Data regulation method and system of air compressor, medium and product

Abstract

A data regulation method and system of an air compressor, a medium and a product, wherein the method comprises: acquiring pipeline geometric parameters from a target air compressor to an end gas point, real-time pressure sequence of the end gas point, real-time dew point value and real-time volume flow, and effective adsorption volume parameters of a post-processing drying device; calculating transmission lag time of compressed air from the outlet of the target air compressor to the end gas point; calculating target compensation flow when air pressure meets the condition; calculating critical residence time, and determining the maximum allowable loading flow rate of the target air compressor at the current time according to the ratio of the effective adsorption volume parameters to the critical residence time; if the target compensation flow is greater than the maximum allowable loading flow rate, a flow limiting quality preserving instruction is generated, and the target air compressor is controlled to run at the maximum allowable loading flow rate based on the flow limiting quality preserving instruction. The application improves the accuracy of data regulation of the air compressor.

Description

Technical Field

[0001] This application relates to the field of data control technology, specifically to a data control method, system, medium, and product for an air compressor. Background Technology

[0002] In modern industrial production, compressed air, as the second largest power source after electricity, is widely used in automation control, pneumatic actuation, process cooling, and other processes. Current technology uses long-distance pipelines to transport compressed air from air compressor stations to various end-user points. Pressure sensors are installed at the air compressor outlet or main pipeline to collect pressure values ​​in real time and feed them back to the controller. The controller compares the measured pressure with a preset threshold. When the pressure drops to the lower threshold, it determines that the air demand has increased, and then controls the air compressor to increase its loading rate or starts a standby unit to supplement the exhaust volume; conversely, it reduces the load or shuts down the compressor.

[0003] However, due to the long physical distance between the air compressor station and the end-user air consumption point, when a large amount of air is used instantaneously at the end-user air consumption point, causing a sharp drop in pressure, the air compressor will quickly load to supplement the airflow in order to overcome the pipeline transmission resistance and quickly restore the end-user pressure. However, during this process, the compressed air velocity through the post-treatment drying equipment increases sharply. If the airflow velocity is too fast, the residence time of the compressed air in the adsorption layer of the drying equipment will be significantly shortened, which may result in the desiccant not having enough time to fully adsorb moisture, causing a large amount of unsaturated humid air to directly enter the pipeline network, resulting in excessive moisture content in the compressed air at the end-user air consumption point (i.e., the dew point is not up to standard). It is difficult to achieve a balance between "pressure response speed for long-distance transportation" and "drying quality of the post-treatment equipment", which reduces the accuracy of the air compressor's data control. Summary of the Invention

[0004] This application provides a data control method, system, medium, and product for air compressors, which solves the problem of air compressors struggling to achieve a balance between pressure response speed during long-distance transportation and drying quality of post-processing equipment, thereby improving the accuracy of air compressor data control.

[0005] The first aspect of this application provides a data control method for an air compressor, the method comprising: The pipeline geometric parameters from the target air compressor to the end air consumption point, the real-time pressure sequence of the end air consumption point, the real-time dew point value and real-time volumetric flow rate of the target air compressor outlet, and the effective adsorption volume parameters of the post-treatment drying equipment are obtained. Based on the pipeline geometry parameters, the real-time dew point value, and the real-time volumetric flow rate, calculate the transmission lag time of compressed air from the outlet of the target air compressor to the end point of air consumption. The pressure change rate is obtained by differential calculation of the real-time pressure sequence. When the pressure change rate is negative and the absolute value of the pressure change rate is greater than the preset pressure change threshold, the target compensation flow is calculated based on the pressure change rate and the transmission lag time. Based on the real-time dew point value and the preset saturated vapor pressure characteristic curve, the critical residence time for the compressed air in the post-treatment drying equipment to meet the preset dew point qualification condition is calculated, and the maximum allowable loading flow rate of the target air compressor at the current moment is determined according to the ratio of the effective adsorption volume parameter to the critical residence time. If the target compensation flow rate is greater than the maximum allowable loading flow rate, a flow-limiting and quality-preserving command is generated, and the target air compressor is controlled to operate according to the maximum allowable loading flow rate based on the flow-limiting and quality-preserving command.

[0006] Optionally, based on the pipeline geometry parameters, the real-time dew point value, and the real-time volumetric flow rate, the transmission lag time of compressed air from the target air compressor outlet to the end-point air consumption is calculated, specifically including: Calculate the physical volume of the pipeline between the target air compressor and the end point of air consumption based on the pipeline geometry parameters; The real-time compressed air pressure in the pipeline between the target air compressor and the end point of air consumption is obtained. Based on the real-time compressed air pressure and the preset gas state equation, the real-time volumetric flow rate is converted into the operating condition state corresponding to the real-time compressed air pressure to obtain the pressure operating condition volumetric flow rate. The current water vapor partial pressure is determined based on the real-time dew point value, and the volumetric flow rate under the pressure condition is corrected for wet air based on the water vapor partial pressure to obtain the actual delivery volumetric flow rate. The actual delivery volumetric flow rate is used to compensate for the velocity increment caused by the water vapor partial pressure occupying the physical space of the pipeline. The transmission lag time is obtained by calculating the ratio of the physical volume of the pipeline to the actual transport volume flow rate.

[0007] Optionally, the volumetric flow rate under the pressure condition is corrected for humid air based on the partial pressure of water vapor to obtain the actual delivery volumetric flow rate, specifically including: The difference between the real-time compressed air pressure and the water vapor partial pressure is calculated to obtain the dry air partial pressure; The ratio of the real-time compressed air pressure to the dry air partial pressure is determined as the humid air expansion correction factor; The actual delivery volumetric flow rate is obtained by multiplying the volumetric flow rate under the pressure condition with the humid air expansion correction coefficient.

[0008] Optionally, the target compensation flow rate is calculated based on the pressure change rate and the transmission lag time, specifically including: The product of the absolute value of the pressure change rate and the transmission lag time is calculated to obtain the predicted pressure drop during the lag period; If the predicted pressure drop during the lag period is greater than the preset critical venting threshold of the pipeline network, then the linear initial compensation flow rate is calculated based on the pressure change rate, and the historical gas consumption cycle duration of the terminal gas consumption point is obtained. The ratio of the transmission lag time to the historical gas consumption cycle duration is calculated to obtain the lag response ratio; The overshoot attenuation coefficient is calculated based on the hysteresis response ratio, and the product of the linear initial compensation flow and the overshoot attenuation coefficient is determined as the target compensation flow. If the predicted pressure drop during the lag period is less than or equal to the critical venting threshold of the pipeline network, then the linear initial compensation flow rate is determined as the target compensation flow rate.

[0009] Optionally, the overshoot attenuation coefficient is calculated based on the hysteresis response ratio, specifically including: The fractional part of the hysteresis response ratio is defined as the periodic synchronization deviation. If the periodic synchronization deviation does not fall into the preset reverse superposition risk zone, the anti-overshoot attenuation coefficient is calculated based on the preset standard attenuation curve. The preset reverse superposition risk zone is used to characterize the risk range where the gas demand decreases when the compensation flow reaches the end due to transmission lag. If the periodic synchronization deviation falls into the preset reverse superposition risk zone, the ratio of the real-time dew point value to the preset limit dew point threshold is calculated to obtain the dew point penalty weight. The initial attenuation is obtained by multiplying the periodic synchronization deviation by the dew point penalty weight. The dynamic clamping attenuation is determined based on the initial attenuation and the preset maximum allowable attenuation threshold. The difference between the preset reference attenuation coefficient and the dynamic clamping attenuation amount is determined as the overshoot attenuation coefficient.

[0010] Optionally, the dynamic clamping attenuation is determined based on the initial attenuation and the preset maximum allowable attenuation threshold, specifically including: If the initial attenuation is greater than the preset maximum allowable attenuation threshold, then the maximum allowable attenuation threshold is determined as the dynamic clamping attenuation. If the initial attenuation is less than or equal to the preset maximum allowable attenuation threshold, then the initial attenuation is determined as the dynamic clamping attenuation.

[0011] Optionally, based on the real-time dew point value and the preset saturated vapor pressure characteristic curve, the critical residence time for the compressed air to meet the preset dew point qualification condition in the post-treatment drying equipment is calculated, specifically including: Based on the preset saturated vapor pressure characteristic curve, the current saturated water vapor partial pressure corresponding to the real-time dew point value and the target saturated water vapor partial pressure corresponding to the preset dew point qualification conditions are determined respectively. Calculate the difference between the current saturated water vapor partial pressure and the target saturated water vapor partial pressure to obtain the water vapor partial pressure difference that needs to be removed; Obtain the adsorption rate constant of the post-treatment drying equipment, and calculate the ratio of the partial pressure difference of water vapor to be removed to the current saturated water vapor partial pressure to obtain the relative humidity removal rate; A logarithmic decay model is constructed based on the relative humidity removal rate and the adsorption rate constant. The critical residence time is obtained by inversely solving the logarithmic decay model.

[0012] In a second aspect, embodiments of this application provide a data control system for an air compressor, the data control system for the air compressor including: one or more processors and a memory; the memory is coupled to the one or more processors, the memory is used to store computer program code, the computer program code including computer instructions, and the one or more processors call the computer instructions to cause the data control system of the air compressor to perform the method as described in the first aspect and any possible implementation thereof.

[0013] Thirdly, embodiments of this application provide a computer-readable storage medium including instructions that, when executed on a data control system of an air compressor, cause the data control system of the air compressor to perform the method described in the first aspect and any possible implementation thereof.

[0014] Fourthly, embodiments of this application provide a computer program product containing instructions that, when the computer program product is run on the data control system of an air compressor, cause the data control system of the air compressor to perform the method described in the first aspect and any possible implementation thereof.

[0015] In summary, one or more technical solutions provided in this application have at least the following technical effects or advantages: 1. By introducing a dual constraint mechanism of transmission lag time and critical residence time, on the one hand, the transmission lag time is accurately calculated based on pipeline geometric parameters, real-time dew point value, and volumetric flow rate, and the target compensation flow rate is proactively determined in conjunction with the pressure change rate, thus solving the overcompensation problem caused by transmission delay. On the other hand, the critical residence time is calculated based on the real-time dew point value, and the maximum allowable loading flow rate is determined in conjunction with the effective adsorption volume parameter. When the target compensation flow rate exceeds this flow rate, the flow is actively limited, thereby ensuring that the compressed air has sufficient adsorption time in the drying equipment while responding quickly to end pressure fluctuations. This avoids quality accidents caused by excessive flow rate leading to dew point exceeding the standard, and ultimately achieves a synergistic control effect that balances pressure response speed and drying quality, improving the accuracy of air compressor data control.

[0016] 2. By introducing the water vapor partial pressure determined based on the real-time dew point value, a humid air correction is applied to the pressure-condition volumetric flow rate obtained from the real-time volumetric flow rate through the gas state equation. Specifically, the difference between the real-time compressed air pressure and the water vapor partial pressure is calculated to obtain the dry air partial pressure. The ratio of the real-time compressed air pressure to the dry air partial pressure is then used as the humid air volume correction coefficient, multiplied by the pressure-condition volumetric flow rate to obtain the actual delivery volumetric flow rate. This correction mechanism considers the physical reality that water vapor occupies a portion of the pressure in humid air, causing the actual delivery volume of dry air to be less than the condition volume. Therefore, based on the ratio of the pipeline's physical volume to the actual delivery volumetric flow rate, the true transmission lag time of compressed air from the air compressor outlet to the end-user point is accurately calculated. This avoids the technical bias of overestimating the actual delivery capacity and underestimating the transmission lag time due to ignoring the water vapor partial pressure. It improves the calculation accuracy of the lag time under humid conditions or dew point fluctuations, providing an accurate time reference for the subsequent forward-looking control of the target compensation flow rate. Ultimately, this achieves the adaptability and reliability of air compressor data control in complex humid air environments.

