas within the steam curing tank. Sensor spatial coordinates refer to the specific location information of each temperature sensor in the three-dimensional space of the steam curing tank, usually recorded in a Cartesian coordinate system or other spatial positioning methods. These coordinates are the basis for analyzing the spatial distribution non-uniformity of temperature. The spatial temperature penalty feature value is an indicator that quantifies the degree of spatial distribution non-uniformity of temperature within the steam curing tank. This characteristic value is calculated by comprehensively considering factors such as the deviation of each temperature measuring point from the average temperature and the distance of the sensor from the steam injection hole, and is used to characterize the severity of uneven heating and cooling within the pool. Dynamic condensation heat transfer efficiency refers to the actual efficiency with which steam condenses in the steam curing pool and releases latent heat to the pipe piles and the surrounding environment. This efficiency is a dynamically changing parameter, affected by various factors such as real-time steam temperature, average temperature within the pool, and temperature non-uniformity.

[0023] Step S20: Based on the system's historical heat input and temperature response, dynamically identify the system's thermal state parameters. Combined with the spatial temperature penalty characteristic value, the reference pipe network velocity shear rate (used to characterize the turbulent mixing kinetic energy during steam injection), and the target set temperature, reconstruct the dynamic net heat demand power for the next stage of the system. System thermal state parameters refer to key physical quantities describing the current thermodynamic characteristics of the steam curing system, such as the system's equivalent comprehensive specific heat capacity and the net heat release power of the pipe pile hydration. These parameters reflect the system's ability to absorb and release heat and the dynamic changes of internal heat sources. The reference pipe network velocity shear rate refers to the magnitude of the shear force generated by the velocity gradient near the inner wall of the pipe when steam is injected into the steam curing tank. This parameter can indirectly characterize the intensity of the turbulent mixing kinetic energy generated when steam is injected into the tank, affecting the diffusion and heat exchange effect of steam within the tank. The dynamic net heat demand power refers to the net heat rate that the system needs to obtain from external steam input in order to achieve the target set temperature and maintain temperature uniformity in the steam curing tank during the next control cycle. This power is calculated comprehensively based on the current system state, target temperature, and various dynamic factors.

[0024] Step S30: Based on the dynamic condensation heat exchange efficiency and the dynamic net heat demand power, construct a target cost function including an adaptive valve damping penalty term, and obtain the optimal instantaneous steam flow increment based on the optimization solution. The adaptive valve damping penalty term is a component of the target cost function, and its function is to limit the instantaneous change in the steam valve opening adjustment. This penalty term can adaptively adjust its weight according to the current temperature non-uniformity and other states of the system to avoid drastic temperature fluctuations caused by over-adjustment. The target cost function is a mathematical expression used to quantify the "cost" or "deviation" of the control system in achieving the target. By optimizing this function, the control variables that optimize system performance can be found. The optimal instantaneous steam flow increment refers to the amount of steam flow that needs to be increased or decreased based on the current actual instantaneous steam inlet flow rate at the current moment in order to achieve the optimal temperature control of the steam curing tank. This increment is the result of the optimization solution and is directly used to adjust the steam valve.

[0025] Step S40: The optimal instantaneous steam flow rate increment is superimposed on the current actual instantaneous steam inlet flow rate to generate a control signal to adjust the steam valve opening.

[0026] This embodiment introduces a highly integrated and adaptive temperature control and energy-saving method by quantifying spatial temperature distribution, dynamically identifying the system's thermal state, considering steam mixing efficiency, and optimizing control strategies. This method effectively solves the core technical problems in traditional steam curing temperature control of concrete pipe piles, such as uneven heating and cooling, energy waste, and unstable product quality. It achieves refined and intelligent management of the steam curing process, demonstrating significant technological advancement.

[0027] This application further proposes step S10, in which the process of extracting the spatial temperature penalty feature value includes: calculating the temperature deviation feature between the actual temperature of each temperature measuring point and the average temperature of the septic tank; constructing a distance attenuation weight function based on the spatial distance from each temperature measuring point to the nearest effective steam injection hole, wherein the distance attenuation weight function monotonically decreases with the increase of spatial distance; performing weighted fusion calculation on the temperature deviation feature and the corresponding distance attenuation weight function to aggregate and obtain the spatial temperature penalty feature value; the spatial temperature penalty feature value is positively correlated with the dispersion of the temperature deviation feature; the formula for calculating the spatial temperature penalty feature value is as follows:

[0028]

[0029] in, The spatial temperature penalty characteristic value at the current time t; This represents the total number of temperature sensors. This is the serial number index of the temperature sensor; Let be the real-time multi-point temperature collected by the i-th sensor at the current time t; This is the arithmetic mean of the temperatures of all sensors in the steam curing tank at the current time t; Let be the straight-line distance between the i-th sensor and the nearest effective steam injection orifice; This represents the diagonal length of the maximum spatial characteristic of the steam curing tank. This scheme introduces distance-weighted correction for temperature deviations within the steam curing tank, obtaining a characteristic value that accurately reflects the actual temperature non-uniformity within the tank. This provides accurate and reliable input for subsequent temperature control calculations, solving the problem of inaccurate non-uniformity calculations in the original method. Spatial temperature penalty characteristic value. It is a comprehensive quantitative indicator used to characterize the non-uniformity of temperature distribution within a steam curing tank. It not only considers the dispersion of temperature data but also assigns different weights to temperature deviations in different areas by incorporating spatial location information, thus more accurately reflecting the actual temperature distribution. Its function is to provide a precise and physically meaningful input parameter for subsequent calculations of dynamic condensation heat transfer efficiency and dynamic net heat demand power reconstruction. Total number of temperature sensors. This refers to the total number of sensors actually installed inside the steam curing tank for collecting temperature data. This number can be flexibly configured based on the size and structural complexity of the steam curing tank, as well as the required temperature monitoring accuracy. For example, depending on the tank size and pipe pile stacking density, multiple sensors can be evenly distributed within the tank, or densely distributed in key areas. Temperature sensor serial number index. This is used to uniquely identify each temperature sensor within the steam curing tank. By assigning a unique serial number to each sensor, the system can distinguish, manage, and process the temperature data collected by each sensor, ensuring accurate referencing and processing of each sensor's independent data during calculations. Real-time multi-point temperature. This refers to the temperature value collected in real time by the i-th temperature sensor at the current time t. These sensors are typically thermocouples, resistance temperature detectors (RTDs), or semiconductor temperature sensors, which are placed at different locations within the steam curing tank to obtain temperature information at various points within the tank. To improve data reliability, this raw temperature data is usually filtered by the underlying hardware, such as using RC filters or digital low-pass filters, to eliminate high-frequency noise and transient interference. Arithmetic mean This refers to the arithmetic mean of the real-time multi-point temperatures collected by all temperature sensors within the steam incubator at the current time t. This average represents the overall temperature level of the steam incubator at that moment and serves as a fundamental reference for measuring the temperature change trend within the incubator. It is calculated by summing the temperature values ​​from all sensors and then dividing by the total number of sensors. (Linear distance) This refers to the linear spatial distance between the i-th temperature sensor and its nearest effective steam injection orifice. This distance is a key parameter for measuring the relative proximity of the sensor location to the steam heat source. It is typically obtained during the design or installation phase of the steam curing tank by measuring the precise three-dimensional coordinates of the sensor and the steam pipe injection orifice, and then calculating the Euclidean distance between them. Maximum spatial characteristic diagonal length. This refers to the maximum diagonal length of the septic tank in three-dimensional space. This parameter is used to measure distance. The weighting term is normalized to a dimensionless relative distance. By using the maximum characteristic size of the steam incubator as a reference, the model's generalization ability can be improved by ensuring that the weighting term has consistent physical meaning and applicability across steam incubators of different sizes.

[0030] The scheme first acquires multi-point temperature data, sensor spatial coordinates, and real-time steam temperature within the steam curing tank. Then, it calculates the spatial temperature penalty characteristic value. At the same time, it not only considers the real-time multi-point temperature collected by various sensors. The arithmetic mean of the temperatures of all sensors in the steam curing tank The squared deviation between them also introduces an exponential weighting term. The core of this weighting term is that it measures the straight-line distance of each sensor from the nearest effective steam injection orifice. Taking into account, and utilizing the maximum spatial characteristic of the steam incubation tank, the diagonal length... Normalization is performed. Because steam diffusion within the steam-curing tank is attenuated, the further away from the steam injection hole, the less the temperature is directly affected by the steam. Therefore, any temperature deviation further indicates severe temperature unevenness within the tank. Thus, using an exponential function, the farther the sensor is, the greater its contribution to the overall unevenness of the temperature deviation, resulting in a higher weighting for the calculated spatial temperature penalty characteristic value. This allows for more precise quantification of the actual temperature unevenness within the steam curing tank, closely aligning with real-world heat transfer patterns. This distance-weighted correction for spatial temperature penalty characteristic value... This weighted characteristic value, as a key output in step S10, is subsequently used to calculate the dynamic condensation heat transfer efficiency. Compared to methods relying solely on simple temperature dispersion, this weighted characteristic value more accurately reflects the actual heat distribution within the pool, thus making the calculation of the dynamic condensation heat transfer efficiency more precise. Furthermore, in step S20, based on a more accurate spatial temperature penalty characteristic value... The system can more accurately reconstruct the dynamic net heat demand power for the next stage. This precise demand power calculation avoids the problem of excessive or insufficient steam caused by inaccurate assessment of temperature non-uniformity in traditional methods, providing a solid foundation for constructing the objective cost function and solving for the optimal instantaneous steam flow increment in subsequent step S30. Finally, in step S40, the control signal generated based on these precise calculation results can more effectively adjust the steam valve opening, achieving refined control of the steam curing tank temperature, thereby significantly improving the accuracy of temperature control and energy-saving effect, ensuring uniform heating of the pipe piles, and guaranteeing product quality.

