A centralized oil supply temperature control system for a plastic pipe production workshop

Abstract

The present application belongs to the technical field of plastic processing equipment temperature control, and discloses a centralized oil supply temperature control system for plastic pipe production workshop. The present application builds a pipeline size-temperature loss mapping relationship, calculates the initial heating temperature in combination with the demand temperature of each branch, reduces the oil temperature loss deviation caused by pipeline differences, reduces the adjustment pressure of secondary temperature control, and improves the adaptability of the initial heating temperature. Through the real-time monitoring and correction of the input oil temperature by the secondary temperature control module, the actual working temperature of each device is ensured to be consistent with the demand temperature, directly improving the stability of the quality of the plastic pipe products. Through the optimization of the target temperature and targeted regulation and control, the decrease of the circulation efficiency or the damage of the equipment caused by the too large temperature difference of the backflow oil is avoided, the service life of the system is prolonged, and the controllability of the backflow oil collection temperature is improved. Through the centralized heating correction module, the main pipeline temperature is dynamically adjusted according to the actual temperature control data, the invalid temperature control operation is reduced, and the energy consumption is reduced.

Description

Technical Field

[0001] This invention belongs to the field of temperature control technology for plastic processing equipment, and relates to a centralized oil supply temperature control system for plastic pipe production workshops. Background Technology

[0002] In the plastic pipe production process, core equipment such as extruders and molding dies require a stable heat source through heat transfer oil. Precise control of their operating temperature directly affects the physical properties and appearance quality of the product. To improve energy efficiency, modern workshops often employ centralized oil supply systems. This involves centrally heating the heat transfer oil through a main pipeline and then distributing it to various equipment, while also allowing it to return to the collection point for recycling through branch pipelines.

[0003] However, the temperature control accuracy of centralized oil supply systems has always been a challenge for the industry. Due to the differences in the size of the branch pipelines, the temperature loss of the heat transfer oil during transmission is inconsistent; at the same time, the required temperature of each device may be different. Traditional systems struggle to balance centralized heating of the main pipeline with precise temperature control of the branch pipelines, resulting in large deviations in the actual input oil temperature of the equipment and drastic fluctuations in the temperature of the return oil. This not only affects product quality but also leads to energy waste due to repeated temperature control adjustments.

[0004] Specifically, the traditional technical solution still has the following problems: 1. The initial heating temperature setting of the traditional technical solution is unreasonable. It does not take into account the impact of the size difference of different branch pipes on temperature loss. The initial heating temperature of the main pipe is set only based on experience or the needs of a single equipment, which leads to the oil temperature of some branches reaching the equipment being too high or too low, requiring frequent secondary adjustments.

[0005] 2. Traditional technical solutions lack real-time monitoring and dynamic control of the oil temperature at the equipment input end. They rely solely on the direct distribution of the heating temperature from the main pipeline, which makes it difficult to match the real-time temperature requirements of each piece of equipment, resulting in fluctuations in the operating temperature of the equipment.

[0006] 3. Traditional technical solutions result in unstable reflux oil collection temperature and large temperature differences in the output oil of each branch. During collection, temperature fluctuations can easily affect the heat transfer oil circulation efficiency, and even cause scaling in pipelines and equipment damage due to local high or low temperatures.

[0007] 4. Traditional technical solutions lack a dynamic correction mechanism and do not adjust the heating temperature of the main pipeline based on actual temperature control data feedback, resulting in the secondary temperature control equipment operating under high load for a long time, with high energy consumption and difficulty in guaranteeing temperature control accuracy. Summary of the Invention

[0008] In view of this, in order to solve the problems mentioned in the background art, a centralized oil supply temperature control system for plastic pipe production workshops is proposed.

[0009] The objective of this invention can be achieved through the following technical solution: A centralized oil supply temperature control system for a plastic pipe production workshop, comprising: a centralized oil heating module, which analyzes the initial heating temperature of the centralized heating main pipeline based on the required temperature of each distributed device and the pre-constructed pipeline size-temperature loss mapping relationship, and uses heating equipment to heat the heat transfer oil in the main pipeline to the initial heating temperature.