[0017] 3. When the predicted pressure drop during the lag period exceeds the critical venting threshold of the pipeline network, it indicates that the sudden drop in current pressure may lead to the risk of venting at the end of the pipeline network. By introducing the ratio of the transmission lag time to the historical gas consumption cycle time to construct the lag response ratio, an overshoot attenuation coefficient is generated to dynamically suppress the linear initial compensation flow. This ensures that the compensation intensity matches the lag characteristics of the pipeline network and the periodic pattern of gas consumption at the end of the pipeline network under the scenario of severe pressure fluctuations. This avoids pressure overshoot and system oscillation caused by blind full compensation and improves the control stability and anti-disturbance capability of the air compressor under critical operating conditions. Attached Figure Description

[0018] Figure 1 This is a flowchart illustrating a data control method for an air compressor according to an embodiment of this application; Figure 2 This is a flowchart illustrating the calculation of the target compensation flow in an embodiment of this application; Figure 3 This is a schematic diagram of the structure of a data control system for an air compressor according to an embodiment of this application.

[0019] Explanation of reference numerals in the attached drawings: 301, Central Processing Unit; 302, Read-Only Memory; 303, Random Access Memory; 304, Bus; 305, Input / Output Interface; 306, Input Section; 307, Output Section; 308, Storage Section; 309, Communication Section; 310, Driver; 311, Removable Media. Detailed Implementation

[0020] To enable those skilled in the art to better understand the technical solutions in this specification, the technical solutions in the embodiments of this specification will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of this application, and not all embodiments.

[0021] In the description of the embodiments of this application, the words "for example" or "for instance" are used to indicate examples, illustrations, or explanations. Any embodiment or design that is described as "for example" or "for instance" in the embodiments of this application should not be construed as being more preferred or advantageous than other embodiments or design options. Rather, the use of the words "for example" or "for instance" is intended to present the relevant concepts in a specific manner.

[0022] In the description of the embodiments of this application, the term "multiple" means two or more. For example, multiple systems means two or more systems, and multiple screen terminals means two or more screen terminals. Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the indicated technical features. Thus, a feature defined with "first" or "second" may explicitly or implicitly include one or more of that feature. The terms "comprising," "including," "having," and variations thereof all mean "including but not limited to," unless otherwise specifically emphasized.

[0023] Figure 1 This is a flowchart illustrating a data control method for an air compressor according to an embodiment of this application.

[0024] Please see Figure 1 This application provides a data control method for an air compressor, the method comprising: S101. Obtain the pipeline geometric parameters from the target air compressor to the end air consumption point, the real-time pressure sequence of the end air consumption point, the real-time dew point value and real-time volumetric flow rate of the target air compressor outlet, and the effective adsorption volume parameters of the post-treatment drying equipment. To achieve precise control over the operating status of the target air compressor and avoid a decline in compressed air quality due to blind loading during sudden increases in air consumption, it is necessary to comprehensively collect basic data on system operation. Pipeline geometric parameters are acquired and stored in the parameter library of the centralized controller through a "digital pipeline ledger." This digital pipeline ledger is a structured compilation of as-built drawings, point mapping, and maintenance records of the on-site pipeline network, providing stable geometric boundary conditions for the algorithm and supporting subsequent verification. Pipeline geometric parameters include at least the total length of the pipe section from the target air compressor outlet to the end point of air consumption, the inner diameter of each pipe section, the equivalent length or resistance coefficient of local resistance elements such as elbows and valves, and the identification information of the friction roughness level. The acquisition method can be as follows: During the system debugging phase, maintenance personnel enter the as-built drawing parameters into the human-machine interface of the central controller, and at the same time, conduct a field re-measurement of the key pipe sections. The re-measurement uses laser ranging or tape measure to measure the length, and vernier calipers or nameplates to confirm the pipe diameter. When there are branch merging or ring network structures, the central controller selects a main supply path according to the gas supply path to which the end gas consumption point belongs and records the path identifier. The path identifier is to mark the multi-path pipeline network as several optional gas supply paths using graph theory. When calculating the transmission lag time in the later stage, a certain geometric link is locked, and the complex network is simplified into the main transmission channel corresponding to the control closed loop to reduce the calculation uncertainty.

[0025] The end-point air consumption refers to the final location in the compressed air system where compressed air is actually consumed, i.e., the air outlet connected to specific equipment / tools (such as machine interface, pneumatic tool interface, purging port, etc.). The air compressor's supply capacity and pressure settings must ultimately be based on the needs (flow rate, pressure, quality) of the end-point air consumption, and must also consider pipeline pressure drop and fluctuations to ensure that the end-point air consumption can still meet the requirements under the most unfavorable operating conditions. The real-time pressure sequence of the end-point air consumption is obtained through a pressure transmitter installed on the main pipe or air manifold of the end-point air consumption. The pressure transmitter outputs a 4–20mA or digital signal to the centralized controller. The real-time pressure sequence is time-series data. The centralized controller collects it at a fixed sampling period and buffers it according to the timestamp sequence to form a sliding window. The sliding window provides a continuous data segment for subsequent differential calculation of the pressure change rate. It uses pressure samples from the most recent period to estimate the instantaneous change trend and suppress single-point noise. The sampling period can be set from 0.5s to 2s based on the terminal pressure fluctuation rate. A low-pass filter or median filter is performed at the acquisition end to suppress spikes caused by electromagnetic interference. The filtered data is stored together with the original data for easy traceability and calibration later. To ensure that the pressure sequence corresponds with the dew point and flow rate data under the same time base, the central controller uses a unified clock for all acquisition channels and writes a unified timestamp on each data point.

[0026] The real-time dew point value at the target air compressor outlet is obtained by an online dew point meter installed before the outlet main pipe of the target air compressor or the inlet of the post-treatment drying equipment. The dew point meter outputs the dew point temperature value and periodically uploads it to the central controller. The reason for choosing this installation location is that the dew point value at this location can characterize the moisture content of the compressed air before it enters the post-treatment drying equipment. This allows the current moisture level and drying load to be calculated in subsequent steps using a preset saturated vapor pressure characteristic curve. The preset saturated vapor pressure characteristic curve is a property curve showing the relationship between the saturated vapor pressure of water vapor at different temperatures. It maps the dew point temperature to the corresponding water vapor partial pressure or absolute moisture content. The dew point temperature is defined as the temperature at which the water vapor partial pressure reaches saturation. Using the property curve, a definite relationship can be established between the dew point and the water vapor content. The real-time volumetric flow rate is obtained by a flow meter installed on the outlet pipe of the target air compressor. The flow meter can be a thermal mass flow meter converted to standard condition volumetric flow rate, or a vortex flow meter can be used to directly output the operating condition volumetric flow rate. To ensure consistency with the transmission lag time in subsequent calculations, the centralized controller records the flow reference status simultaneously when receiving real-time volumetric flow rate, including temperature and pressure conversion conditions and correction coefficients. This avoids lag time estimation deviations caused by the same flow rate value under different references. Both dew point values ​​and real-time volumetric flow rates are uploaded with the same or alignable sampling period as the pressure sequence and written into the same data frame using timestamp alignment. This time-correlating of multi-sensor data reduces interpolation errors and provides consistent input for subsequent joint calculations.

[0027] Post-treatment drying equipment is installed after the air compressor to remove moisture / oil mist from compressed air and lower the dew point (common examples include refrigerated dryers, desiccant dryers, and their matching filters). The post-treatment drying equipment determines the final air quality indicators (dew point, oil content, dust content) and introduces a certain pressure drop; therefore, its selection must match the air compressor's flow rate and pressure margin to ensure that the final air quality meets requirements. The effective adsorption volume parameter of the post-treatment drying equipment is determined by the nameplate parameters and operating status of the equipment and input into the centralized controller. The effective adsorption volume parameter indicates the equivalent volume actually involved in the adsorption and dehumidification process under the current drying equipment structure and valve control switching strategy. It is an equivalent calculation of the space in the drying tower, adsorbent bed voids, and flow channels that contribute to adsorption exchange, quantifying the equipment's "available adsorption space" as the volume boundary required for subsequent critical residence time calculations. The residence time is approximately equal to the ratio of the effective adsorption volume parameter to the volumetric flow rate through the drying equipment. A larger volume or smaller flow rate results in a longer contact time between the gas and the adsorbent, leading to more thorough dehumidification. The acquisition method can be as follows: For dual-tower adsorption dryers, the centralized controller reads the current working tower identifier, switching cycle, and bypass valve status reported by the dryer controller, and calculates the basic effective adsorption volume based on the single-tower bed geometry, bed porosity, and flow channel volume provided by the equipment manufacturer. If there is a bypass or some towers are not in use, the centralized controller reduces the effective adsorption volume according to the valve position status. For refrigerated dryers, the equivalent volume of the effective heat exchange and dehumidification channel is used as the implementation form of the effective adsorption volume parameter, and the naming is kept consistent for unifying subsequent formula interfaces. To improve parameter reliability, a single identification and calibration can be performed when the system is first launched: record the dew point change curve under stable flow, back-calculate the equivalent residence time required to achieve the dew point standard, and correct the effective adsorption volume parameter to make the model consistent with the field equipment. The corrected parameter is written into the centralized controller parameter library with a version number, which is used to mark the source of parameter changes after different maintenance cycles or adsorbent replacements.

[0028] After completing the above data acquisition and parameterization, the centralized controller generates a synchronous data stream containing pipeline geometric parameters, real-time pressure sequences at the end-point air consumption points, real-time dew point and volumetric flow rates at the target air compressor outlet, and effective adsorption volume parameters of the post-treatment drying equipment. The benefits of this implementation are: when calculating the transmission lag time of compressed air from the target air compressor outlet to the end-point air consumption point, the pre-defined geometric boundaries and real-time flow rates can be directly utilized; when calculating the target compensation flow rate, a noise-resistant real-time pressure sequence window can be used; and when calculating the maximum allowable loading flow rate, the real-time dew point and effective adsorption volume parameters can be correlated to the same time section. This establishes a consistent data loop between dynamic pressure compensation and dew point quality constraints, improving the real-time performance, stability, and interpretability of control commands, and reducing erroneous flow limiting or loading caused by data asynchrony, missing parameters, or inconsistent benchmarks.

[0029] S102. Based on the pipeline geometric parameters, the real-time dew point value and the real-time volumetric flow rate, calculate the transmission lag time of compressed air from the outlet of the target air compressor to the end point of air consumption. Step S102 is used to characterize the transmission inertia / response delay of compressed air from the target air compressor outlet to the end point of air consumption, so that the difference in effective delivery caused by pipeline filling effect and water vapor content can be incorporated into the control model when performing flow compensation based on end pressure changes. Specifically, it may include steps S1021 to S1024.

[0030] S1021. Calculate the physical volume of the pipeline between the target air compressor and the terminal air consumption point based on the pipeline geometric parameters; In step S1021, the pipeline physical volume is used to characterize the geometric space of compressed air that the pipeline network can accommodate from the outlet of the target air compressor to the end point of air consumption. The pipeline physical volume, together with the subsequently obtained actual delivery volumetric flow rate, determines the magnitude of the transmission lag time. The reason for calculating the pipeline physical volume is that the response of the end point of air consumption pressure to the load change of the target air compressor is not instantaneous. The compressed air output by the target air compressor first enters the pipeline network and "fills" the pipeline network. The larger the gas storage in the pipeline network, the longer it takes for the pressure at the end point of air consumption to reach a new steady state. Using only the real-time volumetric flow rate of the target air compressor without introducing the pipeline physical volume can easily overestimate the immediate effect of the compensation action when the end pressure shows a downward trend, resulting in an overestimation of the target compensation flow rate, causing load fluctuations and amplifying the dew point quality risk. Based on the above understanding, step S1021 uses the obtained pipeline geometric parameters as input to perform geometric modeling and cumulative calculation on all pipe sections and volumetric components between the target air compressor and the end air consumption point to obtain the pipeline physical volume. This provides a unified "denominator benchmark" for the pressure condition volumetric flow conversion in step S1022 and the humid air correction in step S1023, thereby ensuring physical consistency in the transmission lag time in step S102.