[0031] As a specific implementation method, a rectangular concrete pipe pile steam curing tank can be considered, with a length, width, and height of L, W, and H, respectively. Multiple steam injection holes are evenly arranged along the steam pipes inside the steam curing tank, and a total of [number missing] steam injection holes are installed at different heights and depths within the tank. Each temperature sensor needs to be calibrated during the system initialization phase, and its precise three-dimensional coordinates within the steam incubator need to be recorded. At the same time, it is also necessary to record the precise three-dimensional coordinates of all steam injection holes. For each sensor i, calculate its straight-line distance to all steam injection orifices j. Then take the minimum value as ,Right now The maximum spatial characteristic of the septic tank is its diagonal length. It can be calculated from the geometric dimensions of the pool, for example. These parameters are configured once before the system starts operating. At the beginning of each control cycle of the steam curing process (current time t), the control system acquires real-time multi-point temperature data from $n$ temperature sensors through the data acquisition module. , ,..., These raw data undergo filtering processing by the underlying hardware. For example, if a thermocouple sensor is used, its signal may be pre-processed through a signal conditioning circuit with a low-pass filter to remove power frequency interference and random noise. Next, the arithmetic mean of these real-time temperature data is calculated. Then, for each sensor i, the squared deviation of its temperature from the average temperature is calculated. At the same time, using a predetermined and Calculate the index weighting term Finally, the squared temperature deviation of each sensor is multiplied by its corresponding exponential weighting term, and all products are summed. This sum is then divided by... (For unbiased estimation), finally take the square root to obtain the spatial temperature penalty characteristic value at the current time t. For example, if there are 10 sensors in the steam curing tank, the system will collect 10 temperature values, calculate their average, then calculate the deviation of each temperature value from the average, and weight them according to their distance from the nearest spray nozzle, ultimately obtaining a single... Value. This. The value is then passed to subsequent calculation modules for calculating the dynamic condensation heat transfer efficiency.

[0032] Through the above technical solution, this application can more accurately quantify the actual temperature non-uniformity within the steam curing tank. By introducing an exponential weighting term based on the distance between the sensor and the steam jet orifice, this scheme can better reflect the actual heat transfer patterns within the steam curing tank. This means that areas farther from the steam jet orifice and with greater temperature deviations contribute more significantly to the overall non-uniformity, thus avoiding the problem of traditional methods that underestimate the impact of temperature deviations at distant locations by relying solely on temperature dispersion. This precise spatial temperature penalty characteristic value... As input for subsequent dynamic condensation heat transfer efficiency calculations, system thermal state parameter identification, and dynamic net heat demand power reconstruction, this significantly improves the sensing accuracy and predictive capability of the entire temperature control system. Therefore, the system can make decisions based on more accurate temperature distribution information, effectively avoiding excessive or insufficient steam injection, reducing energy waste, and ensuring uniform heating of the concrete pipe piles during steam curing. This improves the curing quality of the pipe piles and reduces the risk of microcracks caused by uneven thermal stress.

[0033] This application further proposes that step S10, calculating the dynamic condensation heat transfer efficiency, includes: obtaining the maximum steam condensation efficiency of the system under ideal conditions as a benchmark value; establishing a heat conduction driving term based on the difference between the real-time steam temperature at the steam inlet and the average temperature of the steam curing tank; establishing a heat transfer attenuation resistance term based on the space temperature penalty characteristic value; and generating the dynamic condensation heat transfer efficiency by performing a nonlinear mapping based on the benchmark value, the heat conduction driving term, and the heat transfer attenuation resistance term; wherein the value of the dynamic condensation heat transfer efficiency is positively correlated with the heat conduction driving term and negatively correlated with the heat transfer attenuation resistance term; the specific formula for calculating the dynamic condensation heat transfer efficiency is as follows:

[0034]

[0035] in, The dynamic condensation heat transfer efficiency at the current time t; This is the baseline value for the maximum steam condensation efficiency of the system under ideal conditions; This represents the real-time steam temperature measured at the steam inlet at the current time t. This is the arithmetic mean of the temperatures of all sensors in the steam curing tank at the current time t; The spatial temperature penalty characteristic value at the current time t; To prevent the use of tiny regularization constants with a denominator of zero, this scheme considers the dynamic condensation heat transfer efficiency. This represents the actual efficiency at which steam condenses and releases heat to the pipe piles and the environment within the steam curing tank at the current time t. It is a dynamically changing parameter reflecting the complexity and uncertainty of the thermodynamic state within the steam curing tank. As a key input for subsequent heat demand calculations and steam flow regulation, its accuracy directly affects the precision of temperature control and energy utilization efficiency. It is obtained through real-time calculation using the formula proposed in this application. Maximum steam condensation efficiency benchmark value. This refers to the theoretical maximum condensing heat transfer efficiency of a system under ideal operating conditions, i.e., when the heat exchange conditions between steam and the heated medium are optimal, without any loss or interference. This is an inherent physical parameter of the system, usually obtained through experimental calibration or theoretical calculation. It serves as the upper limit and benchmark for dynamic condensing heat transfer efficiency calculations, ensuring the calculation results are physically reasonable and providing a stable reference point for dynamic adjustments. This benchmark value can be determined by conducting precise heat balance experiments on a small-scale steam curing system under ideal heat exchange conditions, measuring the ratio of the heat released by steam condensation to the theoretical maximum heat release; or by statistically analyzing historical data from actual steam curing tanks under stable operation, uniform temperature, and sufficient steam supply, taking the peak or average peak value of the condensing efficiency as the benchmark value. Real-time steam temperature. The temperature of the steam entering the steam curing tank at the inlet of the main steam pipe at the current time t reflects the thermodynamic state of the steam source and is a key parameter for calculating the temperature difference between the steam and the tank environment, directly affecting the heat exchange driving force. This temperature can be obtained by installing a high-precision platinum resistance temperature sensor or thermocouple at the inlet of the main steam pipe to collect steam temperature data in real time and transmitting it to the controller via a data acquisition system; alternatively, an infrared temperature sensor can be used to perform non-contact measurement on the outer wall of the steam pipe, and corrections can be made based on the pipe material and steam flow rate to estimate the internal steam temperature. The arithmetic mean of the temperatures from all sensors within the steam curing tank is also considered. The average temperature value refers to the arithmetic mean of the temperature data collected by all temperature sensors arranged within the steam curing tank at the current time t. It represents the overall average temperature level of the steam curing tank and serves as an indicator of the overall thermal state. Together with the real-time steam temperature, it constitutes the heat transfer temperature difference and participates in the calculation of the spatial temperature penalty characteristic value. This average value can be obtained by having multiple temperature sensors arranged inside the steam curing tank collect temperature data at various points in real time, then summing these data and dividing by the number of sensors by the control system. Alternatively, a distributed fiber optic temperature sensor system can be used, with fibers continuously arranged along the inside of the steam curing tank to continuously monitor the temperature field. The average temperature inside the tank is then obtained by integrating and averaging the temperature data on the fibers using an algorithm. Spatial temperature penalty characteristic value. This refers to a quantitative index characterizing the degree of non-uniformity of temperature spatial distribution within the steam curing tank at the current time t. A larger value indicates a more uneven temperature distribution within the tank. It is used to correct for condensation heat transfer efficiency, enabling it to reflect the reduction in actual heat transfer effect caused by temperature non-uniformity. It is calculated according to the methods described in some embodiments of this application. Small regularization constant. This is a preset, very small positive value used to prevent the denominator from being zero in mathematical calculations, thereby avoiding calculation errors or system crashes, ensuring the formula runs stably under any operating conditions, and improving the robustness of the algorithm. This constant can be set to an extremely small positive floating-point number during system initialization and hard-coded into the control algorithm; alternatively, it can be dynamically adjusted by the system through adaptive adjustment based on actual operating data and numerical stability requirements.