[0010] The secondary oil temperature control module sets up temperature control devices on the branch pipelines near the oil input direction of each distributed device. It performs input temperature control based on the measured input oil temperature, records and constructs a temperature control dataset in real time, which specifically includes the temperature control direction and temperature control amplitude.

[0011] The oil reflux temperature control module installs reflux temperature control devices on each branch pipeline near the oil collection point. Based on the measured output oil temperature, it identifies the target temperature of the oil collection, calibrates the branch pipelines that need output temperature control, and performs oil reflux temperature control on them.

[0012] The centralized heating correction module determines whether the initial heating temperature of the main heating pipe needs to be adjusted based on the temperature control dataset. If so, it outputs the adjusted initial heating temperature.

[0013] Compared with the prior art, the beneficial effects of the present invention are as follows: (1) The present invention constructs a pipeline size-temperature loss mapping relationship, calculates the initial heating temperature in combination with the required temperature of each branch, reduces the oil temperature loss deviation caused by pipeline differences, reduces the adjustment pressure of secondary temperature control, and improves the adaptability of the initial heating temperature.

[0014] (2) The present invention monitors and corrects the input oil temperature in real time through a secondary temperature control module, ensuring that the actual working temperature of each device is consistent with the required temperature, thereby directly improving the stability of the quality of plastic pipe products.

[0015] (3) By optimizing the target temperature and targeted regulation, this invention avoids the decrease in circulation efficiency or equipment damage caused by excessive temperature difference in the return oil, extends the service life of the system, and improves the controllability of the return oil collection temperature.

[0016] (4) The present invention dynamically adjusts the temperature of the main pipeline based on the actual temperature control data through a centralized heating correction module, thereby reducing ineffective temperature control operations and reducing energy consumption; at the same time, the system can be adapted to different sizes of branches and equipment requirements, and has strong versatility. Attached Figure Description

[0017] To more clearly illustrate the technical solutions of the embodiments of the present invention, the accompanying drawings used in the description of the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0018] Figure 1 This is a schematic diagram showing the connections of the various modules in the system of the present invention.

[0019] Figure 2 This is a schematic diagram of a dynamic adaptability analysis process based on a reference temperature, corresponding to one embodiment of the present invention.

[0020] Figure 3 This is a schematic diagram of the matching analysis process based on temperature range and equipment capability for one embodiment of the present invention. Detailed Implementation

[0021] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0022] Please see Figure 1 As shown, the present invention provides a centralized oil supply temperature control system for a plastic pipe production workshop, comprising a centralized oil heating module, a secondary oil temperature control module, an oil reflux temperature control module, and a centralized heating correction module, wherein the centralized oil heating module is connected to the secondary oil temperature control module, the secondary oil temperature control module is connected to the oil reflux temperature control module, and the oil reflux temperature control module is connected to the centralized heating correction module.

[0023] The centralized oil heating module analyzes the initial heating temperature of the main pipeline based on the required temperature of each distributed device and the pre-constructed pipeline size-temperature loss mapping relationship, and uses heating equipment to heat the heat transfer oil in the main pipeline to the initial heating temperature.

[0024] It's important to explain why the initial heating temperature of the centralized heating main pipeline is analyzed based on the required temperatures of each distributed device and the pre-built pipeline size-temperature loss mapping relationship: different branch pipeline sizes lead to varying temperature losses during heat transfer oil transmission. The mapping relationship quantifies this loss, and combined with the device's required temperature, the required initial temperature for each branch can be determined. Analyzing the initial heating temperature of the main pipeline based on this ensures that, after transmission losses, the heat transfer oil reaches each device at a temperature close to the required value, reducing the burden of subsequent secondary temperature control, improving the accuracy and efficiency of system temperature control, and avoiding energy waste and equipment instability caused by unreasonable initial temperatures.