[0031] In specific implementation, the pipeline geometric parameters include at least the pipe segment identification, pipe segment length, pipe segment inner diameter or equivalent inner diameter, pipe segment material roughness identification, friction component information, and branch and confluence topology information. Among them, the pipe segment inner diameter is used to determine the cross-sectional area, the pipe segment length is used to determine the friction volume, and the branch and confluence topology information is used to identify the effective set of pipe segments participating in the transmission lag calculation between the target air compressor and the end air consumption point. The calculation of the physical volume of the pipeline follows the principle of geometric volume superposition. The volume of each effective pipe segment is calculated and summed according to the geometric relationship of a cylinder. The volume of a single pipe segment is calculated according to V_i=A_i·L_i. The cross-sectional area A_i is obtained from the inner diameter D_i of the pipe segment, A_i=π·D_i^2 / 4, and then the volume of the pipe segment V_i=A_i·L_i=π·D_i^2·L_i / 4. The physical volume of the pipeline V_pipe=sum(V_i)+sum(V_eq,j) is obtained by summing the volumes of all effective pipe segments, where D_i represents the inner diameter of the i-th pipe segment, L_i represents the length of the i-th pipe segment, and V_eq,j represents the equivalent volume of the j-th volumetric component. When the pipe geometry includes a variable diameter section, the volume of the variable diameter section is calculated as a frustum or a segmented cylinder. The frustum is calculated by using the inner diameters at both ends D_(i,1) and D_(i,2) and the length L_i to obtain V_i=pi·L_i·(D_(i,1)^2+D_(i,1)·D_(i,2)+D_(i,2)^2) / 12, where D_(i,1) and D_(i,2) represent the inner diameters at both ends of the variable diameter section, and L_i represents the length of the variable diameter section. When the pipeline geometry parameters include components with significant internal cavities such as elbows, tees, valve bodies, filter housings, and pressure tanks, a "Volumetric Component Equivalent Volume" field is set in the pipeline geometry parameters, and the corresponding volume is incorporated into the pipeline physical volume. The volumetric component equivalent volume is the internal volume marked in the component product sample or the internal cavity volume obtained through geometric measurement, used to correct the systematic underestimation caused by calculating only based on the cylindrical pipe section. The volumetric component equivalent volume is also required to fill the internal space of the component during the transmission of compressed air. The contribution of the internal cavity of the component to the gas storage is equivalent to adding a straight pipe with the same volume. To avoid invalid accumulation caused by branch pipelines, the branch convergence topology information is used to select the effective path connected to the end air consumption point. When there are multiple parallel paths from the target air compressor to the end air consumption point, the physical volume of the pipeline is weighted according to the effective volume allocation of the parallel paths. The weight depends on the equivalent flow resistance allocation of each path. The equivalent flow resistance is calculated from the length and inner diameter in the pipeline geometry parameters. The purpose is to make the physical volume of the pipeline reflect the path space where compressed air is actually preferentially filled, thereby improving the prediction accuracy of transmission lag time.

[0032] S1022. Obtain the real-time compressed air pressure in the pipeline between the target air compressor and the end air consumption point. Based on the real-time compressed air pressure and the preset gas state equation, convert the real-time volumetric flow rate into the operating condition state corresponding to the real-time compressed air pressure to obtain the pressure operating condition volumetric flow rate. In step S1022, the real-time volumetric flow rate needs to be converted to a working condition consistent with the real-time compressed air pressure in the pipeline between the target air compressor and the end-point air consumption. The purpose is to ensure that the flow rate used for subsequent transmission lag calculations is under the same thermodynamic reference conditions as the pipeline physical volume obtained in step S1021. The real-time volumetric flow rate at the air compressor outlet may come from either the "discharge volume" signal output by the air compressor controller or the "standard volumetric flow rate" signal output by the flow meter. Both are volumetric flow rate expressions under specific reference pressures and temperatures. The filling rate of gas in the pipeline is determined by the actual gas density corresponding to the real-time pressure in the pipeline. The volumetric flow rate corresponding to the same mass flow rate varies significantly under different pressures. Directly using the unconverted real-time volumetric flow rate will lead to an overestimation of the actual delivery capacity at higher pressures, further resulting in an underestimation of the transmission lag time and amplifying the error in the target compensation flow rate calculation in step S103. Therefore, step S1022 obtains the real-time compressed air pressure in the pipeline and introduces a preset gas state equation to complete the working condition conversion, thereby obtaining the pressure working condition volumetric flow rate, which provides the correct reference quantity for the humid air correction in step S1023.

[0033] In practical implementation, the real-time compressed air pressure within the pipeline is obtained using a pressure acquisition link. This link includes a pressure sensor, a signal conditioning module, and a data acquisition module installed on the main pipeline between the target air compressor outlet and the end-point air consumption. When the pressure sensor outputs a gauge pressure signal, the data acquisition module converts the gauge pressure into absolute pressure based on the on-site atmospheric pressure sensor or a preset atmospheric pressure constant, obtaining the real-time compressed air pressure P_pipe(t). The absolute pressure is used for gas state equation calculations to avoid zero-point offset. The preset gas state equation describes the relationship between compressed air pressure, temperature, and volume. This preset gas state equation is a fundamental gas thermodynamic model that unifies volumetric flow rates under different reference conditions to pipeline pressure conditions. In engineering implementation, the preset gas state equation is preferably an ideal gas state equation or a state equation with compressibility factor correction. The ideal gas law, based on the principle P·V = n·R·T, states that for the same amount of gas at a constant temperature, volume and pressure are approximately inversely proportional. Here, P is the absolute pressure of the gas, V is the volume occupied by the gas, n is the amount of substance (mol), directly proportional to the number of gas molecules, R is the universal gas constant, and T is the thermodynamic temperature (K). Compressibility factor corrections are used to compensate for errors in real-world gas calculations at higher pressures, making the conversion results closer to reality.

[0034] The calculation of the pressure condition volumetric flow rate uses the real-time volumetric flow rate Q_out(t) as input and combines it with the real-time compressed air pressure P_pipe(t) and reference state variables for conversion. To facilitate stable implementation within the controller, step S1022 can solidify the reference conditions corresponding to the real-time volumetric flow rate as the standard reference pressure P_ref and the standard reference temperature T_ref, while using the real-time measured temperature T_pipe(t) or a preset operating temperature constant for the pipeline condition temperature. When using the ideal gas equation of state and neglecting the compressibility factor, the conversion of the volumetric flow rate Q_pipe(t) under pressure conditions satisfies the mass conservation relationship and can be written as: Q_pipe(t) = Q_out(t)·(P_ref / P_pipe(t))·(T_pipe(t) / T_ref). When the compressibility factor Z is introduced, the equation of state is written as P·V = Z·n·R·T, and the corresponding conversion form is: Q_pipe(t) = Q_out(t)·(P_ref / P_pipe(t))·(T_pipe(t) / T_ref)·(Z_pipe(t) / Z_ref), where Z_pipe(t) and Z_ref are the compressibility factors for the pipeline condition and the reference condition, respectively. The compressibility factor can be obtained from the pressure and temperature using a preset lookup table function. In order to ensure that the humid air correction in step S1023 can focus on the effect of water vapor partial pressure on volume distribution, the pressure condition volume flow rate output in step S1022 is defined as the volume flow rate that is already consistent with the pipeline pressure conditions before the water vapor partial pressure correction is performed.

[0035] Through the above implementation method, the pressure condition volumetric flow rate obtained in step S1022 is consistent with the real-time compressed air pressure in the pipeline. This means that when calculating the "ratio of pipeline physical volume to actual transport volumetric flow rate" in step S102, the volumetric dimensions under different operating conditions are no longer mixed. The trend of the transmission lag time increasing reasonably with the increase of pressure is reflected. As a result, when calculating the target compensation flow rate based on the pressure change rate in step S103, the terminal pressure response delay can be reflected more accurately, the overshoot and frequent fluctuations of the target air compressor loading command are reduced, and a more reliable comparison benchmark is provided for the flow-limiting and quality-preserving command under the maximum allowable loading flow rate constraint.

[0036] S1023. Determine the current water vapor partial pressure based on the real-time dew point value, and perform humid air correction on the pressure condition volumetric flow rate based on the water vapor partial pressure to obtain the actual delivery volumetric flow rate. The actual delivery volumetric flow rate is used to compensate for the velocity increment caused by the water vapor partial pressure occupying the physical space of the pipeline. Step S1023 is used to incorporate the real-time dew point value of the target air compressor outlet into the flow rate calculation. This is because compressed air in the pipeline is a humid air system, and water vapor occupies a portion of the pipeline's pressure and volume in the form of partial pressure. This causes a discrepancy between the pressure condition volumetric flow rate obtained in step S1022, when interpreted only as "total compressed air," and the actual rate of change of the dry air volume available for filling the pipeline. Specifically, this may include the following steps: calculating the difference between the real-time compressed air pressure and the water vapor partial pressure to obtain the dry air partial pressure; determining the ratio of the real-time compressed air pressure to the dry air partial pressure as a humid air expansion correction factor; and calculating the product of the pressure condition volumetric flow rate and the humid air expansion correction factor to obtain the actual delivery volumetric flow rate.

[0037] The real-time dew point value is used to deduce the partial pressure of water vapor in the compressed air. The partial pressure of water vapor and the partial pressure of dry air together constitute the real-time compressed air pressure in the pipeline. The relationship between the partial pressures comes from Dalton's law of partial pressures, which states that the total pressure of the mixed gas is equal to the sum of the partial pressures of each component, expressed as P_pipe(t) = P_dry(t) + P_vapor(t). Since the pressure-condition volumetric flow rate obtained in step S1022 reflects the volumetric transport capacity of the mixed gas under pipeline pressure, the subsequent calculation of the transmission lag time needs to characterize the "effective volume distribution occupying the physical space of the pipeline". The volume component corresponding to the water vapor partial pressure will squeeze the volume component of dry air. The higher the dew point, the greater the water vapor partial pressure. If the water vapor partial pressure is not separated from the total pressure, it is easy to mistakenly believe that the volume expansion caused by water vapor is an increase in the dry air transport capacity, thus making the actual transport volumetric flow rate too large and the transmission lag time too small. Therefore, in the step of "calculating the difference between the real-time compressed air pressure and the water vapor partial pressure to obtain the dry air partial pressure", the controller reads the real-time compressed air pressure P_pipe(t) in the pipeline formed in step S1022, and at the same time calls the preset saturated vapor pressure characteristic curve to obtain the saturated vapor pressure Psat(Td(t)) based on the real-time dew point value Td(t). P_vapor(t) is defined as Psat(Td(t)) and the difference between P_pipe(t) is calculated to obtain the dry air partial pressure, P_dry(t) = P_pipe(t) - P_vapor(t). The dry air partial pressure makes the pressure share of the total pressure borne by dry air explicit, so that the volume flow rate correction of moist air can be completed based on the pressure share rather than empirical coefficients. When the dew point increases and P_vapor(t) increases, P_dry(t) will decrease synchronously. The model can naturally reflect the hysteresis increase trend caused by the decrease in the "effective driving capacity" of dry air. For example, if P_pipe(t) = 800 kPa and the real-time dew point value corresponds to P_vapor(t) = 2 kPa, then P_dry(t) = 798 kPa. The partial pressure of dry air directly reflects the pressure share occupied by water vapor as 2 kPa.

[0038] After obtaining the partial pressure of dry air, the ratio of the real-time compressed air pressure to the partial pressure of dry air is determined as the wet air expansion correction coefficient. This is used to convert the partial pressure ratio into a multiplicative correction term for the volumetric flow rate. The wet air expansion correction coefficient is an engineering calculation quantity defined to achieve wet air correction. It is a derivation of the state equation under the ideal gas approximation that "under the same temperature and the same mass flow rate, the volumetric flow rate is inversely proportional to the pressure". When the total pressure is kept at P_pipe(t), the actual pressure corresponding to dry air is only P_dry(t). This means that dry air with the same mass flow rate exhibits a larger volumetric occupancy ratio under a lower effective pressure share. The wet air expansion correction coefficient is used to quantify the degree of this "volume amplification". In implementation, the controller calculates the ratio periodically and limits the value range to avoid abnormal amplification caused by sensor noise. K_wet(t) = P_pipe(t) / P_dry(t), where K_wet(t) is defined as the humid air expansion correction coefficient. This coefficient is typically slightly greater than 1. The higher the dew point, the larger P_vapor(t), and the smaller P_dry(t), the larger K_wet(t). The effect is to transfer the influence of dew point changes on the "proportion of dry air per unit volume" into a coefficient that can be directly used for flow rate correction, thereby enabling the control logic to maintain consistent hysteresis estimation accuracy under different humidity conditions. For example, using the aforementioned values, K_wet(t) = 800 / 798 ≈ 1.0025. When the dew point further increases, causing P_vapor(t) to increase, K_wet(t) will increase accordingly.