[0036] This application aims to address the problem that traditional temperature control methods, with their fixed condensation heat transfer efficiency, cannot adapt to the complex dynamic thermodynamic changes within the steam curing tank. By introducing the calculation of dynamic condensation heat transfer efficiency, the system can more accurately assess the actual heat transfer capacity of the steam. The core of this solution lies in using the maximum steam condensation efficiency benchmark value under ideal conditions. As a foundation, it is dynamically corrected based on real-time operating conditions. Specifically, the calculation process considers the actual heat transfer driving force between the steam and the pool environment, i.e., the real-time steam temperature. The arithmetic mean of the temperatures of all sensors in the steam curing tank The temperature difference between them. The greater the temperature difference, the stronger the heat transfer driving force, and theoretically the higher the condensation heat transfer efficiency. Furthermore, this scheme creatively introduces a space temperature penalty characteristic value. This characteristic value quantifies the degree of temperature non-uniformity within the steam curing tank through the analysis of multi-point temperature data. In the formula for calculating condensation heat transfer efficiency, the spatial temperature penalty characteristic value... As part of the denominator, the larger its value (i.e., the more uneven the temperature), the smaller the absolute value of the negative part of the exponent, leading to... The smaller the value of the term, the lower the dynamic condensation heat transfer efficiency. The efficiency decreases accordingly. This accurately reflects that even with a large temperature difference between the steam and the average pool temperature, the actual effective heat transfer efficiency will be affected by the presence of local cold or hot zones when the temperature distribution is uneven. This correction mechanism allows the calculated condensation heat transfer efficiency to more realistically reflect the complex heat transfer process within the steam curing tank, avoiding the biases introduced by traditional fixed efficiency models. Furthermore, a small regularization constant is introduced. This ensures the numerical stability of the calculation process, preventing calculation interruption due to a zero denominator in extreme cases. Through the above dynamic calculation, this scheme can provide a real-time, accurate, and physically meaningful condensation heat transfer efficiency parameter for subsequent heat demand calculations and steam flow regulation. This is related to obtaining multi-point temperature data and calculating the spatial temperature penalty characteristic value. and average temperature These steps are closely integrated to form a complete and adaptive temperature control strategy. Space temperature penalty eigenvalues The introduction of this technology allows the system to focus not only on the average temperature but also on the uniformity of the temperature field. This enables the system to take into account the impact of spatial non-uniformity on the heat transfer effect when calculating the condensation heat transfer efficiency, significantly improving the intelligence level and energy-saving effect of the entire temperature control system.

[0037] As a specific implementation method, during the steam curing process of concrete pipe piles, multiple temperature sensors evenly distributed within the curing tank—for example, thermal resistors installed on the tank walls, bottom, top, and at different heights of the pipe pile stacks—can be used to collect temperature data at various points within the tank in real time. This data, after being filtered by the underlying hardware, is then arithmetically averaged by the control system to obtain the average temperature of the curing tank at the current moment. Simultaneously, utilizing these multi-point temperature data and the relative position information of each sensor and the steam injection orifice, and according to the methods described in some embodiments of this application above, the spatial temperature penalty characteristic value at the current moment is calculated. A high-precision industrial-grade thermocouple, such as a type K thermocouple, can be installed at the inlet of the main steam pipe to measure the temperature of the steam entering the steam curing tank in real time. During the initial design phase, thermodynamic analysis and experimental calibration of the steam curing tank were conducted to determine a benchmark value for the maximum steam condensation efficiency achievable under ideal heat exchange conditions. For example, it can be set to 0.95. To ensure the stability of the calculation, a very small positive number can be preset as the regularization constant. ,For example In each control cycle, the control system acquires the above parameters in real time: , , and combined with preset and Substitute into the formula The dynamic condensation heat transfer efficiency at the current moment is calculated. For example, when the temperature distribution in the steam incubator is relatively uniform ( When the temperature difference between the steam temperature and the average temperature inside the pool is relatively large (smaller), the calculated value is... Approaching ; and when the unevenness of temperature distribution within the pool increases ( When the temperature difference between the steam and the average temperature inside the pool decreases (increases), the calculated value is... This will decrease accordingly to reflect the decline in actual heat exchange efficiency. This dynamically calculated efficiency value is then passed to subsequent modules for accurate calculation of heat demand and adjustment of steam flow.

[0038] Through the above technical solution, this application effectively solves the problem that the fixed condensation heat exchange efficiency in traditional temperature control methods cannot match the dynamic changes in the actual heat exchange state within a large-volume steam curing tank. This solution dynamically calculates the condensation heat exchange efficiency, enabling subsequent heat demand calculations and steam flow adjustments to more accurately reflect the real-time operating conditions of the steam curing tank. Specifically, by introducing the temperature difference between the real-time steam temperature and the average temperature within the tank, the calculation of heat exchange efficiency can fully consider the actual heat exchange driving force, ensuring the accuracy of efficiency assessment when steam supply and tank temperature conditions change. More importantly, by incorporating a spatial temperature penalty characteristic value that characterizes the degree of unevenness in spatial temperature distribution, the calculated condensation heat exchange efficiency can adaptively reflect the impact of uneven temperature distribution within the tank on the actual heat exchange effect. When the temperature distribution within the tank is uneven, the system can identify and accordingly lower the expected heat exchange efficiency, thereby avoiding excessive steam injection and energy waste due to overestimation of efficiency. Conversely, when the temperature within the tank is uniform and heat exchange conditions are good, the system can fully utilize the heat exchange potential of the steam. This dynamic and adaptive efficiency evaluation mechanism significantly improves the accuracy and response speed of the temperature control system, effectively avoiding temperature overshoot and ineffective steam venting. This ensures the quality of steam curing of concrete pipe piles while achieving significant energy savings and reducing production costs. Simultaneously, the introduction of a small regularization constant ensures the numerical stability of the calculation process, improving the system's robustness and reliability.

[0039] Traditional methods for controlling the temperature of concrete pipe piles during steam curing fail to adequately consider the dynamic changes in the thermal properties of the curing system. This leads to the use of fixed parameters when calculating heat demand, resulting in deviations in steam flow regulation, ineffective improvement of uneven temperature within the curing tank, and energy waste. To address this, this application further proposes that step S20 includes system thermal state parameters such as the system's equivalent comprehensive specific heat capacity and net hydration heat release power. The system's equivalent comprehensive specific heat capacity characterizes the amount of heat absorbed by all materials in the curing tank to increase the temperature by one degree per unit mass. Because factors such as the water content of the pipe pile, the degree of concrete curing, and the density of steam in the tank dynamically change during steam curing, the overall heat storage capacity of the system is not constant. Accurately obtaining this parameter is crucial for accurately calculating the system's heat demand. This parameter can be identified online and updated in real time based on actual heat input and temperature response; or a baseline value can be calibrated under different operating conditions through offline experiments and then corrected using online data. The net hydration heat release power quantifies the contribution of the heat generated by the concrete itself during the hydration reaction to the temperature of the curing tank. The hydration reaction of concrete is an exothermic process, and its rate of heat release is affected by various factors such as temperature, humidity, cement type, and curing time. This exothermic effect is most pronounced in the early stages of curing and gradually diminishes in the later stages. Accurately assessing the net power of hydration heat release can prevent the system from over-supplying external steam due to a lack of consideration for internal heat sources, thus achieving energy savings. This parameter can be calculated backwards from the system's energy balance using a state observer; or it can be estimated using a pre-set hydration heat release model combined with real-time temperature data.

[0040] To accurately obtain these dynamically changing parameters, this application employs a two-pronged strategy. First, the equivalent comprehensive specific heat capacity of the system is dynamically identified online using the energy conservation equation over a historical time window. This method utilizes the actual steam heat input received by the septic tank over a past period (derived from the historical instantaneous steam inlet flow rate). Enthalpy difference of steam and dynamic condensation heat transfer efficiency (Jointly determined) and the resulting change in the system's average temperature. This is achieved by incorporating the historical total heat input with the total mass of the system. By relating it to temperature change, the energy conservation equation can be solved in reverse to calculate the system's equivalent comprehensive specific heat capacity at the current time t. This online identification method, based on actual operating data and the principle of energy balance, enables the system's equivalent comprehensive specific heat capacity to reflect in real time the dynamic evolution of the thermodynamic properties of components such as pipe piles, steel molds, and water vapor in the steam curing tank, such as the increase in the degree of concrete hydration and changes in water content, thereby avoiding the deviations caused by using fixed parameters.

[0041] Secondly, the net power of hydration heat release is calculated in reverse using a state observer. This is based on the system's equivalent comprehensive specific heat capacity at the current time t. Based on this, the state observer utilizes the system's average temperature change at adjacent time points and the previous time point Actual input steam heat and corresponding dynamic condensation heat transfer efficiency An energy balance equation is constructed. This equation allows for the precise extraction of the heat contribution from external steam input from the total energy change, enabling the reverse calculation of the net heat generated by the concrete hydration reaction itself. This method accurately quantifies the dynamic changes in the internal heat sources of concrete, avoiding energy waste and temperature overshoot caused by excessive external steam supply during the peak hydration heat release period.