[0025] In a preferred embodiment of the present invention, the specific construction method of the pipeline size-temperature loss mapping relationship is as follows: collect pipeline size information of each branch pipeline in the plastic pipe production workshop, including key parameters such as pipeline length, diameter, and material thickness.

[0026] Different sizes of branch pipes were selected as test objects. Heat transfer oil at a specific temperature was introduced at the starting point of each test branch pipe, and the oil flow rate was kept stable.

[0027] Temperature detection devices are installed at the end of each test pipeline to monitor and record the actual temperature of the oil flowing through the pipeline in real time. The difference between the starting temperature and the ending temperature is calculated to obtain the temperature loss value corresponding to the pipeline size.

[0028] By changing to test pipes of different sizes, repeat the above steps of inputting oil at a specific temperature, monitoring the endpoint temperature, and calculating the temperature loss, and accumulate multiple sets of data on pipe dimensions and corresponding temperature losses.

[0029] The collected data were organized to establish the correspondence between pipeline size parameters and temperature loss values, forming a pipeline size-temperature loss mapping relationship.

[0030] It should be noted that the reason for establishing the pipeline size-temperature loss mapping relationship is as follows: 1. To solve the problem of inconsistent temperature loss caused by differences in pipelines. Within the plastic pipe production workshop, the length, diameter, and material thickness of each branch pipeline vary, and these differences directly affect the heat loss of the heat transfer oil during transmission. By establishing this mapping relationship, the temperature loss value corresponding to different pipeline sizes can be quantified, avoiding oil temperature deviations caused by different pipeline characteristics.

[0031] 2. To provide a basis for calculating the initial heating temperature, the initial heating temperature of the centralized heating main pipeline needs to be adjusted based on the required temperature of each distributed device, combined with the temperature loss of the branch pipelines. If there is a lack of correspondence between pipeline size and temperature loss, it is impossible to accurately estimate the heat loss of different branches, which will lead to unreasonable initial heating temperature settings, and consequently cause problems such as large deviations in oil temperature of subsequent branches and frequent secondary temperature control.

[0032] 3. Reduce secondary temperature control load and improve system efficiency. The mapping relationship can predict the temperature loss of each branch in advance, so that the initial heating temperature of the main pipeline is closer to the actual needs of each branch. This reduces the oil temperature deviation at the input end of the branch from the source, reduces the adjustment frequency and amplitude of the secondary temperature control module, thereby saving energy and extending the life of the temperature control equipment.

[0033] It should be further explained that stratified sampling can be used to select typical pipeline size combinations as test objects, prioritizing the coverage of commonly used sizes and extreme values ​​of key parameters with a high proportion in the workshop, thereby reducing the amount of testing. For untested size combinations, temperature loss values ​​are predicted based on existing data using interpolation methods or machine learning models, and then corrected by a small number of validation tests. At the same time, pipeline size parameters are normalized to simplify variable dimensions and reduce data complexity, thereby solving the problem of construction difficulties caused by too many size combination groups while ensuring the accuracy of the mapping relationship.

[0034] In another embodiment, temperature loss testing is performed only on branch pipelines with corresponding dimensions in the factory workshop, thereby constructing a targeted pipeline size-temperature loss mapping relationship.

[0035] In a preferred embodiment of the present invention, the specific analysis method for the initial heating temperature of the centralized heating main pipeline is as follows: the pipeline size of each branch pipeline is matched with the pipeline size-temperature loss mapping relationship to obtain the initial heating temperature correction amount of each branch pipeline.

[0036] The initial required temperature of each branch pipeline is obtained by summing the initial heating temperature correction of each branch pipeline with the required temperature of the corresponding distributed equipment.