[0039] After the humid air expansion correction coefficient is formed, the "product of the pressure condition volumetric flow rate and the humid air expansion correction coefficient to obtain the actual delivery volumetric flow rate" is used to output the actual delivery volumetric flow rate that can be directly used in the calculation of the transmission lag time. The actual delivery volumetric flow rate is used to compensate for the velocity increment caused by the water vapor partial pressure occupying the physical space of the pipeline, so that the ratio between the physical volume of the pipeline and the flow rate reflects the true renewal rate of the mixed gas on the pipeline space at the current dew point. In implementation, the controller reads the pressure condition volumetric flow rate Q_pipe(t) from step S1022, multiplies Q_pipe(t) by K_wet(t) to obtain Q_actual(t), Q_actual(t) = Q_pipe(t) * K_wet(t); when the dew point increases, K_wet(t) increases, making Q_actual(t) slightly larger than Q_pipe(t), indicating that under the same quality transportation conditions, the volume occupied by humid air increases due to the proportion of water vapor partial pressure. This is reflected in the corresponding change of transmission lag time in the calculation of "the ratio of pipeline physical volume to actual transportation volumetric flow rate" in step S102. The effect is to avoid omitting the volume change caused by humidity from the lag model, so that the target compensation flow calculation and flow-limiting quality constraint are based on the input quantity that is closer to the actual pipeline filling process. For example, if Q_pipe(t) = 0.270 m^3 / min and K_wet(t) = 1.0025, then Q_actual(t) = 0.270 * 1.0025 ≈ 0.271 m^3 / min. This correction is more significant under conditions of high dew point or lower dry air partial pressure, which helps to maintain a stable and consistent estimation of transmission lag time when the dew point fluctuates.

[0040] S1024. Calculate the ratio of the physical volume of the pipeline to the actual transport volume flow rate to obtain the transmission lag time.

[0041] Step S1024 uses the ratio of "pipeline physical volume to actual delivery volumetric flow rate" to obtain the transmission lag time. This is because the pipeline from the target air compressor outlet to the end-user point can be considered an equivalent volumetric unit that needs continuous filling and replacement by compressed air. Before the end-user pressure responds to changes in air compressor load, it must undergo a gas renewal process within the pipeline. The time scale required for this renewal process is directly proportional to the size of the space to be renewed and inversely proportional to the volume that can be renewed per unit time. The pipeline physical volume comes from the volumetric calculation of the pipeline's geometric parameters in step S1021, representing the space occupied by the effective gas from the target air compressor outlet to the end-user point. The actual delivery volumetric flow rate comes from the result of the pressure-condition volumetric flow rate corrected for wet air in step S1023, representing the equivalent volumetric flow rate entering the pipeline and participating in space renewal per unit time under the combined constraints of real-time compressed air pressure and real-time dew point value within the pipeline. To avoid jitter introduced by sensor noise, the controller performs low-pass filtering or moving average on the actual delivery volumetric flow rate during calculation. The filter window length is matched with the sampling period of the real-time pressure sequence at the end gas consumption point to suppress the amplification effect of instantaneous fluctuations on hysteresis estimation. Simultaneously, a lower limit clamping value Q_min is set for the actual delivery volumetric flow rate. Q_min is the minimum stable gas supply flow rate on site or the minimum measurable flow rate of the equipment. This prevents division by zero and resulting in infinite hysteresis when the air compressor is unloaded or the flow meter approaches zero, which would affect the stable calculation of the subsequent target compensation flow rate. After completing the above preprocessing, the controller performs a ratio calculation periodically to obtain the transmission hysteresis time tau(t), tau(t) = V_pipe / Q_actual,eff(t), where V_pipe represents the physical volume of the pipe, and Q_actual,eff(t) represents the actual delivery volumetric flow rate after filtering and lower limit clamping. When using minute-based flow rate, tau(t) is in minutes; when using second-based flow rate, tau(t) is in seconds. By calculating this ratio, the transmission lag time can adaptively increase or decrease with changes in pipe length and diameter, and dynamically update with changes in actual delivery volumetric flow rate caused by real-time pressure and real-time dew point. This allows step S103 to introduce a propagation delay that better reflects the physical process when judging the drop in terminal pressure and calculating the target compensation flow rate. The effect is that the loading adjustment of the target air compressor is closer to the actual response rhythm when the terminal pressure fluctuates, reducing pressure overshoot caused by premature compensation and reducing the negative impact of frequent loading and unloading on energy consumption and dew point quality. For example, if the pipe geometry parameters calculate the pipe physical volume V_pipe = 2.5 m^3, and the actual delivery volumetric flow rate output in step S1023 is obtained by moving average as Q_actual,eff(t) = 0.50 m^3 / min, then the transmission lag time tau(t) = 2.5 / 0.50 = 5 min. Based on this, the controller aligns the compensation decision corresponding to the terminal pressure change rate with the approximately 5-minute propagation delay, thereby improving the reliability of compensation flow rate estimation and the generation of flow-limiting and quality-preserving commands.

[0042] S103. Differentiate the real-time pressure sequence to obtain the pressure change rate. When the pressure change rate is negative and the absolute value of the pressure change rate is greater than the preset pressure change threshold, calculate the target compensation flow based on the pressure change rate and the transmission lag time. Step S103 calculates the pressure change rate by differentiating the real-time pressure sequence of the terminal gas consumption point. The sign and amplitude of the pressure change rate characterize the downward trend and speed of the terminal pressure. Thus, before the terminal pressure begins to decline rapidly but before the adjustment effect of the target air compressor outlet is transmitted to the terminal, a compensation decision matching the transmission lag time is constructed in advance. A negative pressure change rate with an absolute value exceeding the preset pressure change threshold indicates that the terminal gas consumption point is experiencing a gas consumption shock or insufficient gas supply trend that exceeds the normal fluctuation range. Directly waiting for the pressure closed loop to reach the set lower limit may cause the terminal pressure to drop too deeply due to the dynamic lag of pipelines and equipment. Therefore, step S103 couples the pressure change rate with the transmission lag time obtained in step S102 to predict the amount of pressure drop that may continue within the lag time window, and calculates the target compensation flow rate accordingly. This ensures that the load adjustment of the target air compressor can both cover the response delay caused by the lag and suppress the pressure overshoot caused by overcompensation by combining historical gas consumption cycle characteristics.

[0043] The pressure change rate is obtained by numerically differentiating the real-time pressure sequence P_end(t) at the end gas consumption point according to the sampling period Δt. In engineering implementation, the controller uses differential sampling on adjacent sampling points and anti-noise processing to obtain a stable slope. The typical calculation method is dP / dt(k)=(P_end(k)-P_end(k-1)) / Delta_t. When the pressure sensor noise is large, a moving average can be performed on the real-time pressure sequence or a multi-point differential form dP / dt(k)=(P_end(k)-P_end(km)) / (m*Delta_t) can be used to reduce the interference of occasional spikes on the slope judgment. A negative pressure change rate indicates that the terminal pressure is decreasing, which aligns with the physical direction of energy release in the pipeline network caused by a sudden increase in gas consumption or insufficient gas supply. If the absolute value of the pressure change rate is greater than the preset pressure change threshold, it means that the rate of decrease has exceeded the normal operating fluctuation range. Continuing to wait for the conventional pressure control action to be transmitted to the terminal will be limited by the transmission lag time, resulting in the risk of "pressure dropping significantly before the response arrives". Therefore, under this triggering condition, subsequent target compensation flow calculation is initiated. The pressure change rate is used to characterize the intensity of the decrease and combined with the transmission lag time to predict the pressure drop trend within a short time window. This allows for an advance increase in the load on the target air compressor's gas supply side to offset the impending drop in terminal pressure, while avoiding frequent compensation triggers caused by small fluctuations or false drops due to noise, which could lead to overshoot and increased energy consumption.

[0044] Figure 2This is a flowchart for calculating the target compensation flow rate. The following section will combine... Figure 2 Step S103 will be further explained.

[0045] S201. Calculate the product of the absolute value of the pressure change rate and the transmission lag time to obtain the predicted pressure drop during the lag period; Step S201 couples the pressure change rate with the transmission lag duration to predict the pressure drop during the lag period. The purpose is to extrapolate the observed pressure drop rate at the end-point gas consumption point to the time window before the control action reaches the end point, thereby elevating the risk assessment from an instantaneous slope judgment to a judgment of the pressure drop magnitude over a future period. Under conditions where the sampling period is sufficiently short and the pipeline network status changes relatively smoothly over a short time, the real-time pressure sequence at the end-point gas consumption point can be approximated by the first derivative. The absolute value of the pressure change rate represents the pressure drop rate per unit time, and the transmission lag duration represents the propagation delay length of the perceptible impact of the target air compressor outlet regulation on the end-point pressure. Multiplying the two yields the expected pressure drop magnitude within the lag time window. In specific implementation, after the controller has obtained the pressure change rate dP / dt in step S103 and completed the trigger judgment that "the pressure change rate is negative and the absolute value is greater than the preset pressure change threshold", it reads the transmission lag time τ output in step S1024, takes the absolute value of the pressure change rate to form a positive pressure drop rate v_P=|dP / dt|, and then performs a multiplication operation to obtain the predicted pressure drop ΔP_pred=v_P×τ. To ensure dimensional consistency, the controller standardizes the pressure change rate to kPa / s or kPa / min and the transmission lag time to s or min. Before calculation, a moving average slope matching the sampling period of the real-time pressure sequence is applied to the pressure change rate to suppress noise spikes and prevent artificially high predicted pressure drop during the lag period caused by a single abnormal sampling. The predicted pressure drop during the lag period serves as the input for subsequent threshold branch judgments, comparing it with the preset critical venting threshold of the pipeline network. This characterizes the potential pressure drop at the end of the pipeline within the time range covered by the transmission lag time, thereby determining whether the target compensation flow rate should be compensated directly linearly or conservatively by incorporating the historical gas usage cycle duration and the overshoot attenuation coefficient. The effect is that, under the same instantaneous pressure drop rate, pipelines with longer transmission lag times are identified as having a higher risk of pressure drop and trigger a stronger compensation strategy earlier, while pipelines with shorter transmission lag times avoid overcompensation that could lead to pressure overshoot and frequent loading. For example, if the pressure change rate at the end gas point is calculated to be −3 kPa / min and the transmission lag time is calculated to be 4 min, then the predicted pressure drop during the lag period is |−3|×4=12 kPa. Based on this, the controller enters the comparison process with the preset critical venting threshold of the pipeline network, providing a quantitative basis for the subsequent calculation of the target compensation flow rate.