[0042] The dynamic identification process includes: identification of the system's equivalent comprehensive specific heat capacity: based on the energy conservation relationship between the accumulated net effective heat input of steam within a set historical sliding time window and the actual temperature rise of the steam curing tank during that window, the system's equivalent comprehensive specific heat capacity at the current moment is dynamically estimated; reverse calculation of the net power of hydration heat release: a system thermal state observer is constructed, and based on the currently calculated system's equivalent comprehensive specific heat capacity and the actual temperature rise rate at the previous moment, the total sensible heat demand of the system is calculated; the effective condensation heat of steam actually input at the previous moment is removed from the total sensible heat demand, and the difference between the two is taken as the net power of hydration heat release spontaneously released by the pipe pile hydration reaction; the formula for dynamically identifying the system's equivalent comprehensive specific heat capacity online through the energy conservation equation of the historical time window is as follows:

[0043]

[0044] The formula for inversely calculating the net power of hydration heat release using a state observer is as follows:

[0045]

[0046] in, The equivalent comprehensive specific heat capacity of the system at the current time t is obtained by inverse calculation through the temperature rise response of the historical time window; This represents the total number of sampling periods within the sliding time window; A step index for historical time series; For a historic moment The actual instantaneous flow rate of steam at the inlet; Enthalpy of superheated or saturated vapor; The specific enthalpy of the discharged condensate; For a historic moment Dynamic condensation heat transfer efficiency; This refers to the time sampling step size of the control system. The equivalent total mass within the steam curing tank; This is the arithmetic mean of the temperatures of all sensors in the steam curing tank at the current time t; The arithmetic mean of the temperatures of all sensors in the steam curing tank at the starting point of the historical time window; The net power of heat release from hydration at the current time t; For the previous moment The arithmetic mean of the temperatures of all sensors in the steam curing tank; For the previous moment The actual measured instantaneous flow rate at the steam inlet; For the previous moment Dynamic condensation heat exchange efficiency.

[0047] Through the aforementioned dynamic online identification and reverse calculation, this application can obtain two key thermal state parameters—the system's equivalent comprehensive specific heat capacity and the net power of hydration heat release—in real time and accurately during the steam curing process. The dynamic updating of these parameters provides accurate and realistic basic data for reconstructing the dynamic net heat demand power of the system in the next stage in subsequent step S20.

[0048] As a specific implementation method, during the steam curing process of concrete pipe piles, the following approach can be used to achieve dynamic online identification and inverse calculation of the system's thermal state parameters. For the system's equivalent comprehensive specific heat capacity... The dynamic online identification can set a sliding time window W, for example, 10 control cycles, with a time sampling step size for each control cycle. The duration is 30 seconds. At the end of each control cycle, the system collects data from the past 10 cycles (i.e., from...). arrive Instantaneous flow rate of steam inlet and dynamic condensation heat transfer efficiency Simultaneously, obtain the arithmetic mean of the temperatures of all sensors in the steam curing tank at the current time t. and the starting point of the historical time window arithmetic mean Enthalpy of superheated or saturated vapor Enthalpy of the discharged condensate The equivalent total mass in the steam curing tank can be obtained by consulting a table or by real-time calculation based on steam pressure and temperature. The equivalent specific heat capacity of the system at time t can be obtained by pre-weighing or estimating the total mass of the pipe piles, steel formwork, and pool structure. Substituting this data into the energy conservation equation, the equivalent comprehensive specific heat capacity of the system at the current time t can be calculated. For example, in practice, the calculation of the above formula can be performed using the built-in mathematical operation module of the industrial controller or an external computing unit. Secondly, regarding the net power of hydration heat release... The inverse solution is used to obtain the system's equivalent comprehensive specific heat capacity at the current time t. Then, calculations can be performed using a state observer. Specifically, the system will obtain the arithmetic mean of the temperatures of all sensors in the steam curing tank at the current time t. and the previous moment arithmetic mean At the same time, obtain the previous time step. Actual measured instantaneous flow rate at the steam inlet and the corresponding dynamic condensation heat transfer efficiency These parameters, along with the known ones... , , and Substituting the formula for the net heat release power of hydration into the inverse calculation formula, we can obtain the net heat release power of hydration at the current time t. For example, the state observer could be a software module based on a discrete-time model, running on the control system's processor, receiving sensor data and identified parameters in real time, and outputting an estimate of the net power released by hydration heat. In this way, the system can continuously and adaptively update its thermal state parameters, providing an accurate physical basis for subsequent control decisions.

[0049] Through the above technical solution, this application enables accurate dynamic online identification of the system's thermal state parameters during the steam curing process of concrete pipe piles. Specifically, by dynamically identifying the equivalent comprehensive specific heat capacity of the system, the system can capture the dynamic changes in the overall heat storage capacity within the steam curing tank in real time. For example, as the degree of concrete hydration deepens, its specific heat capacity may change slightly, or the effective mass may change due to water evaporation within the tank, thus making the heat demand calculation more realistic. Simultaneously, by inversely calculating the net power of hydration heat release through a state observer, the system can accurately quantify the heat contribution generated by the concrete's own hydration reaction, avoiding excessive external steam supply during the peak hydration heat release period due to the lack of consideration for internal heat sources. Compared to traditional methods relying solely on fixed parameters, the solution in this application significantly improves the system's understanding and response capability to the complex thermodynamic processes within the steam curing tank. Because the system's thermal state parameters can accurately reflect the current operating conditions in real time, the subsequent dynamic net heat demand power reconstructed based on these parameters will be more precise, thereby guiding more accurate steam flow regulation. This not only helps to effectively improve the "uneven heating and cooling" phenomenon that is common in steam curing tanks and ensure the quality of pipe pile maintenance, but also significantly reduces energy consumption by avoiding unnecessary steam supply, thus achieving the goal of energy saving.

[0050] Traditional methods for controlling the temperature of steam curing concrete pipe piles do not fully integrate the dynamically identified system thermal state parameters when calculating net heat demand. They also do not consider the impact of concrete hydration self-heating, the degree of temperature non-uniformity in the steam curing tank, and the kinetic energy of steam injection turbulence on the actual heat demand. This results in a large deviation in the calculated net heat demand, which can easily lead to excessive steam input causing energy waste and temperature overshoot, or insufficient steam input causing substandard temperature and uneven heating. Consequently, these methods cannot simultaneously meet the requirements of energy conservation and consumption reduction while ensuring the quality of pipe pile steam curing.

[0051] To address this, this application further proposes that step S20, which involves reconstructing the dynamic net heat demand power for the next stage of the system, includes: calculating the basic sensible heat power requirement required for the system to follow the standard process curve based on the process target set temperature for the next control cycle, the equivalent total mass of the steam curing tank, and the identified equivalent comprehensive specific heat capacity of the system; subtracting the identified net hydration heat release power from the basic sensible heat power requirement to obtain the basic net heat demand; introducing the reference pipeline flow velocity shear rate characterizing the steam injection kinetic energy and the spatial temperature penalty characteristic value to construct a dynamic heat compensation term for mitigating local thermal gradients and fluid disturbance dissipation; and superimposing and fusing the basic net heat demand with the dynamic heat compensation term to reconstruct the dynamic net heat demand power for the next stage of the system. The formula for reconstructing the dynamic net heat demand power for the next stage of the system is as follows:

[0052]