[0037] It should be noted that summing the initial heating temperature correction for each branch pipeline with the required temperature of the corresponding distributed equipment is to obtain the temperature that the heat transfer oil needs to reach when it exits the main pipeline to the starting point of that branch. This is because the initial heating temperature correction represents the temperature loss caused by the dimensional characteristics of the branch pipeline, while the equipment required temperature is the target temperature that the heat transfer oil must meet when it reaches the equipment. Summing the two ensures that after the heat transfer oil enters the branch from the main pipeline, due to the temperature loss during the transmission process, the oil temperature when it finally reaches the equipment is close to the required temperature. This reduces the adjustment pressure for subsequent precise temperature control and is a key calculation step in balancing the centralized heating of the main pipeline and the individual needs of the branches.

[0038] Arrange the initial required temperatures of each branch pipeline from highest to lowest, and select the median as the initial heating temperature of the centralized heating main pipeline.

[0039] It should be noted that the median value was selected as the initial heating temperature of the main pipeline after arranging the initial demand temperatures of each branch from highest to lowest. This is because the median balances the demands of different branches and avoids the influence of extreme values. If the maximum value were selected, most branches would have excessively high oil temperatures requiring cooling, increasing energy consumption; if the minimum value were selected, most branches would have insufficient oil temperatures requiring heating, which is also inefficient. The median value ensures that the initial demand temperatures of about half of the branches are close to the temperature of the main pipeline, reducing the overall temperature control adjustment range and frequency. While meeting the basic requirements of most equipment, it reduces the system load and balances temperature control efficiency and energy consumption.

[0040] It should be further explained that the reason for choosing the median instead of the mean in this invention is that the initial demand temperature of each branch may have extreme values ​​due to differences in pipe size. If the average value is used, it will be affected by extreme values ​​and biased too high or too low, resulting in increased oil temperature deviation in most branches and increasing the burden on secondary temperature control. The median, on the other hand, is not affected by extreme values ​​and can reflect the intermediate level, so that the initial demand temperature of about half of the branches is close to the main pipe temperature, reducing the overall adjustment range, which is more in line with the temperature control goal of balancing the demand of most branches and reducing the system load, thus taking into account both efficiency and stability.

[0041] It should be noted that this invention reduces the deviation in oil temperature loss caused by differences in pipelines by constructing a pipeline size-temperature loss mapping relationship and calculating the initial heating temperature in combination with the required temperature of each branch, thereby reducing the adjustment pressure of secondary temperature control and improving the adaptability of the initial heating temperature.

[0042] The secondary oil temperature control module sets up temperature control devices on the branch pipelines near the oil input direction of each distributed device. It performs input temperature control based on the measured input oil temperature, records and constructs a temperature control dataset in real time, which specifically includes the temperature control direction and temperature control amplitude.

[0043] In a preferred embodiment of the present invention, the specific method for performing input end temperature control is as follows: the measured input oil temperature of each branch pipeline is compared with the required temperature of each distributed device. If the relative deviation between the measured input oil temperature and the required temperature of the distributed device exceeds the limit, it is determined that input end temperature control is required.

[0044] In one embodiment, when comparing the measured input oil temperature of each branch pipeline with the required temperature of each distributed device, an analysis is performed by setting a relative deviation threshold. The relative deviation threshold is set based on two factors: first, the actual requirements of the plastic pipe production equipment for oil temperature accuracy, which must be combined with the process standards of different equipment to ensure that the oil temperature deviation does not affect product quality; second, the adjustment capability of the temperature control equipment, the threshold must match the temperature control accuracy that the equipment can achieve, to avoid frequent start-ups or adjustment failures due to the threshold being too small, while also taking into account energy consumption and control efficiency, and finally determining a reasonable range through experimental verification.

[0045] If the measured input oil temperature is greater than the required temperature of the distribution equipment, the temperature control direction is determined to be cooling, and the difference between the measured input oil temperature and the required temperature of the distribution equipment is recorded as the temperature control amplitude of the corresponding input end temperature control.

[0046] If the measured input oil temperature is lower than the required temperature of the distribution equipment, the temperature control direction is determined to be heating. The difference between the required temperature of the distribution equipment and the measured input oil temperature is recorded as the temperature control amplitude of the corresponding input terminal temperature control.