[0046] S202. If the predicted pressure drop during the lag period is greater than the preset critical venting threshold of the pipeline network, then the linear initial compensation flow rate is calculated based on the pressure change rate, and the historical gas consumption cycle duration of the terminal gas consumption point is obtained. Step S202 is initiated when the predicted pressure drop during the lag period exceeds the preset critical venting threshold of the pipeline network. This is because the predicted pressure drop during the lag period indicates a significant pressure drop at the end-point gas consumption point within the time window covered by the transmission lag, rapidly depleting the effective gas storage in the pipeline network and approaching the "venting risk." Continuing to use mild compensation could easily lead to the end-point pressure falling below the process lower limit or even triggering false alarms in the gas-consuming equipment. The preset critical venting threshold of the pipeline network is derived from the on-site calibration of the minimum acceptable pressure margin of the pipeline network. It distinguishes between the situation of "requiring a rapid increase in gas supply capacity" and the situation of "allowing natural decline followed by compensation," representing the pressure margin with a comparable pressure drop threshold, thereby converting the predicted pressure drop into an executable compensation strategy switching condition. In specific implementation, after obtaining the predicted pressure drop ΔP_pred during the lag period in step S201, the controller compares the predicted pressure drop with the preset critical venting threshold ΔP_crit of the pipeline network. When ΔP_pred > ΔP_crit, the process of calculating the linear initial compensation flow and obtaining the historical gas consumption cycle duration begins. The linear initial compensation flow is an intermediate variable that provides a "benchmark compensation amount" for the subsequent target compensation flow. The term "linear" in the name indicates that the compensation amount and the pressure change rate adopt a linear mapping relationship at this stage. The mapping relationship converts the rate of pressure drop at the end into the magnitude of the additional gas supply flow, avoiding compensation lag caused by relying solely on the pressure setpoint error. The mapping relationship is based on a small disturbance model where the pipeline network is approximately linear in the short term. The faster the pressure drops, the larger the flow gap on the gas consumption side, and the compensation flow should be increased proportionally. In engineering, the controller can use a calibration gain K_q to map the absolute value of the pressure change rate to a flow compensation amount, forming a linear initial compensation flow rate Q_lin = K_q × |pressure change rate|, where K_q is the joint calibration of the equivalent volume of the pipeline network, the range of the terminal pressure sensor, and the loading characteristic curve of the target air compressor. This ensures the controllability of the compensation amplitude under different pipe diameters and air compressor specifications. To ensure the correct compensation direction, the absolute value of the pressure change rate is taken before entering the calculation, ensuring that the linear initial compensation flow rate is non-negative. Subsequently, the upper-level logic superimposes the compensation onto the air supply side setpoint of the target air compressor. Synchronous with the linear initial compensation flow rate, step S202 obtains the historical air consumption cycle duration of the terminal air consumption point to characterize the periodic scale of air consumption fluctuations, providing a time reference for the subsequent hysteresis response ratio and overshoot attenuation coefficient, thereby achieving a combined control of "rapid compensation first, then periodic overshoot suppression" in high venting risk scenarios. The duration of historical gas consumption cycles can be obtained by periodic identification of the real-time pressure sequence or equivalent gas flow sequence of the end gas consumption point. The controller saves the real-time pressure sequence within the most recent time window. The time window length can be the coverage length of multiple potential cycles, such as 10 minutes to 60 minutes. Then, the time interval between adjacent pressure valley values ​​is extracted as candidate cycles using the zero-crossing method or the peak-valley interval method. The median or weighted average of the candidate cycles is then used to obtain the duration of historical gas consumption cycles, T_hist.The peak-valley interval method is a statistical estimation of the interval between repetitive events in periodic signal processing, designed to mitigate misjudgments of a single cycle caused by occasional spikes. Periodic gas consumption forms an approximately repetitive decline-recovery pattern on the pressure curve, and the valley interval reflects the main gas consumption cycle. After completing the above calculations, the linear initial compensation flow rate and the historical gas consumption cycle duration are output together to subsequent steps to construct the hysteresis response ratio and generate an overshoot attenuation coefficient. This ensures timely gas supply increases in high-risk pressure drop scenarios while reducing pressure rebound, frequent loading, and increased energy consumption caused by overcompensation when gas consumption fluctuations are clearly periodic. For example, if the pressure change rate is measured to be −4 kPa / min, the transmission hysteresis duration is 3 min, the predicted pressure drop during the hysteresis period is 12 kPa, and the preset critical venting threshold for the pipeline is set to 10 kPa, the controller will operate at the calibrated gain K_q = 0.15 (m) after the over-threshold condition is met. 3 The linear initial compensation flow rate is calculated using the formula (kPa / min) / (kPa / min), yielding Q_lin = 0.15 × 4 = 0.6 m³. 3 / min, and at the same time, in the real-time pressure sequence of the most recent 30 minutes, the interval of continuous valley values ​​is concentrated around 6 minutes, and the historical gas consumption cycle duration T_hist=6min is obtained, which provides input for the subsequent calculation of hysteresis response ratio and overshoot attenuation coefficient.

[0047] S203. Calculate the ratio of the transmission lag time to the historical gas consumption cycle duration to obtain the lag response ratio; Step S203 calculates the lag response ratio by comparing the transmission lag time with the historical gas consumption cycle duration. The purpose is to quantify the relative magnitude of the "control action propagation delay" with respect to the "gas consumption fluctuation cycle" using a dimensionless index, thus providing a direct basis for the subsequent calculation of the overshoot attenuation coefficient. The transmission lag time reflects the dynamic propagation time of compressed air from the target air compressor outlet to the end gas consumption point, while the historical gas consumption cycle duration reflects the main periodic scale of load changes at the end gas consumption point. A larger proportion of the transmission lag time in the historical gas consumption cycle duration means that when the load change of the target air compressor reaches the end, the gas consumption side may have already entered the next fluctuation phase, making compensation actions more prone to phase mismatch and causing pressure rebound or overshoot. Conversely, a smaller proportion means that compensation actions can be effective within the same gas consumption fluctuation phase, and the risk of overshoot is relatively low. Based on this understanding, step S203 uses a ratio method to unify the two time characteristics to the same scale, avoiding the problem of incompatibility of thresholds for different factory pipeline scales and different gas consumption cycles caused by using only absolute time. In specific implementation, the controller has already obtained the historical gas consumption cycle duration T_hist in step S202, and the transmission lag duration τ in step S102. The controller first performs unit consistency processing, unifying τ and T_hist to seconds or minutes, and applies boundary constraints to outliers to ensure the stability of the ratio calculation. The historical gas consumption cycle duration may be too small when the gas consumption cycle changes or data is missing, leading to an abnormally amplified ratio. In engineering implementation, a minimum cycle protection value T_min can be set. T_min is an empirical lower limit of the terminal pressure sampling cycle and the actual production cycle, which is to avoid the historical gas consumption cycle duration approaching zero and causing numerical divergence. The controller updates the cycle duration used for calculation to T_use=max(T_hist,T_min). After completing the above processing, the controller performs a ratio calculation to obtain the lag response ratio R_lag=τ / T_use. The lag response ratio is a dimensionless quantity. A larger value indicates a higher proportion of transmission lag time to the historical gas consumption cycle time, and a more "lag-dominated" system dynamic. A smaller value indicates a more "fast response" system dynamic. The lag response ratio serves as the input for the overshoot attenuation coefficient in subsequent steps, enabling the linear initial compensation flow to automatically attenuate in scenarios with a high lag ratio, reducing pressure overshoot caused by the misalignment of compensation reaching the end with gas consumption fluctuations. Simultaneously, it maintains the compensation intensity in scenarios with a low lag ratio to improve the end-pressure recovery speed. The final effect is that the compensation strategy can adaptively adjust under different pipeline lengths and different production cycle conditions, eliminating the need for repeated manual parameter adjustments for each pipeline.For example, the transmission lag time is calculated to be 4 minutes, and the historical gas consumption cycle time is identified to be 8 minutes. After the units are consistent, the lag response ratio R_lag=4 / 8=0.5 is calculated. The lag response ratio represents that the control action needs to cross half a gas consumption cycle to reach the end. The subsequent overshoot attenuation coefficient will be attenuated according to the proportion of 0.5 to the linear initial compensation flow, thereby reducing the probability of compensation overshoot while the end pressure drops rapidly.

[0048] S204. Calculate the overshoot attenuation coefficient based on the hysteresis response ratio, and determine the target compensation flow rate by multiplying the linear initial compensation flow rate by the overshoot attenuation coefficient. After obtaining the hysteresis response ratio, step S204 introduces an anti-overshoot attenuation mechanism to adaptively correct the linear initial compensation flow. The core purpose is to simultaneously satisfy the constraints of "rapidly compensating for pressure drop" and "avoiding overshoot caused by hysteresis". The hysteresis response ratio represents the proportion of transmission hysteresis time to the historical gas consumption cycle duration. The larger the hysteresis response ratio, the more likely the compensation action is to mismatch the phase of gas consumption fluctuation when it reaches the end gas consumption point. Simply using the linear initial compensation flow can easily lead to the continued addition of gas supply when gas demand has already fallen, causing end pressure rebound or even overshoot. Therefore, step S204 calculates the anti-overshoot attenuation coefficient based on the hysteresis response ratio and uses the anti-overshoot attenuation coefficient as the proportional coefficient of the linear initial compensation flow for attenuation. This transforms the linear strategy of "compensating according to the pressure drop intensity" into a dynamic strategy of "adjusting the compensation intensity according to the relationship between hysteresis and cycle". The product of the linear initial compensation flow and the anti-overshoot attenuation coefficient is determined as the target compensation flow. Because the overshoot attenuation coefficient needs to further distinguish whether there is a risk of reverse superposition with the gas consumption decline phase when the compensation reaches the end, and if the risk exists, the attenuation magnitude should be constrained in conjunction with the dew point margin. This may include the following steps: The fractional part of the hysteresis response ratio is determined as the periodic synchronization deviation. If the periodic synchronization deviation does not fall into the preset reverse superposition risk zone, the overshoot prevention attenuation coefficient is calculated based on the preset standard attenuation curve. The preset reverse superposition risk zone is used to characterize the risk range where the compensation flow arrives at the end of the transmission lag just in time to coincide with a decrease in gas demand. If the periodic synchronization deviation falls into the preset reverse superposition risk zone, the ratio of the real-time dew point value to the preset limit dew point threshold is calculated to obtain the dew point penalty weight. The product of the periodic synchronization deviation and the dew point penalty weight is calculated to obtain the initial attenuation amount. The dynamic clamping attenuation amount is determined based on the initial attenuation amount and the preset maximum allowable attenuation threshold. The difference between the preset reference attenuation coefficient and the dynamic clamping attenuation amount is determined as the overshoot prevention attenuation coefficient.

[0049] In the specific implementation process, the fractional part of the hysteresis response ratio is determined as the periodic synchronization deviation. After the controller obtains the hysteresis response ratio R_lag=τ / T_hist in step S203, it splits R_lag into an integer part and a fractional part, and records the fractional part as the periodic synchronization deviation ϕ. The reason for using the fractional part is that the integer part represents the number of times the compensation action crosses the complete gas consumption cycle when it reaches the end of the gas consumption point. Crossing the entire cycle will not change the phase relationship, while the fractional part directly describes "which segment within a cycle" is crossed, which can be used to determine whether the compensation is closer to the rising or falling segment of gas consumption when it reaches the end. Specifically, R_lag is rounded to obtain ⌊R_lag⌋, and ϕ=R_lag−⌊Rlag⌋ is calculated to obtain the periodic synchronization deviation with a value range of [0,1). The periodic synchronization deviation maps the transmission hysteresis time to the phase offset within the gas consumption cycle. The phase position can be obtained by dividing the "delay time" by the "cycle time" and taking the remainder. A cycle synchronization deviation closer to 0 indicates greater synchronization between the compensation reaching the end of the current gas consumption cycle and the start of the current cycle; a deviation closer to 0.5 indicates closer to a half-cycle phase misalignment; and a deviation closer to 1 indicates closer to the start of the next cycle. For example, with a transmission lag of 4 minutes and a historical gas consumption cycle duration of 6 minutes, R_lag = 0.666, and a cycle synchronization deviation ϕ = 0.666. This indicates that the compensation reaches its end in the latter part of the current gas consumption cycle, potentially overlapping with a gas consumption decline.

[0050] When the periodic synchronization deviation does not fall into the preset reverse superposition risk zone, during the calculation of the overshoot attenuation coefficient based on the preset standard attenuation curve, the controller receives the periodic synchronization deviation ϕ and performs interval determination between ϕ and the preset reverse superposition risk zone. The preset reverse superposition risk zone is derived from the statistical calibration of the historical pressure sequence and gas consumption cycle of the terminal gas consumption point, marking the phase interval where "compensation is more likely to arrive at the end of the gas consumption phase when gas demand is decreasing." When the phase of compensation arriving at the end falls near the decreasing segment, the increase in gas supply and the decrease in demand will form a reverse superposition, causing unnecessary rebound in terminal pressure. In engineering implementation, the preset reverse superposition risk zone can be set as a continuous interval [ϕ_d1, ϕ_d2] or multiple sub-intervals. The controller determines whether ϕ falls into this interval through comparison calculation. When ϕ does not fall into the preset reverse superposition risk zone, it indicates that the arrival of compensation at the end of the gas consumption phase is offset from the decreasing segment of gas demand, and the overshoot risk is controllable. The controller calls the preset standard attenuation curve f(ϕ) to calculate the overshoot attenuation coefficient α=f(ϕ). The preset standard attenuation curve is a "phase deviation-overshoot sensitivity" mapping obtained from step load tests or simulations of typical pipe networks during the commissioning phase. Without introducing additional quality constraints, it only smoothly attenuates the linear initial compensation flow based on the degree of phase mismatch. The greater the phase deviation from the synchronization point, the more likely the compensation is to lag behind the actual demand, thus requiring a more conservative compensation ratio to suppress dynamic overshoot of the end pressure. For example, the preset reverse superposition risk zone is set to [0.55, 0.85]. The cycle synchronization deviation ϕ = 0.30 does not fall within this range. The preset standard attenuation curve gives f(0.30) = 0.92, and the controller obtains an anti-overshoot attenuation coefficient α = 0.92, meaning that the linear initial compensation flow retains 92% of its strength to balance response speed and stability.