[0053] in, The dynamic net heat demand power for the next stage of the reconstructed system; The equivalent total mass within the steam curing tank; The equivalent overall specific heat capacity of the system; Set the target temperature for the process at the end of the next control cycle; The arithmetic mean temperature at the current time t; This refers to the time sampling step size of the control system. Net power generated by heat release during hydration; For reference, the shear rate of the pipeline flow velocity; This is the conversion factor for the geometric cross-sectional area of ​​the pipeline network; Enthalpy of superheated or saturated vapor; The specific enthalpy of the discharged condensate; The spatial temperature penalty characteristic value at the current time t. The reconstructed dynamic net heat demand power for the system in the next stage. This represents the net heat power that the system needs to obtain from the outside at the current time t in order for the steam curing tank to reach the target set temperature at the end of the next control cycle. This power is a key input parameter for subsequent calculations of the optimal instantaneous steam flow rate increment. The equivalent total mass within the steam curing tank... This represents the total mass equivalent of all heated media (including pipe piles, steel molds, steam, condensate, etc.) in the steam curing tank in thermodynamic calculations, and can usually be set in advance by measurement or based on empirical parameters. The system's equivalent comprehensive specific heat capacity. This parameter reflects the amount of heat absorbed or released by the steam curing system per unit mass and per unit temperature change. Acquired through a dynamic online identification method, this parameter more accurately characterizes the thermodynamic properties of the system at different curing stages, thus providing dynamic and precise heat capacity information for calculating net heat demand. The target setpoint temperature at the end of the next control cycle. It is determined based on a preset steam curing process curve or real-time optimization strategy, and represents the target temperature that the system expects to achieve at the end of the next control cycle. The arithmetic mean temperature at current time t. This data, obtained by averaging data collected from multiple temperature sensors within the steam curing tank, reflects the overall temperature level of the tank. The time sampling step size of the control system is also shown. This defines the time interval for a complete calculation and decision-making process in a control system, and is a key parameter for system response speed and control accuracy. (Watering heat release net power) This represents the heat power released by the concrete pipe pile itself during the hydration reaction. This power is dynamically changing and is obtained through inverse calculation using a state observer. It is deducted as an internal heat source in the heat balance calculation. Reference pipeline flow velocity shear rate. This characterizes the average turbulent mixing kinetic energy intensity when steam is injected into the pool. It can be calculated from the radial velocity distribution measured by the pipeline velocity profile sensor array, reflecting the efficiency of steam diffusion and mixing within the pool. (Pipeline geometric cross-sectional area conversion factor) It is used to convert the steam velocity shear rate into an equivalent heat transfer capacity, and its calculation formula is as follows: , The calibration steam density under the current pipeline pressure. Given the known inner diameter of the main steam pipe. This is the characteristic roughness length of the fluid boundary layer on the inner wall of the pipe. This coefficient comprehensively considers the physical properties of the steam and the geometric characteristics of the pipe. Specific enthalpy of superheated or saturated steam. Enthalpy of the discharged condensate These represent the heat per unit mass carried by the steam entering the system and the condensate leaving the system, respectively, and can be calculated by consulting a steam enthalpy table or by measuring the steam pressure and temperature in real time. The spatial temperature penalty characteristic value at the current time t. It quantifies the degree of unevenness in temperature distribution within the steam curing tank. The larger the value, the worse the temperature uniformity. Its calculation method has been described in detail in the above scheme.

[0054] This solution provides a detailed calculation method for dynamic net heat demand, integrating multiple actual parameters affecting actual heat demand. This yields net heat demand results that better reflect actual industrial conditions, providing an accurate calculation basis for subsequent steam flow regulation. This solution utilizes the equivalent total mass of the steam curing tank. Multiply by the system equivalent overall specific heat capacity obtained by dynamic identification Then, combined with the target temperature of the next control cycle Compared with the current average temperature The difference divided by the sampling step size The obtained temperature change rate is used to calculate the basic heat power required to reach the target temperature in the next stage. The system's equivalent comprehensive specific heat capacity obtained through dynamic identification is used as the basis for this calculation. This is because this parameter reflects the dynamic changes in the system's heat capacity during steam curing, and is closer to the actual thermal state of the system than a fixed parameter, ensuring the accuracy of the basic heat calculation. Subtract the net power released by hydration. This is because the hydration reaction of concrete pipe piles during curing releases heat, which can already be used to raise the system temperature. Subtracting this portion avoids the need for additional steam input, preventing energy waste and temperature overshoot, and aligns with the actual heat balance logic of the system. The increase is based on the reference pipe network flow velocity shear rate. Conversion factor for geometric cross-sectional area of ​​pipeline network Enthalpy difference of steam and space temperature penalty characteristic value Compared with the current average temperature The compensation term is composed of ratios, where the reference pipeline flow velocity shear rate is used. It can characterize the turbulent mixing kinetic energy during steam injection, reflect the actual diffusion mixing capacity of steam, and represent the space temperature penalty characteristic value. This allows us to reflect the degree of temperature unevenness within the steam curing tank. The more severe the temperature unevenness, the more additional heat is needed to promote temperature uniformity. Therefore, by setting compensation items based on these parameters, the net heat demand can be dynamically adjusted according to the actual temperature uniformity requirements and steam diffusion capacity on site. This not only improves the problem of uneven heating and cooling within the steam curing tank but also avoids excessive steam supplementation and energy waste. The entire calculation process fully considers various practical influencing factors in industrial steam curing, resulting in a dynamic net heat demand that better reflects the actual site conditions. This provides a reliable basis for obtaining accurate optimal steam flow rates, helping to achieve precise temperature control and energy conservation goals.

[0055] As a specific implementation method, in practical applications, the equivalent total mass in the septic tank... The system's equivalent comprehensive specific heat capacity can be estimated based on the type and quantity of the pipe piles, the weight of the steel mold, and the volume of the steam curing tank, and then corrected using empirical coefficients. and net power of heat release during hydration This can be achieved by updating in real time based on historical operating data using online identification algorithms (e.g., based on Kalman filtering or recursive least squares). Process target set temperature. It can be read from a preset "time-temperature" process curve, or dynamically issued by a higher-level optimization and scheduling system. The arithmetic mean temperature at current time t. and space temperature penalty eigenvalue This is obtained through real-time data acquisition and calculation using multiple temperature sensors arranged within the steam curing tank. (Reference pipeline flow velocity shear rate) The radial velocity distribution of steam can be measured by installing a miniature Pitot tube array or hot-wire anemometer near the main steam pipeline or injection port, and then calculated. The conversion factor for the geometric cross-sectional area of ​​the pipeline network. Then it can be based on the known inner diameter of the steam pipe And material properties, combined with steam density (Acquired via steam pressure and temperature sensors) and empirical characteristic roughness length Perform calculations. Specific enthalpy of superheated or saturated vapor. Enthalpy of the discharged condensate The enthalpy of steam can be obtained by consulting industrial steam enthalpy tables or using thermodynamic calculation software based on real-time measured steam pressure and temperature. Through real-time acquisition and accurate calculation of the above parameters, the system can dynamically reconstruct the net heat demand power for the next stage.

[0056] Through the above technical solution, this application can obtain net heat demand results that are more consistent with the actual working conditions of industrial sites, providing an accurate calculation basis for subsequent steam flow regulation. This solution fully considers various influencing factors such as the dynamic changes in system heat capacity during steam curing, the self-heating of concrete hydration, the degree of temperature unevenness within the steam curing tank, and the kinetic energy of steam injection turbulent mixing. It effectively avoids the problem of excessive or insufficient steam input caused by inaccurate calculation of net heat demand in traditional temperature control methods. This not only significantly reduces energy consumption and waste, and reduces temperature overshoot and uneven heating, but also helps ensure the curing quality of concrete pipe piles, avoiding micro-cracks caused by thermal stress, thereby improving the overall performance and production efficiency of the product.

[0057] This application further proposes that step S30, the process of generating the adaptive valve damping penalty term, includes: extracting the current spatial temperature penalty feature value and the average temperature of the steam curing tank as feature variables, and evaluating the current spatial temperature non-uniformity within the tank; constructing a damping amplification mapping relationship with the spatial temperature non-uniformity as the independent variable, and combining it with the physical flow parameters of the steam pipeline network to generate an adaptive valve damping penalty term; the strength of the adaptive valve damping penalty term increases adaptively with the aggravation of the spatial temperature non-uniformity, used to limit drastic changes in the steam valve opening when the temperature gradient is large; the formula for generating the adaptive valve damping penalty term is as follows:

[0058]

[0059] in, This is an adaptive valve damping penalty term; Enthalpy of superheated or saturated vapor; The specific enthalpy of the discharged condensate; This is the benchmark value for maximum steam condensation efficiency; For reference, the shear rate of the pipeline flow velocity; This refers to the time sampling step size of the control system. The spatial temperature penalty characteristic value at the current time t; The arithmetic mean temperature at the current time t. Adaptive valve damping penalty term. It is a dynamically adjusted coefficient, whose function is to adjust the instantaneous steam flow rate increment during the subsequent optimization of the objective cost function. The adjustment range is constrained. The magnitude of this penalty term directly affects the conservatism or aggressiveness of the flow increment in the optimization result. Enthalpy of superheated or saturated steam. Enthalpy of the discharged condensate These are key physical parameters characterizing the heat-carrying capacity of steam; the difference between them... This represents the effective heat released per unit mass of steam. These specific enthalpy values ​​can be obtained by consulting tables of steam thermodynamic properties or calculating using equations of state, based on the steam's pressure and temperature. (Maximum steam condensation efficiency benchmark value) This represents the upper limit of the steam condensation heat exchange efficiency of the system under ideal operating conditions. It reflects the inherent performance of the steam curing tank heat exchange system and is typically calibrated using system design parameters or historical operating data. (Reference pipeline flow velocity shear rate) The average turbulent mixing kinetic energy intensity, used to characterize the steam injection within the pool, is related to factors such as the steam injection velocity and pipeline geometry. It can be calculated from the radial velocity distribution measured by a pipeline velocity profile sensor array, or estimated using a fluid dynamics model. The time sampling step size of the control system... This is the time interval required for a control system to perform a complete measurement, calculation, and control action. It determines the response speed and discretization accuracy of the control system and is typically set by the controller's hardware performance and control strategy requirements. Space temperature penalty characteristic value. This is an indicator of the unevenness of temperature spatial distribution within a steam curing tank. A higher value indicates a more uneven temperature distribution. This characteristic value is calculated using a specific formula based on data collected by multiple temperature sensors within the steam curing tank, combined with the sensor's spatial coordinates and distance from the steam injection holes. The arithmetic mean temperature at the current time t is... It is the average temperature collected by all temperature sensors in the steam curing tank, representing the overall temperature level of the steam curing tank. It can be obtained by calculating the arithmetic average of all sensor data.