[0047] It should be noted that this invention monitors and corrects the input oil temperature in real time through a secondary temperature control module, ensuring that the actual operating temperature of each device is consistent with the required temperature, thereby directly improving the stability of the quality of plastic pipe products.

[0048] The oil reflux temperature control module installs reflux temperature control devices on each branch pipeline near the oil collection point. Based on the measured output oil temperature, it identifies the target temperature of the oil collection, calibrates the branch pipelines that need output temperature control, and performs oil reflux temperature control on them.

[0049] It's important to explain that oil reflux temperature control is necessary because the output oil temperatures of each branch pipeline differ. Directly collecting these temperatures would cause drastic overall temperature fluctuations, affecting the heat transfer oil circulation efficiency and potentially leading to pipe scaling and equipment damage due to excessive local temperature differences. By identifying and adjusting the target collection temperature, the output oil temperatures of each branch can be made more uniform, reducing energy loss and temperature shocks during collection, ensuring stable operation of the circulation system, and providing a stable initial temperature for subsequent heat transfer oil reuse. This reduces energy consumption for reheating or cooling, improving the economy and safety of the entire centralized oil supply system.

[0050] In a preferred embodiment of the present invention, the specific method for identifying the target temperature of the oil collection is as follows: obtain the measured output oil temperature of each branch pipeline, take the measured output oil temperature of any branch pipeline as the reference output oil temperature, and calculate the sum of the actual temperature adjustment spans of the other branch pipelines adjusted to the reference output oil temperature.

[0051] The actual output oil temperature of each branch pipeline is calculated as the sum of the actual temperature adjustment spans corresponding to the reference output oil temperature.

[0052] The sum of each actual temperature adjustment span is compared, and the reference output oil temperature corresponding to the smallest sum of actual temperature adjustment spans is selected as the target temperature for oil collection.

[0053] It's important to explain that by comparing the sum of all actual temperature adjustment spans, the minimum total output oil temperature is selected as the target temperature. The core principle is to achieve efficient reflux temperature control by minimizing overall temperature adjustment costs. The sum of the actual temperature adjustment spans reflects the total workload of adjusting the output oil from all branches to a certain reference temperature. The smaller the sum, the smaller the overall temperature adjustment range required for each branch. Using this as the target temperature minimizes the adjustment load on the reflux temperature control equipment, reduces energy consumption, and avoids oil temperature fluctuations caused by large temperature adjustments. This ensures stable temperature when the output oil from each branch converges, improves the operating efficiency and stability of the heat transfer oil circulation system, and lays a good foundation for subsequent oil reuse.

[0054] In a preferred embodiment of the present invention, the specific method for calibrating the branch that requires output end temperature control is as follows: the measured output oil temperature of each branch pipeline is compared with the reference output oil temperature to determine whether the deviation between the measured output oil temperature of each branch pipeline and the reference output oil temperature exceeds the limit.

[0055] If the measured output oil temperature of a branch pipeline deviates from the reference output oil temperature beyond the limit, then the branch pipeline is designated as a branch pipeline that requires output end temperature control; otherwise, it is determined that output end temperature control is not required.

[0056] The specific method for determining whether the deviation between the measured output oil temperature and the reference output oil temperature of each branch pipeline exceeds the limit is as follows: calculate the absolute difference between the measured output oil temperature and the reference output oil temperature of each branch pipeline, compare the result with the preset output oil temperature deviation threshold, and if the result is greater than the output oil temperature deviation threshold, it is determined that the deviation between the measured output oil temperature and the reference output oil temperature of the branch pipeline exceeds the limit; otherwise, it is determined that the deviation between the measured output oil temperature and the reference output oil temperature of the branch pipeline does not exceed the limit.