[0051] When the periodic synchronization deviation falls into the preset reverse superposition risk zone, the controller calculates the dew point penalty weight by comparing the ratio of the real-time dew point value to the preset limit dew point threshold. After determining that ϕ falls into the preset reverse superposition risk zone, the controller no longer relies solely on phase for attenuation. Instead, it introduces the quality constraint information of the real-time dew point value to generate the dew point penalty weight w, which expresses the need for a more conservative attenuation strategy when the air drying margin is insufficient. This is because compensation actions within the reverse superposition risk zone are more prone to causing pressure rebound. If the dew point is also close to the limit, blindly increasing the air supply flow will shorten the equivalent residence time of the post-treatment drying equipment and amplify the risk of dew point exceeding the limit. The control strategy needs to explicitly incorporate quality risk into the attenuation calculation. The specific approach involves reading the real-time dew point value D at the outlet of the target air compressor and comparing it with a preset limit dew point threshold D_lim. The preset limit dew point threshold represents the upper limit requirement for the moisture content of compressed air or a guarantee indicator from the equipment manufacturer for post-treatment drying equipment, serving as the boundary where the dew point cannot deteriorate further. The controller calculates the dew point penalty weight w = D / D_lim and imposes boundary constraints on w at the implementation level to avoid weight distortion caused by abnormal data, for example, limiting w to the range [0, 1.5]. The dew point penalty weight uses a normalized ratio to express the degree to which the dew point approaches the limit as a dimensionless coefficient. A larger w indicates that the dew point is closer to the limit or even close to exceeding the standard, requiring stronger subsequent decay to reduce the decrease in residence time caused by loading. A smaller w indicates sufficient dew point margin, meaning that even in the reverse superposition risk zone, there is no need to excessively sacrifice pressure response.

[0052] In the process of obtaining the initial attenuation amount by multiplying the periodic synchronization deviation and the dew point penalty weight, the controller calculates the initial attenuation amount δ_0 = ϕ × w through a product operation after obtaining the periodic synchronization deviation and the dew point penalty weight. The reason for using the product form is to couple and amplify the "degree of phase being in the reverse superposition risk zone" and the "degree of dew point quality margin tension": when ϕ is large, it means that the compensation reaches the end closer to the end of the descent segment or deeper into the risk zone, and the overshoot sensitivity is higher; when w is large, it means that the quality risk of the post-treatment drying equipment is higher. When both factors increase simultaneously, the attenuation needs to be significantly increased. The product can generate a larger initial attenuation amount when both factors are high, while keeping the initial attenuation amount from being excessively amplified when either factor is low. The initial attenuation amount serves as a candidate value for the subsequent dynamic clamping attenuation amount. The two dimensionless factors are combined into a single dimensionless attenuation amplitude recommendation value, so that the anti-overshoot attenuation coefficient can respond to both phase risk and dew point risk simultaneously. In engineering implementation, the controller can perform renormalization of ϕ within the risk zone to improve sensitivity. For example, ϕ within the risk zone [ϕ_d1, ϕ_d2] can be mapped to ϕ′=(ϕ−ϕ_d1) / (ϕ_d2−ϕ_d1), and then δ_0=ϕ′×w can be calculated. This renormalization makes the initial attenuation continuous at the entrance of the risk zone and more sensitive at the depth of the risk zone, mapping the interval length to [0,1] to unify the scale. For example, if the preset reverse superposition risk zone is [0.55, 0.85], the period synchronization deviation ϕ=0.70 is mapped to ϕ′=(0.70−0.55) / (0.30)=0.50, the dew point penalty weight w=0.95, and the initial attenuation δ_0=0.475, it means that approximately 0.475 of the attenuation amplitude should be deducted from the baseline attenuation coefficient before entering the next clamping constraint.

[0053] After obtaining the initial attenuation amount, a preset maximum allowable attenuation threshold is introduced as an upper limit constraint based on the initial attenuation amount obtained by the combined effect of the period synchronization deviation and the dew point penalty weight. The final output dynamic clamping attenuation amount is selected by comparing the initial attenuation amount with the threshold. Specifically: if the initial attenuation amount is greater than the preset maximum allowable attenuation threshold, the maximum allowable attenuation threshold is determined as the dynamic clamping attenuation amount; if the initial attenuation amount is less than or equal to the preset maximum allowable attenuation threshold, the initial attenuation amount is determined as the dynamic clamping attenuation amount.

[0054] The controller uses the initial attenuation amount as the input of the desired attenuation amplitude, and simultaneously reads the preset maximum allowable attenuation threshold δ_max. This preset maximum allowable attenuation threshold is jointly calibrated based on the target air compressor's controllable loading range, the minimum allowable pressure margin at the terminal, and the minimum effectiveness requirement of the compensation strategy. It is used to limit the upper limit of the attenuation amplitude, preventing excessive attenuation that could lead to excessive weakening of the target compensation flow and thus fail to prevent further decline in terminal pressure. When δ_0 > δ_max, the dynamic clamping attenuation amount δ is set to δ_max; when δ_0 ≤ δ_max, the dynamic clamping attenuation amount δ is set to δ_0. The term "dynamic" in the name of the dynamic clamping attenuation amount comes from the real-time update of δ as the periodic synchronization deviation and dew point penalty weight change. "Clamping" comes from the mathematical operation of applying an upper limit to the attenuation amplitude. This enhances the overshoot suppression capability as the risk increases, while ensuring that the compensation action retains the necessary strength to maintain the safety boundary of the terminal pressure. The effect is that even when extreme adverse superposition risks and dew point margins are simultaneously strained, the attenuation will not increase indefinitely, leading to "compensation failure," and the control strategy maintains interpretable and debuggable stability. For example, if the initial attenuation δ_0 = 0.475 and the preset maximum allowable attenuation threshold δ_max = 0.35, the comparison result satisfies δ_0 > δ_max, and the dynamic clamp attenuation δ is clamped to 0.35, thereby avoiding excessive reduction of the subsequent overshoot attenuation coefficient.

[0055] After obtaining the dynamic clamping attenuation amount, the controller reads the preset baseline attenuation coefficient α_base. This preset baseline attenuation coefficient is the empirically optimal setting or experimental tuning result for the pipeline network under moderate hysteresis and moderate fluctuation conditions. It serves as the default starting point for overshoot attenuation, ensuring a basic overshoot suppression capability even in the absence of risk triggers. By reserving a certain compensation margin at a fixed ratio, the aggressiveness of the compensation action on pressure dynamics is reduced. The controller calculates the overshoot attenuation coefficient α = α_base − δ and imposes effective range constraints on α to ensure the physical feasibility of multiplicative compensation. For example, α is limited to the interval [α_min, 1]. α_min is the minimum allowable compensation retention ratio of the system, preventing negative attenuation coefficients or excessive attenuation that could lead to a reversal of the compensation direction. This is a feasible domain constraint of the control coefficient. After the calculation is completed, the overshoot attenuation coefficient is used in step S204. The linear initial compensation flow rate is multiplied by the overshoot attenuation coefficient to obtain the target compensation flow rate. This allows the target compensation flow rate to automatically decrease within the reverse superposition risk zone to suppress terminal pressure overshoot. Furthermore, it is further conservative when the dew point approaches its limit to reduce the impact on the residence time of the post-treatment drying equipment. The overall effect is smoother terminal pressure fluctuations, less compressor vibration, and more stable dew point compliance rate. For example, with a preset baseline attenuation coefficient α_base = 0.90 and a dynamic clamping attenuation δ = 0.35, the overshoot attenuation coefficient α = 0.55 is obtained. If the linear initial compensation flow rate is 0.60 m³ / s... 3If the flow rate is / min, then the target compensation flow rate becomes 0.33 m³ / min. 3 / min, the compensation intensity is significantly reduced to avoid pressure rebound caused by reverse superposition, while retaining positive compensation capacity to prevent the end pressure from continuing to deteriorate.

[0056] S205. If the predicted pressure drop during the lag period is less than or equal to the critical venting threshold of the pipeline network, then the linear initial compensation flow rate is determined as the target compensation flow rate.

[0057] The preset critical venting threshold for the pipeline network is derived from the calibration results of the pipeline network's operational safety boundary. Calibration can be achieved by using drop tests of the terminal pressure under different operating conditions or by regressing historical operating data to obtain the correspondence between "pressure drop" and "terminal gas supply availability." The preset critical venting threshold serves as the trigger boundary for determining whether the pipeline network has entered a "critical venting" trend. Critical venting occurs when the pressure drop accumulates to a certain level within the transmission lag window, and the compressible gas reserves in the pipeline are insufficient to cover the instantaneous gas demand at the terminal. This leads to an accelerated pressure drop at the terminal, triggering a greater risk of compensation and overshoot. When the predicted pressure drop during the lag period is less than or equal to the preset critical venting threshold, the controller determines that the pipeline network is still within the buffer zone. The accumulated pressure drop caused by the transmission lag has not yet reached the level required to trigger a strong suppression strategy. Continuing to calculate the lag response ratio, periodic synchronization deviation, and anti-overshoot attenuation coefficient will lead to unnecessary compensation weakening and may even prolong the terminal pressure recovery time. Therefore, step S205 adopts a direct-through strategy to directly determine the linear initial compensation flow as the target compensation flow. The linear initial compensation flow rate is a linear mapping relationship based on the pressure change rate. This mapping relationship can be achieved by the proportional gain or empirical coefficient built into the controller. The linear initial compensation flow rate is used to quickly provide feedforward compensation for the current negative pressure change trend. The linear mapping treats the pressure drop rate as a representation of the demand gap; the greater the drop rate, the greater the gap per unit time. Accordingly, increasing the compensation flow rate can replenish the pipeline pressure more quickly. The specific implementation of step S205 is that when the judgment condition is met, the controller no longer calls the calculation link of "calculating the overshoot attenuation coefficient based on the hysteresis response ratio," but directly performs the assignment operation to make the target compensation flow rate equal to the linear initial compensation flow rate. The target compensation flow rate is then output to the subsequent maximum allowable loading flow rate constraint link to ensure that the compensation action still accepts the quality constraint corresponding to the "flow limiting and quality assurance command." The effect of adopting step S205 is that when the pipeline network is not close to the critical emptying state, the target compensation flow maintains sufficient response strength, and the terminal pressure can stop falling and rise more quickly within the transmission lag window. At the same time, it avoids the additional attenuation caused by the introduction of periodic synchronization deviation and reverse superposition risk zone in low-risk scenarios, reduces the excessive conservatism of the control strategy under small fluctuation conditions, and thus takes into account both the stability of terminal pressure and the control efficiency.

[0058] S104. Based on the real-time dew point value and the preset saturated vapor pressure characteristic curve, calculate the critical residence time of the compressed air in the post-treatment drying equipment to meet the preset dew point qualification conditions, and determine the maximum allowable loading flow rate of the target air compressor at the current moment according to the ratio of the effective adsorption volume parameter to the critical residence time. Step S104 is used to convert the dew point compliance requirement into the upper limit of the target air compressor's load. The controller reads the real-time dew point value at the outlet of the target air compressor and converts the dew point into the water vapor saturation partial pressure using a preset saturated vapor pressure characteristic curve. The preset saturated vapor pressure characteristic curve is a calibration or standard fitting of the thermodynamic characteristics of water vapor, establishing a calculable correspondence between dew point and water vapor partial pressure, which is the water vapor partial pressure under saturated conditions corresponding to the dew point. The controller then uses the target state corresponding to the preset dew point compliance condition as a benchmark to calculate the minimum residence time required for compressed air to decrease from the current humidity level to the compliance level in the post-treatment drying equipment. The minimum residence time is defined as the critical residence time, which characterizes the minimum processing time required to ensure the dew point compliance. Finally, the controller determines the maximum allowable loading flow rate based on the ratio of the effective adsorption volume parameter to the critical residence time, thereby improving the air supply response while avoiding excessive processing volume that leads to dew point non-compliance. Specifically, this may include the following steps: Based on the preset saturated vapor pressure characteristic curve, the current saturated water vapor partial pressure corresponding to the real-time dew point value and the target saturated water vapor partial pressure corresponding to the preset dew point qualification conditions are determined respectively. Calculate the difference between the current saturated water vapor partial pressure and the target saturated water vapor partial pressure to obtain the water vapor partial pressure difference that needs to be removed; Obtain the adsorption rate constant of the post-treatment drying equipment, and calculate the ratio of the partial pressure difference of water vapor to be removed to the current saturated water vapor partial pressure to obtain the relative humidity removal rate; A logarithmic decay model is constructed based on the relative humidity removal rate and the adsorption rate constant. The critical residence time is obtained by inversely solving the logarithmic decay model.