[0060] This solution generates an adaptive valve damping penalty term by combining existing baseline parameters of the steam curing system with real-time temperature data. Specifically, the calculation of this penalty term first uses the steam specific enthalpy difference... and the maximum condensation efficiency benchmark value The product of the squares serves as a basis, reflecting the inherent heat transfer capacity of steam and setting a reference amplitude for the damping term that matches the system's thermodynamic characteristics. Next, the reference pipe network flow velocity shear rate is introduced. and the time sampling step of the control system As a denominator term, this ensures that the damping strength is adapted to the system's control rhythm and the kinetic energy characteristics of the steam injection, avoiding the problem of mismatch between constraint strength and system control characteristics. Based on this, this scheme introduces a space temperature penalty eigenvalue. Arithmetic mean temperature at current time t The ratio of these factors is used as the independent variable of the exponential function to construct an exponential adjustment term. This design allows the penalty term to dynamically adjust the damping magnitude based on the current temperature non-uniformity within the steam curing tank. When the temperature non-uniformity within the steam curing tank is high, the spatial temperature penalty characteristic value... This will increase, leading to an increase in the exponential term, and thus affecting the calculated adaptive valve damping penalty term. This also increases accordingly. In the subsequent optimization and solution of the objective cost function, the larger... The excessively large instantaneous steam flow rate increment will be addressed. Applying stronger constraints effectively avoids the problem of excessively large adjustment ranges potentially exacerbating temperature unevenness and steam waste. Conversely, when the temperature uniformity within the steam curing tank is good, Smaller This also reduces the constraint accordingly, avoiding excessive constraints on necessary adjustment actions and ensuring the response speed of temperature regulation. In this way, when constructing the objective cost function in step S30, this scheme can introduce this dynamically adjusted constraint into the optimization solution process, ensuring that the obtained optimal instantaneous steam flow rate increment... It can meet the temperature control requirements while also taking into account energy saving and temperature uniformity, thus solving the problem that fixed damping cannot adapt to dynamic working conditions.

[0061] As a specific implementation method, in practical applications, the specific enthalpy of superheated or saturated steam... Enthalpy of the discharged condensate The maximum steam condensation efficiency benchmark value can be obtained in advance by consulting the steam meter or calculating using engineering thermodynamics software and stored as a constant in the controller, or it can be calculated online based on real-time measured steam pressure and temperature. Offline calibration can be performed based on the design parameters and historical operating data of the steam curing tank, for example, by conducting heat balance tests under stable operating conditions. Reference pipeline flow velocity shear rate. The radial velocity distribution can be measured in real time by installing a velocity profile sensor array at the inlet of the main steam pipe and calculated based on fluid dynamics principles, or estimated during the system design phase using CFD simulation and used as a fixed parameter. The time sampling step size of the control system... This is set by the controller's program; for example, it can be set to 10 seconds or 30 seconds. Space temperature penalty characteristic value. and the arithmetic mean temperature at the current time t This requires real-time data acquisition. For example, multiple temperature sensors, such as PT100 RTDs, are evenly distributed within the steam curing tank. These sensors collect temperature data from different locations within the tank in real time. This data is filtered by the underlying hardware and then processed by the controller. The controller first calculates the arithmetic mean of the temperatures from all sensors to obtain... Simultaneously, based on the preset sensor spatial coordinates and steam injection orifice coordinates, the straight-line distance from each sensor to the nearest effective steam injection orifice is calculated. And combined with the maximum spatial characteristic of the septic tank, the diagonal length Using the formula Calculate Once these parameters are obtained, the controller can calculate the adaptive valve damping penalty term in real time according to the above formula. The result is then used as input into the objective cost function for optimization.

[0062] Through the above technical solution, this application can dynamically adjust the constraint strength of valve flow regulation according to the actual working conditions of the steam curing tank, solving the problem that fixed damping cannot adapt to dynamic working conditions. When the temperature non-uniformity in the steam curing tank is high, the calculated damping penalty term is larger, which can exert a stronger constraint on excessive flow regulation increments, avoiding excessive adjustment ranges that exacerbate temperature non-uniformity and steam waste. When the temperature uniformity in the steam curing tank is good, the damping penalty term is smaller, avoiding excessive constraint on necessary adjustment actions, ensuring the response speed of temperature regulation, and enabling rapid adjustment of the temperature to the target value required by the process. This makes the entire temperature control regulation process more reasonable, ensuring the temperature control requirements of concrete pipe pile steam curing while avoiding unnecessary steam waste, thus achieving the goal of energy saving.

[0063] This application further proposes that step S30, obtaining the optimal instantaneous steam flow rate increment, includes: constructing a target cost function with the instantaneous steam flow rate increment as the decision variable. The target cost function is composed of two related parts: the first part is a heat tracking deviation evaluation term, used to characterize the deviation level between the actual expected heating power and the dynamic net heat demand power; the second part is a control action damping evaluation term, composed of the instantaneous steam flow rate increment and the adaptive valve damping penalty term; the target cost function is solved using an extreme value optimization algorithm to find the optimal solution that makes the partial derivative or gradient of the target cost function approach zero, thereby outputting the optimal instantaneous steam flow rate increment that balances heat demand tracking accuracy and valve action stability; the formula for constructing the target cost function and setting its Jacobian matrix gradient with respect to the flow rate increment to zero is as follows:

[0064]

[0065] Therefore, the formula for obtaining the optimal instantaneous steam flow rate increment through optimization is:

[0066]

[0067] in, The Jacobian gradient of the objective cost function with respect to the flow increment is obtained by differentiating the cost function, which includes the energy tracking bias and damping terms. Enthalpy of superheated or saturated vapor; The specific enthalpy of the discharged condensate; The dynamic condensation heat transfer efficiency at the current time t; The reconstructed dynamic net heat demand power; This represents the instantaneous steam inlet flow rate actually measured at the current moment. This represents the optimal instantaneous steam flow rate increment. This is the adaptive valve damping penalty term. The formula for the objective cost function with respect to the Jacobian matrix gradient of the flow increment being zero is based on finding the flow increment that minimizes the objective cost function through mathematical means. In optimization theory, when the gradient of a function is zero, the function is usually at a local minimum, providing a theoretical basis for directly solving for the optimal solution. This formula combines the energy tracking deviation term with the adaptive valve damping penalty term to form a comprehensive optimization objective. By differentiating it and setting it to zero, the analytical expression for the optimal instantaneous steam flow increment can be derived. The formula for the optimal instantaneous steam flow increment is the analytical solution obtained directly through algebraic derivation under the condition that the gradient is zero. The significance of this formula is that it provides a method for directly calculating the optimal flow increment without iteration, greatly improving the solution efficiency and real-time performance. (Jacobi gradient) The objective cost function is expressed as a function of the flow rate increment. The rate and direction of change are key indicators for measuring the trend of function changes during the optimization process. (Specific enthalpy of superheated or saturated vapor) Enthalpy of the discharged condensate These are important parameters of steam thermodynamics, characterizing the energy carried by steam and condensate, and forming the basis for calculating heat input and energy balance. The dynamic condensation heat transfer efficiency at the current time t... This is a real-time changing parameter that reflects the actual efficiency of steam condensation and heat release within the septic tank; its dynamic nature ensures the accuracy of heat calculations. The reconstructed dynamic net heat demand power... This is the net heat input rate required by the system to reach the target temperature in the next stage, and it is the direct basis for the control system to adjust the steam flow rate. The actual measured instantaneous steam inlet flow rate at the current moment. This is the current operating state of the system and serves as the benchmark for incremental adjustments. Optimal instantaneous steam flow rate increment. This is the final output of the optimization process, representing the steam flow adjustment required to bring the system to its optimal state. Adaptive valve damping penalty term. It is a dynamically adjusted coefficient used to balance the response speed and stability of the control system, prevent system oscillations caused by over-adjustment, and ensure a rapid response when necessary.