[0059] In practice, the controller reads the real-time dew point value at the outlet of the target air compressor and the target dew point value corresponding to the preset dew point qualification conditions. Both are used as query variables input into the preset saturated vapor pressure characteristic curve to obtain the current saturated water vapor partial pressure and the target saturated water vapor partial pressure. The preset saturated vapor pressure characteristic curve is derived from standard data tables or empirical formula fitting results of water vapor thermodynamic properties. It converts the dew point, a temperature-based quantity, into the water vapor partial pressure, a pressure-based quantity that can be used for mass transfer kinetic calculations. The conversion principle lies in the fact that the dew point temperature is defined as the state point at which water vapor reaches saturation, and each state point corresponds to a unique saturated water vapor partial pressure. The controller can implement this using either a lookup table interpolation method or a fitting function for direct calculation. The lookup table interpolation method maps the dew point value to the saturated water vapor partial pressure of adjacent temperature nodes and linearly interpolates to obtain the current and target saturated water vapor partial pressures. The fitting function method directly substitutes the dew point value into the function to output the partial pressure. Both methods ensure that the partial pressure changes monotonically with the dew point, facilitating the subsequent characterization of demand intensity using the "partial pressure difference." Through this pressure-division process, the drying load of the post-treatment drying equipment is quantified into a calculable water vapor driving force index, establishing a unified dimensional basis for the inverse calculation of the critical residence time.

[0060] The controller inputs the current saturated water vapor partial pressure and the target saturated water vapor partial pressure into the difference calculation unit, and performs a subtraction operation to obtain the water vapor partial pressure difference to be removed. The water vapor partial pressure difference to be removed is an engineered representation of the difference between the "current humidity state" and the "qualified humidity state" using the same physical quantity. It serves as a quantitative indicator of the drying target and as a driving force for the subsequent adsorption kinetic model. A higher water vapor partial pressure indicates a higher water vapor content in the gas. When the target saturated water vapor partial pressure is lower than the current saturated water vapor partial pressure, the difference corresponds to the reduction in water vapor partial pressure that needs to be removed by the post-treatment drying equipment. The controller incorporates boundary constraints to prevent measurement noise from causing negative differences. Specifically, when the current saturated water vapor partial pressure is less than or equal to the target saturated water vapor partial pressure, the water vapor partial pressure difference to be removed is clamped to zero, and the critical residence time is set to zero or the minimum residence time of the equipment, thus ensuring that the model input meets physical feasibility. Through this difference calculation, the removal task that the post-treatment drying equipment needs to complete is converted into a single scalar, facilitating the use of a unified model to inversely calculate the minimum residence time required to meet the preset dew point qualification conditions.

[0061] The controller reads the adsorption rate constant from the equipment parameter table, factory calibration documents, or on-site tuning results of the post-treatment drying equipment, and calculates the relative humidity removal rate by correlating the adsorption rate constant with the partial pressure difference of water vapor to be removed and the current saturated water vapor partial pressure. The adsorption rate constant is an engineering model result that normalizes the equivalent removal rate of water vapor by the drying medium using a single constant. It incorporates equipment capacity into the critical residence time calculation, so that the same dew point load yields different minimum residence times on different post-treatment drying equipment. The adsorption process can be approximated as a first-order decay kinetic within a certain operating range, and the decay rate is determined by the rate constant. The relative humidity removal rate is a normalized expression of the "proportion to be removed". It eliminates the influence of partial pressure dimensions and ensures that the model input falls within a stable range of 00 to 11. The partial pressure difference of water vapor to be removed is divided by the current saturated water vapor partial pressure to obtain the removal ratio relative to the current humidity level. In implementation, the controller can limit the relative humidity removal rate to [0,1) to avoid the ratio being greater than or equal to 1 due to excessively low target saturated water vapor partial pressure or sensor malfunction, which could cause divergence in the logarithmic solution. By introducing the adsorption rate constant and the relative humidity removal rate, the subsequent logarithmic decay model includes both the removal target intensity and the equipment removal capacity, and the critical residence time calculation is portable and tunable.

[0062] The controller substitutes the relative humidity removal rate and adsorption rate constant into a first-order logarithmic decay model to inversely calculate the minimum time required to meet the preset dew point qualification condition. The inverse calculation result is defined as the critical residence time. The logarithmic decay model is derived from the empirical law that adsorption drying exhibits exponential decay within a certain range. It maps the "removal ratio" and "equipment rate" to time requirements. The first-order kinetics satisfy Δ / Δ_0 = 1 − exp(−k_t) or an equivalent form, where k is the adsorption rate constant, t is the residence time, and Δ / Δ0 is the removal ratio. Taking the logarithm linearizes the exponential relationship to facilitate the inverse calculation of time. In implementation, the controller constructs r = 1 − exp(−k_t) based on the relative humidity removal rate r and the adsorption rate constant k, and inversely solves for the critical residence time t = −ln(1 − r) / k. At the same time, numerical protection is implemented for the input to prevent the logarithmic term from approaching infinity when r is close to 1. Numerical protection can be achieved by limiting the upper limit of r to 1 − ϵ, where ϵ is a small positive number configured for the numerical stability of the controller, ensuring that the critical residence time is finite and can be used for subsequent calculation of the maximum allowable loading flow rate. Through this reverse calculation process, the controller obtains the minimum residence time required to ensure the dew point meets the requirements under the current dew point load and the current adsorption capacity of the equipment. The larger the critical residence time, the longer the processing time is required. Therefore, in step S104, the maximum allowable loading flow rate is automatically reduced by the ratio of the effective adsorption volume parameter to the critical residence time to achieve the effect of flow restriction and quality preservation.

[0063] After obtaining the critical residence time, the controller further converts the throughput capacity of the post-treatment drying equipment under the current dew point load into the upper limit of the load on the target air compressor, thereby determining the maximum allowable loading flow rate of the target air compressor at the current moment. The reason for this step is that the larger the partial pressure difference of the water vapor to be removed corresponding to the real-time dew point value, or the smaller the adsorption rate constant, the longer the critical residence time. This means the post-treatment drying equipment needs more time to allow the compressed air to complete mass transfer with the drying medium. If the target air compressor is still loaded at a higher flow rate, the residence time of the compressed air in the post-treatment drying equipment will be shortened and less than the critical residence time, resulting in the outlet dew point failing to meet the preset dew point qualification conditions. To translate the "residence time constraint" into an executable "flow rate upper limit constraint," the controller calculates the maximum allowable loading flow rate using the ratio of the effective adsorption volume parameter to the critical residence time, ensuring that the throughput of the post-treatment drying equipment remains consistent with the drying kinetic requirements. The effective adsorption volume parameter is an engineering abstraction representing the equivalent space within the post-treatment drying equipment that truly participates in adsorption and mass transfer, characterized by a single parameter. It can be derived by comprehensively calculating the equivalent usable volume from the void volume of the drying tower bed, the effective channel volume, and the unusable dead zone volume caused by the internal structure, or it can be calculated back from the factory calibration under rated operating conditions. The effective adsorption volume parameter transforms the differences in equipment structure into a unified "volume capacity" input, allowing the controller to calculate the matching relationship between residence time and throughput without analyzing complex internal flow fields. When the usable volume is expressed in terms of the effective adsorption volume parameter, the average residence time of compressed air within the post-treatment drying equipment can be approximately expressed as t_res≈V_eff / Q, where V_eff is the effective adsorption volume parameter and Q is the volumetric flow rate through the post-treatment drying equipment. To meet the dew point qualification requirement, t_res ≥ t_crit, where t_crit is the critical residence time. Therefore, the maximum allowable volumetric flow rate upper limit Q_max = V_eff / t_crit can be derived. The controller determines this upper limit as the maximum allowable loading flow rate, thus converting the dew point quality requirement into a hard constraint on the target air compressor. In specific implementation, the controller reads the effective adsorption volume parameters of the post-treatment drying equipment from the equipment parameter table and reads the critical residence time output from the previous calculation stage, performing a ratio calculation to obtain the maximum allowable loading flow rate.To ensure control stability and physical feasibility, the controller incorporates numerical protection in the ratio calculation: when the critical residence time is set to zero or less than the preset minimum residence time by boundary constraints, the controller replaces the critical residence time with the preset minimum residence time in the ratio calculation. The preset minimum residence time is a comprehensive setting based on the minimum flow time still existing in the post-treatment drying equipment under empty tower flow conditions and the actuator response time, preventing the ratio from mathematically approaching infinity and causing abnormal amplification of the maximum allowable loading flow rate. When the maximum allowable loading flow rate calculated by the ratio exceeds the rated maximum output capacity of the target air compressor, the controller clamps the maximum allowable loading flow rate to the rated maximum output capacity of the target air compressor, thereby ensuring that the loading upper limit does not exceed the equipment capacity boundary. The controller can also introduce smoothing filtering or rate of change limits on the maximum allowable loading flow rate, so that the upper limit does not cause loading command jitter when it fluctuates with the real-time dew point value. The rate of change limit limits the upper limit change amplitude of adjacent control cycles, preventing dew point sensor noise from being amplified into frequent flow limiting actions. The maximum allowable loading flow rate obtained through the above method has direct control significance: the smaller the maximum allowable loading flow rate, the longer the residence time required by the post-treatment drying equipment to complete adsorption removal under the current dew point load, and the target air compressor must reduce its load to ensure that the residence time is not lower than the critical residence time; the larger the maximum allowable loading flow rate, the more sufficient the drying margin, and the target air compressor can increase its load without compromising the dew point qualification conditions. The effect of this step is to map the adsorption kinetic constraints of the post-treatment drying equipment to the upper limit of the flow rate of the target air compressor in real time, so that subsequent compensation control can meet the terminal pressure requirements without exceeding the dew point quality boundary, reducing dew point exceedance, excessive desiccant consumption, and fluctuations in process gas quality.

[0064] S105. If the target compensation flow rate is greater than the maximum allowable loading flow rate, a flow-limiting and quality-preserving command is generated, and the target air compressor is controlled to operate according to the maximum allowable loading flow rate based on the flow-limiting and quality-preserving command.

[0065] After obtaining the target compensation flow rate and the maximum allowable loading flow rate, the controller performs a unified arbitration between the compensation requirement and the dew point quality constraint. The reason for setting the arbitration logic is that when a rapid pressure drop occurs at the end gas consumption point, the gas supply needs to be increased through the target compensation flow rate to suppress the pressure drop. However, the processing capacity of the post-treatment drying equipment is constrained by the critical residence time. If the target air compressor loads at the target compensation flow rate in a short period of time, the volume processing rate entering the post-treatment drying equipment will exceed the upper limit of the matching between the effective adsorption volume parameter and the critical residence time. Insufficient residence time will prevent water vapor from being adsorbed in time, ultimately causing the real-time dew point value to deviate from the preset dew point qualification condition. Based on this conflict, the controller identifies a target compensation flow rate exceeding the maximum allowable loading flow rate as a trigger condition requiring flow limiting and generates a flow limiting and quality assurance command. This command is an engineering encapsulation that combines "flow limiting" and "dew point quality assurance" into a single executable instruction. The maximum allowable loading flow rate is written as a hard constraint into the air compressor control loop to prevent compensation control from exceeding the drying capacity boundary in pressure-priority mode. An upper limit clamp is applied to the target air compressor's loading setpoint, with the clamp value set to the maximum allowable loading flow rate. This limits the throughput entering the post-processing drying equipment to within a range that meets the critical residence time. The specific generation method for the flow limiting and quality assurance command can be implemented using instruction fieldization. The controller assigns the maximum allowable loading flow rate to the flow limiting threshold field, the flow limiting mode to the execution mode field, and a control cycle or a holding condition until the target compensation flow rate no longer exceeds the maximum allowable loading flow rate to the duration field. Simultaneously, the real-time dew point value, target compensation flow rate, and maximum allowable loading flow rate at the trigger moment are written as diagnostic parameters into the instruction extension field, facilitating subsequent tracing of the triggering cause of the dew point quality constraint. When the target air compressor operates under the flow-limiting and quality-preserving command, the controller switches the flow rate setpoint of the target air compressor from the target compensation flow rate to the maximum allowable loading flow rate. It then smoothly adjusts the loading using a ramp-limiting method to avoid sudden load changes that could cause motor current surges, pipeline pressure oscillations, and frequent valve actuations. In each control cycle, the load setpoint is allowed to change only up to the preset maximum change, ensuring the flow rate setpoint continuously converges to the maximum allowable loading flow rate. Simultaneously, the controller maintains real-time monitoring of the pressure sequence at the end-point gas consumption. When the pressure change rate returns to a non-negative value or the absolute value of the pressure change rate is less than the preset pressure change threshold, the controller allows exiting the flow-limiting mode and reverting to a pressure compensation strategy primarily based on the target compensation flow rate. This achieves a dynamic balance between dew point compliance and stable end-point pressure.By executing S105, the system's effects are reflected in three aspects: First, the target air compressor still provides the maximum possible load when terminal pressure compensation is needed, but the upper limit of the load is constrained by the maximum allowable loading flow rate. Second, the post-treatment drying equipment obtains the necessary residence conditions to meet the critical residence time, and the real-time dew point value is maintained near the preset dew point qualification condition. Third, the pressure compensation process avoids the risk of dew point exceeding the standard due to excessive loading, reducing downtime for troubleshooting, increased desiccant replacement frequency, and fluctuations in terminal process quality caused by dew point non-compliance. Fourth, the smooth execution brought about by the ramp limit reduces secondary fluctuations in pipeline pressure and equipment impact, improving control stability. For example, the target compensation flow rate is calculated to be 12 m³ / s. 3 The maximum allowable loading flow rate is calculated to be 9m / min. 3 / min, the controller generates a current-limiting and quality-preserving command and loads the target air compressor to a given clamp position of 9m. 3 / min, while using ramp limiting to gradually approach this value within several control cycles, the decline in terminal pressure is alleviated and the outlet dew point of the post-treatment drying equipment remains in compliance with the preset dew point qualification conditions.

[0066] Please see Figure 3 This is a schematic diagram of the data control system for an air compressor in an embodiment of this application.

[0067] It should be noted that, Figure 3 The structure of the data control system for an air compressor shown is merely an example and should not impose any limitations on the functionality and scope of application of the embodiments of the present invention.

[0068] like Figure 3 As shown, a data control system for an air compressor includes a central processing unit 301, which can perform various appropriate actions and processes according to a program stored in a read-only memory 302 or a program loaded from a storage section 308 into a random access memory 303, such as executing the methods described in the above embodiments. The random access memory 303 also stores various programs and data required for system operation. The central processing unit 301, the read-only memory 302, and the random access memory 303 are interconnected via a bus 304. An input / output interface 305 is also connected to the bus 304.

[0069] The following components are connected to the input / output interface 305: an input section 306 including audio input devices, push-button switches, etc.; an output section 307 including an LCD display, audio output devices, indicator lights, etc.; a storage section 308 including a hard disk, etc.; and a communication section 309 including a network interface card such as a LAN (Local Area Network) card, modem, etc. The communication section 309 performs communication processing via a network such as the Internet. A drive 310 is also connected to the input / output interface 305 as needed. A removable medium 311, such as a disk, optical disk, magneto-optical disk, semiconductor memory, etc., is installed on the drive 310 as needed so that computer programs read from it can be installed into the storage section 308 as needed.

[0070] In particular, according to embodiments of the present invention, the processes described above with reference to the flowcharts can be implemented as computer software programs. For example, embodiments of the present invention include a computer program product comprising a computer program carried on a computer-readable medium, the computer program containing computer programs for performing the methods shown in the flowcharts. In such embodiments, the computer program can be downloaded and installed from a network via communication section 309, and / or installed from removable medium 311. When the computer program is executed by central processing unit 301, it performs the various functions defined in the present invention.

[0071] It should be noted that specific examples of computer-readable storage media may include, but are not limited to: electrical connections having one or more wires, portable computer disks, hard disks, random access memory, read-only memory, erasable programmable read-only memory, flash memory, optical fiber, portable compact disk read-only memory, optical storage devices, magnetic storage devices, or any suitable combination thereof. In this invention, a computer-readable storage medium can be any tangible medium containing or storing a program that can be used by or in conjunction with an instruction execution system, apparatus, or device.

[0072] The flowcharts and block diagrams in the accompanying drawings illustrate the architecture, functionality, and operation of possible implementations of systems, methods, and computer program products according to various embodiments of the present invention. Each block in a flowchart or block diagram may represent a module, segment, or portion of code, which contains one or more executable instructions for implementing a specified logical function. It should also be noted that in some alternative implementations, the functions indicated in the blocks may occur in a different order than those shown in the drawings.

[0073] Specifically, the data control system for an air compressor in this embodiment includes a processor and a memory. The memory stores a computer program, and when the computer program is executed by the processor, it implements the data control method for an air compressor provided in the above embodiment.

[0074] In another aspect, the present invention also provides a computer-readable storage medium, which may be included in a data control system for an air compressor as described in the above embodiments; or it may exist independently and not assembled into the data control system for the air compressor. The storage medium carries one or more computer programs, which, when executed by a processor of the air compressor's data control system, cause the air compressor's data control system to implement the air compressor data control method provided in the above embodiments.

Claims

1. A data control method for an air compressor, characterized in that, The method includes: The pipeline geometric parameters from the target air compressor to the end air consumption point, the real-time pressure sequence of the end air consumption point, the real-time dew point value and real-time volumetric flow rate of the target air compressor outlet, and the effective adsorption volume parameters of the post-treatment drying equipment are obtained. Based on the pipeline geometry parameters, the real-time dew point value, and the real-time volumetric flow rate, calculate the transmission lag time of compressed air from the outlet of the target air compressor to the end point of air consumption. The pressure change rate is obtained by differential calculation of the real-time pressure sequence. When the pressure change rate is negative and the absolute value of the pressure change rate is greater than the preset pressure change threshold, the target compensation flow is calculated based on the pressure change rate and the transmission lag time. Based on the real-time dew point value and the preset saturated vapor pressure characteristic curve, the critical residence time for the compressed air in the post-treatment drying equipment to meet the preset dew point qualification condition is calculated, and the maximum allowable loading flow rate of the target air compressor at the current moment is determined according to the ratio of the effective adsorption volume parameter to the critical residence time. If the target compensation flow rate is greater than the maximum allowable loading flow rate, a flow-limiting and quality-preserving command is generated, and the target air compressor is controlled to operate according to the maximum allowable loading flow rate based on the flow-limiting and quality-preserving command.

2. The method according to claim 1, characterized in that, The calculation of the transmission lag time of compressed air from the outlet of the target air compressor to the end-use point, based on the pipeline geometric parameters, the real-time dew point value, and the real-time volumetric flow rate, specifically includes: Calculate the physical volume of the pipeline between the target air compressor and the end point of air consumption based on the pipeline geometry parameters; The real-time compressed air pressure in the pipeline between the target air compressor and the end point of air consumption is obtained. Based on the real-time compressed air pressure and the preset gas state equation, the real-time volumetric flow rate is converted into the operating condition state corresponding to the real-time compressed air pressure to obtain the pressure operating condition volumetric flow rate. The current water vapor partial pressure is determined based on the real-time dew point value, and the volumetric flow rate under the pressure condition is corrected for wet air based on the water vapor partial pressure to obtain the actual delivery volumetric flow rate. The actual delivery volumetric flow rate is used to compensate for the velocity increment caused by the water vapor partial pressure occupying the physical space of the pipeline. The transmission lag time is obtained by calculating the ratio of the physical volume of the pipeline to the actual transport volume flow rate.

3. The method according to claim 2, characterized in that, The step of correcting the volumetric flow rate under pressure conditions for wet air based on the partial pressure of water vapor to obtain the actual delivery volumetric flow rate specifically includes: The difference between the real-time compressed air pressure and the water vapor partial pressure is calculated to obtain the dry air partial pressure; The ratio of the real-time compressed air pressure to the dry air partial pressure is determined as the humid air expansion correction factor; The actual delivery volumetric flow rate is obtained by multiplying the volumetric flow rate under the pressure condition with the humid air expansion correction coefficient.

4. The method according to claim 1, characterized in that, The calculation of the target compensation flow rate based on the pressure change rate and the transmission lag time specifically includes: The product of the absolute value of the pressure change rate and the transmission lag time is calculated to obtain the predicted pressure drop during the lag period; If the predicted pressure drop during the lag period is greater than the preset critical venting threshold of the pipeline network, then the linear initial compensation flow rate is calculated based on the pressure change rate, and the historical gas consumption cycle duration of the terminal gas consumption point is obtained. The ratio of the transmission lag time to the historical gas consumption cycle duration is calculated to obtain the lag response ratio; The overshoot attenuation coefficient is calculated based on the hysteresis response ratio, and the product of the linear initial compensation flow and the overshoot attenuation coefficient is determined as the target compensation flow. If the predicted pressure drop during the lag period is less than or equal to the critical venting threshold of the pipeline network, then the linear initial compensation flow rate is determined as the target compensation flow rate.

5. The method according to claim 4, characterized in that, The calculation of the overshoot attenuation coefficient based on the hysteresis response ratio specifically includes: The fractional part of the hysteresis response ratio is defined as the periodic synchronization deviation. If the periodic synchronization deviation does not fall into the preset reverse superposition risk zone, the anti-overshoot attenuation coefficient is calculated based on the preset standard attenuation curve. The preset reverse superposition risk zone is used to characterize the risk range where the gas demand decreases when the compensation flow reaches the end due to transmission lag. If the periodic synchronization deviation falls into the preset reverse superposition risk zone, the ratio of the real-time dew point value to the preset limit dew point threshold is calculated to obtain the dew point penalty weight. The initial attenuation is obtained by multiplying the periodic synchronization deviation by the dew point penalty weight. The dynamic clamping attenuation is determined based on the initial attenuation and the preset maximum allowable attenuation threshold. The difference between the preset reference attenuation coefficient and the dynamic clamping attenuation amount is determined as the overshoot attenuation coefficient.

6. The method according to claim 5, characterized in that, The determination of the dynamic clamping attenuation based on the initial attenuation and the preset maximum allowable attenuation threshold specifically includes: If the initial attenuation is greater than the preset maximum allowable attenuation threshold, then the maximum allowable attenuation threshold is determined as the dynamic clamping attenuation. If the initial attenuation is less than or equal to the preset maximum allowable attenuation threshold, then the initial attenuation is determined as the dynamic clamping attenuation.

7. The method according to claim 1, characterized in that, The calculation of the critical residence time for compressed air in the post-treatment drying equipment to meet the preset dew point qualification condition based on the real-time dew point value and the preset saturated vapor pressure characteristic curve specifically includes: Based on the preset saturated vapor pressure characteristic curve, the current saturated water vapor partial pressure corresponding to the real-time dew point value and the target saturated water vapor partial pressure corresponding to the preset dew point qualification conditions are determined respectively. Calculate the difference between the current saturated water vapor partial pressure and the target saturated water vapor partial pressure to obtain the water vapor partial pressure difference that needs to be removed; Obtain the adsorption rate constant of the post-treatment drying equipment, and calculate the ratio of the partial pressure difference of water vapor to be removed to the current saturated water vapor partial pressure to obtain the relative humidity removal rate; A logarithmic decay model is constructed based on the relative humidity removal rate and the adsorption rate constant. The critical residence time is obtained by inversely solving the logarithmic decay model.

8. A data control system for an air compressor, characterized in that, The air compressor data control system includes: one or more processors and a memory; the memory is coupled to the one or more processors, the memory is used to store computer program code, the computer program code includes computer instructions, and the one or more processors call the computer instructions to cause the air compressor data control system to perform the method as described in any one of claims 1-7.

9. A computer-readable storage medium comprising instructions, characterized in that, When the instruction is executed on the air compressor's data control system, the air compressor's data control system performs the method as described in any one of claims 1-7.

10. A computer program product, characterized in that, When the computer program product is run on the data control system of the air compressor, the data control system of the air compressor performs the method as described in any one of claims 1-7.

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