[0068] This scheme constructs a target cost function that includes energy tracking bias and adaptive valve damping penalty terms, and cleverly utilizes optimization theory to directly derive the optimal instantaneous steam flow rate increment by setting the Jacobian gradient of this cost function with respect to the flow rate increment to zero. The analytical expression for this is given. In the actual operation, the system first obtains the dynamic condensation heat transfer efficiency at the current time t from the preceding steps. The reconstructed dynamic net heat demand power The instantaneous flow rate of steam inlet actually measured at the current moment. and adaptive valve damping penalty term These parameters comprehensively reflect the current actual thermodynamic state of the steam curing tank, heat demand, and stability considerations of the control system. Subsequently, these real-time parameters are substituted into the pre-derived optimal instantaneous steam flow rate increment. The analytical formula directly calculates the required steam flow adjustment under the current system state to minimize the objective cost function—that is, to meet heat demand while maintaining control stability. This direct calculation method avoids the computational burden and convergence problems that may arise from traditional iterative optimization methods. Ultimately, the calculated optimal instantaneous steam flow increment... The signals will be passed to the subsequent control output and closed-loop execution module to generate precise control signals to adjust the steam valve opening, thereby achieving precise control of the steam curing tank temperature. In this way, this solution transforms a complex dynamic optimization problem into an efficient analytical solution process, ensuring the real-time performance, accuracy, and stability of the control commands, thus effectively addressing the shortcomings of traditional methods in terms of efficiency and accuracy.

[0069] As a specific implementation method, the above-mentioned technical means can be implemented with reference to the following example. In an industrial control system, for example, a high-performance industrial PC or embedded controller is used as the core processing unit, which can be configured with a real-time operating system (RTOS). At the beginning of each control cycle, the processing unit obtains the dynamic condensation heat transfer efficiency at the current time t from the sensor data acquisition module. The reconstructed dynamic net heat demand power The instantaneous flow rate of steam inlet actually measured at the current moment. and adaptive valve damping penalty term Acquiring these parameters may involve communication with underlying sensor interfaces (such as Modbus TCP / IP, EtherCAT, etc.) and the output of preceding calculation modules. Once all the necessary input parameters are ready, the control algorithm module of the processing unit will immediately execute the pre-programmed optimal instantaneous steam flow increment. The analytical formula is derived from this. The calculation process involves direct algebraic operations without any iterative loops, thus allowing for completion in a very short time. For example, in environments such as C / C++ or MATLAB / Simulink, this formula can be compiled into efficient machine code or generated as executable real-time code. After calculation, the optimal instantaneous steam flow rate increment is obtained. As a numerical result, it is immediately sent to the control output interface, such as through an analog output module (AO) or a digital output module (DO) to drive the actuator of the steam valve, thereby achieving precise adjustment of the steam flow. The entire process is completed within a fixed control cycle, ensuring real-time control and fast response.

[0070] Through the above technical solution, this application provides a clear and directly implementable optimization solution path that balances solution accuracy and computational efficiency. This solution directly derives the analytical expression for the optimal instantaneous steam flow increment by setting the gradient of the Jacobian matrix of the objective cost function with respect to the flow increment to zero. This avoids the computational burden and convergence problems that may arise from traditional iterative optimization methods, significantly improving the real-time response capability of the control system. Furthermore, since this analytical solution is calculated based on real-time system parameters such as dynamic condensation heat transfer efficiency, dynamic net heat demand power, the current actual instantaneous steam inlet flow rate, and adaptive valve damping penalty terms, it accurately reflects the current true thermodynamic state and control requirements of the system, providing accurate and reliable adjustment values ​​for steam valve regulation. This not only ensures the temperature control accuracy of the steam curing process and effectively avoids temperature overshoot and fluctuations, but also minimizes energy waste through precise steam flow control, achieving significant energy-saving effects.

[0071] This application further proposes that in step S40, the actual measured instantaneous steam inlet flow rate at the current moment is arithmetically superimposed with the calculated optimal instantaneous steam flow rate increment, and this superposition is used as the target control signal to be executed at the next moment and sent to the steam valve; the formula for generating the control signal to adjust the steam valve opening is as follows:

[0072]

[0073] in, The target instantaneous steam inlet flow rate should be executed at the next moment; This represents the instantaneous steam inlet flow rate actually measured at the current moment. This represents the optimal instantaneous steam flow rate increment. The target instantaneous steam inlet flow rate to be executed at the next moment. This represents the desired steam supply volume of the control system in the next control cycle. As the final output of the control command, it directly determines the opening degree of the steam regulating valve. This target flow rate can be sent to the steam valve controller as a digital signal or converted into a standard analog signal (e.g., a 4-20mA current signal or a 0-10V voltage signal) to drive the valve actuator. The actual measured instantaneous steam inlet flow rate at the current moment... This refers to the steam supply obtained by the system in real-time monitoring at the current moment, reflecting the current actual operating status and steam consumption level of the steam curing system. This flow rate can be measured in real-time by flow sensors (such as vortex flow meters, differential pressure flow meters, Coriolis mass flow meters, etc.) installed at the inlet of the main steam pipeline, and the analog signal is converted into a digital signal by a data acquisition system for use by the controller. Optimal instantaneous steam flow rate increment. This is a recommended value for adjusting the current steam flow rate, derived through a series of calculations and optimization processes (steps S10 to S30 in claim 1) based on the thermal state of the steam curing tank, the target temperature, and energy-saving optimization objectives. It represents the amount that needs to be increased or decreased from the current steam flow rate to achieve or maintain the target temperature while also achieving energy savings. This incremental value is typically calculated and generated by the optimization algorithm module within the control system. The superposition operation refers to adding the currently measured instantaneous steam inlet flow rate... With the optimal instantaneous steam flow rate increment By performing arithmetic summation, the target instantaneous steam inlet flow rate that should be executed at the next moment can be obtained. This operation is performed in the controller's computing unit, and its function is to transform the adjustment suggestions of the optimization algorithm into specific, executable flow setpoints, thereby achieving dynamic and refined control of the steam flow.

[0074] As a specific implementation method, an industrial programmable logic controller (PLC) or a distributed control system (DCS) can be used as the central control unit. At the beginning of each control cycle, a flow sensor installed at the inlet of the main steam pipe measures the instantaneous flow rate at the steam inlet in real time. The analog signal is then converted into a digital signal and transmitted to the control unit. Simultaneously, the optimization module within the control unit, based on multi-point temperature data from the steam curing tank, real-time steam temperature, system thermal state parameters, and the target set temperature, performs a series of complex calculations to determine the optimal instantaneous steam flow rate increment required for the current control cycle. Subsequently, the control unit performs a simple arithmetic operation, converting the real-time measured instantaneous steam inlet flow rate... Compared with the calculated optimal instantaneous steam flow rate increment Add them together to obtain the target instantaneous steam inlet flow rate that should be executed at the next moment. For example, if the currently measured steam flow rate The optimal increment calculated by the optimization module is 100 kg / h. If the target steam flow rate is +5 kg / h, then the target steam flow rate at the next moment is... It will be set at 105 kg / h. This is the target flow rate. The command is then sent to the actuator of the steam regulating valve. Upon receiving the command, the valve actuator adjusts the valve opening accordingly to ensure that the actual steam flow rate approaches this new target value. In this way, a seamless connection is achieved between complex optimization calculations and actual physical control actions.

[0075] Through the above technical solution, this application provides a clear and operable method for controlling steam flow output, solving the problem of lacking clear basis for control output in traditional methods. By superimposing the optimal instantaneous steam flow increment onto the current actual instantaneous steam inlet flow, the effective implementation of the previous optimization calculation results can be ensured, achieving precise steam supply. This not only avoids excessive or insufficient steam supply due to deviations in target flow calculation, thereby effectively saving energy and reducing operating costs, but also maintains stable temperature within the steam curing tank, reducing the impact of temperature fluctuations on the quality of concrete pipe piles and ensuring product performance. This incremental adjustment based on actual feedback makes the entire temperature control system more stable, efficient, and energy-saving.

[0076] Traditional steam curing temperature control systems for concrete pipe piles face challenges in practical industrial applications, including uneven heating within the curing tank, significant energy waste, and large temperature fluctuations that negatively impact product quality. Specifically, due to the large volume of the curing tank and the numerous pipe piles and steel molds stacked inside, it is a typical high-inertia, highly nonlinear thermodynamic system. Simply relying on local temperature feedback to open and close valves cannot cope with the three-dimensional heat gradient formed by steam diffusion within the complex geometry, leading to severe uneven heating within the tank. Furthermore, traditional methods treat the curing system as a simple passive heat receiver, failing to consider the dynamic evolution of the pipe pile's heat absorption capacity at different curing stages and the complex thermodynamic changes within the system. The crude "add steam when cold, cut off steam when hot" strategy often causes temperature overshoot and ineffective steam venting during the heating and isothermal phases. The lack of feedforward physical compensation leads to drastic local temperature fluctuations, resulting not only in significant energy consumption but also easily inducing micro-cracks in the surface of the pipe piles due to thermal stress.

[0077] To address the aforementioned issues, this application proposes a temperature control and energy-saving device for steam curing concrete pipe piles, comprising: a feature extraction and efficiency calculation module, used to acquire multi-point temperature data, sensor spatial coordinates, and real-time steam temperature within the steam curing tank, extract spatial temperature penalty feature values ​​characterizing the degree of spatial unevenness, and calculate the dynamic condensation heat transfer efficiency; a state identification and demand reconstruction module, used to dynamically identify system thermal state parameters based on historical system heat input and temperature response, and reconstruct the dynamic net heat demand power for the next stage of the system by combining the spatial temperature penalty feature values, reference pipeline flow velocity shear rate, and target set temperature; a cost optimization and increment generation module, used to construct a target cost function including an adaptive valve damping penalty term based on the dynamic condensation heat transfer efficiency and the dynamic net heat demand power, and obtain the optimal instantaneous steam flow increment based on the optimization solution; and a control output and closed-loop execution module, used to superimpose the optimal instantaneous steam flow increment onto the current actual instantaneous steam inlet flow to generate a control signal to adjust the steam valve opening.

[0078] The core innovation of this embodiment lies in combining the quantification of spatial temperature distribution with the dynamic identification of the system's thermal state, and introducing considerations for steam mixing efficiency and optimized control strategies. This allows for the accurate calculation of dynamic net heat demand and the suppression of valve regulation fluctuations, effectively addressing uneven heating and cooling within the steam curing tank, reducing energy waste, and ensuring product quality. Specifically, the feature extraction and efficiency calculation module performs spatial analysis of multi-point temperature data, enabling the system to identify and quantify the distribution of hot and cold regions. The state identification and demand reconstruction module dynamically tracks changes in the heat source of the pipe pile's hydration reaction, ensuring that the heat demand calculation closely matches actual operating conditions. The adaptive damping mechanism of the cost optimization and incremental generation module effectively constrains the adjustment range, preventing excessive response from exacerbating temperature fluctuations. Through these technical solutions, the uniformity of temperature distribution within the steam curing tank is significantly improved, steam consumption is reduced, and the negative impact of drastic temperature fluctuations on the quality of the pipe piles is avoided, achieving refined and intelligent management of the steam curing process.

[0079] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, and improvements made within the spirit and principles of the present invention should be included within the protection scope of the present invention.

Claims

1. A method for temperature control and energy saving during steam curing of concrete pipe piles, characterized in that, Includes the following steps: Step S10: Obtain multi-point temperature data, sensor spatial coordinates and real-time steam temperature in the steam curing tank, extract spatial temperature penalty feature values ​​that characterize the degree of spatial distribution non-uniformity, and calculate dynamic condensation heat exchange efficiency. Step S20: Based on the historical heat input and temperature response of the system, dynamically identify the thermal state parameters of the system, and combine the spatial temperature penalty characteristic value, the reference pipeline flow rate shear rate and the target set temperature to reconstruct the dynamic net heat demand power of the system in the next stage. Step S30: Based on the dynamic condensation heat exchange efficiency and the dynamic net heat demand power, construct an objective cost function that includes an adaptive valve damping penalty term, and obtain the optimal instantaneous steam flow increment based on the optimization solution; Step S40: The optimal instantaneous steam flow rate increment is superimposed on the current actual instantaneous steam inlet flow rate to generate a control signal to adjust the steam valve opening.

2. The energy-saving method for temperature control during steam curing of concrete pipe piles according to claim 1, characterized in that, In step S10, the process of extracting the space temperature penalty feature value includes: Calculate the temperature deviation characteristics between the actual temperature at each temperature measurement point and the average temperature of the steam incubator. By combining the spatial distance from each temperature measuring point to the nearest effective steam injection hole, a distance attenuation weight function is constructed, which monotonically decreases as the spatial distance increases. The temperature deviation feature is weighted and fused with the corresponding distance attenuation weight function to obtain the space temperature penalty feature value; the space temperature penalty feature value is positively correlated with the dispersion of the temperature deviation feature.

3. The energy-saving method for steam curing temperature control of concrete pipe piles according to claim 2, characterized in that, In step S10, the process of calculating the dynamic condensation heat transfer efficiency includes: The maximum steam condensation efficiency of the system under ideal conditions is obtained as a benchmark value; A heat conduction driving term is established based on the difference between the real-time steam temperature at the steam inlet and the average temperature of the septic tank; A heat transfer attenuation inhibition term is established based on the aforementioned space temperature penalty characteristic value; A nonlinear mapping is performed based on the baseline value, the heat conduction driving term, and the heat transfer attenuation resistance term to generate a dynamic condensation heat transfer efficiency; wherein the value of the dynamic condensation heat transfer efficiency is positively correlated with the heat conduction driving term and negatively correlated with the heat transfer attenuation resistance term.

4. The energy-saving method for temperature control during steam curing of concrete pipe piles according to claim 3, characterized in that, In step S20, the system thermal state parameters include the system's equivalent comprehensive specific heat capacity and net hydration heat release power, and the dynamic identification process includes: System equivalent comprehensive specific heat capacity identification: Based on the energy conservation relationship between the effective heat of net steam input accumulated within a set historical sliding time window and the actual temperature rise of the steam curing tank during that window period, the system equivalent comprehensive specific heat capacity at the current moment is dynamically estimated. Inverse calculation of net hydration heat release power: Construct a system thermal state observer, and calculate the total sensible heat demand of the system based on the currently calculated equivalent comprehensive specific heat capacity of the system and the actual temperature rise rate at the previous moment; remove the effective condensation heat of steam actually input at the previous moment from the total sensible heat demand, and take the difference between the two as the net hydration heat release power spontaneously released by the hydration reaction of the pipe pile.

5. The energy-saving method for temperature control during steam curing of concrete pipe piles according to claim 4, characterized in that, In step S20, the process of reconstructing the dynamic net heat demand power of the system in the next stage includes: Based on the process target set temperature, equivalent total mass of the steam curing tank, and the identified equivalent comprehensive specific heat capacity of the system for the next control cycle, the basic sensible heat power requirement required for the system to follow the standard process curve is calculated. The basic net heat demand is obtained by subtracting the identified net hydration heat release power from the basic sensible heat power demand. By introducing the reference network flow velocity shear rate characterizing the steam injection kinetic energy and the space temperature penalty characteristic value, a dynamic heat compensation term is constructed to smooth out local thermal gradients and fluid disturbance dissipation. The basic net heat demand is superimposed and integrated with the dynamic heat compensation item to reconstruct the dynamic net heat demand power for the next stage of the system.

6. The energy-saving method for temperature control during steam curing of concrete pipe piles according to claim 1, characterized in that, In step S30, the process of generating the adaptive valve damping penalty term includes: Extract the spatial temperature penalty feature value and the average temperature of the septic tank at the current moment as feature variables to evaluate the spatial temperature non-uniformity in the tank at the current moment. A damping amplification mapping relationship with the aforementioned spatial temperature non-uniformity as the independent variable is constructed, and an adaptive valve damping penalty term is generated by combining the physical flow parameters of the steam pipeline network. The strength of the adaptive valve damping penalty term increases adaptively with the aggravation of the spatial temperature non-uniformity, which is used to limit drastic changes in the opening of the steam valve when the temperature gradient is large.

7. The energy-saving method for temperature control during steam curing of concrete pipe piles according to claim 1, characterized in that, In step S30, the process of obtaining the optimal instantaneous steam flow rate increment includes: A target cost function is constructed with the instantaneous steam flow increment as the decision variable. The target cost function is composed of two related parts: the first part is a heat tracking deviation evaluation term, which is used to characterize the deviation level between the actual expected heating power and the dynamic net heat demand power; the second part is a control action damping evaluation term, which is composed of the instantaneous steam flow increment and the adaptive valve damping penalty term. An extreme value optimization algorithm is used to solve the target cost function, and the optimal solution is found that makes the partial derivative or gradient of the target cost function approach zero, thereby outputting the optimal instantaneous steam flow increment that balances the accuracy of heat demand tracking and the smoothness of valve operation.

8. The energy-saving method for temperature control during steam curing of concrete pipe piles according to claim 1, characterized in that, In step S40, the instantaneous flow rate of the steam inlet measured at the current moment is arithmetically superimposed with the incremental value of the optimal instantaneous steam flow rate obtained by solving, and sent to the steam valve as the target control signal to be executed at the next moment.

9. A temperature control and energy-saving device for steam curing concrete pipe piles, characterized in that, include: The feature extraction and efficiency calculation module is used to acquire multi-point temperature data, sensor spatial coordinates and real-time steam temperature in the steam curing tank, extract spatial temperature penalty feature values ​​that characterize the degree of spatial distribution non-uniformity, and calculate the dynamic condensation heat transfer efficiency. The state identification and demand reconstruction module is used to dynamically identify the system's thermal state parameters based on the system's historical heat input and temperature response, and reconstruct the dynamic net heat demand power of the system in the next stage by combining the space temperature penalty characteristic value, the reference pipeline flow rate shear rate and the target set temperature. The cost optimization and increment generation module is used to construct a target cost function containing an adaptive valve damping penalty term based on the dynamic condensation heat exchange efficiency and the dynamic net heat demand power, and to obtain the optimal instantaneous steam flow increment based on the optimization solution. The control output and closed-loop execution module is used to superimpose the optimal instantaneous steam flow rate increment onto the current actual instantaneous steam inlet flow rate to generate a control signal to adjust the steam valve opening.

Images