[0057] It should be noted that the output oil temperature deviation threshold is a critical value used to determine whether the deviation between the branch pipeline's output oil temperature and the target convergence temperature needs to be adjusted. Its setting is based on two aspects: first, the stability requirements of the heat transfer oil circulation system; if the deviation is too large, it can easily cause drastic temperature fluctuations during convergence, affecting pipeline lifespan and circulation efficiency; second, the adjustment capability of the return flow temperature control equipment, avoiding a threshold that is too small leading to frequent start-ups and shutdowns, or too large causing temperature control failure. It is usually determined experimentally, for example, based on the system's tolerance range for convergence temperature fluctuations. If this value is exceeded, it is determined that output temperature control of the branch is necessary to ensure that the return flow oil temperature approaches the target, balancing control accuracy and system load.

[0058] For a preferred embodiment of the present invention, please refer to Figure 2 , 3 As shown, when performing oil reflux temperature control, it is necessary to determine whether the reflux temperature control equipment has temperature control capability. The specific analysis method is as follows: A1. Calculate the difference between the measured output oil temperature of each branch pipeline and the reference output oil temperature, and then compare it with the maximum temperature control capability of the reflux temperature control equipment of each branch pipeline.

[0059] A2. If the calculated difference between the measured output oil temperature and the reference output oil temperature of all branch pipelines is less than the maximum temperature control capability of the corresponding reflux temperature control device, the reflux temperature control device is deemed to have temperature control capability.

[0060] A3. If the calculated difference between the measured output oil temperature and the reference output oil temperature in any branch pipeline is greater than the maximum temperature control capacity of the corresponding reflux temperature control device, then adjust the reference output oil temperature.

[0061] A4. Based on the adjusted reference output oil temperature, re-analyze until the reference output oil temperature is equal to half of the sum of the maximum measured output oil temperature and the minimum measured output oil temperature. If the calculated difference between the measured output oil temperature and the reference output oil temperature of any branch pipeline is still greater than the maximum temperature control capability of the corresponding reflux temperature control device, then it is determined that the reflux temperature control device does not have temperature control capability.

[0062] It needs to be explained that when the temperature difference in some branches exceeds the maximum temperature control capability of the equipment, the reference output oil temperature is adjusted to try to match the equipment capability. Theoretically, half of the sum of the maximum and minimum measured output oil temperatures is the most balanced reference point. If, under this optimal reference, the measured output oil temperature of a branch still exceeds the maximum temperature control capability of the corresponding equipment, it means that even if the most reasonable target temperature is selected, the equipment cannot meet the control requirements of all branches. In this case, it is determined that the return flow temperature control equipment does not have the temperature control capability, and other methods, such as replacing the equipment or adjusting the system, are needed to solve the problem.

[0063] B1. Compare the measured output oil temperatures of each branch pipeline, and calculate the difference between the maximum and minimum measured output oil temperatures to obtain the measured output oil temperature range.

[0064] B2. The maximum temperature control capability is obtained by summing the maximum measured output oil temperature and the minimum measured output oil temperature.

[0065] B3. Compare the measured output oil temperature range with the maximum temperature control capability limit. If the measured output oil temperature range is greater than the maximum temperature control capability limit, it is determined that the reflux temperature control device does not have temperature control capability; otherwise, it is determined that the reflux temperature control device has temperature control capability.

[0066] It should be noted that this invention combines two methods to determine the capability of reflux temperature control equipment: dynamic adaptability analysis based on a reference temperature and matching analysis based on temperature range and equipment capability. The advantage lies in balancing accuracy and comprehensiveness. Dynamic adaptability analysis verifies the equipment's adaptability to different target temperatures by adjusting the reference temperature, avoiding misjudgments caused by a single reference. Matching analysis directly assesses the overall control range coverage by comparing the sum of the oil temperature range and the equipment capability. The combination of these two methods considers both the optimized adaptability to the target temperature and the equipment's extreme capabilities under extreme temperature differences, allowing for a more comprehensive check of whether the equipment can meet the control needs of all branches. This reduces temperature control failures caused by oversights in a single judgment method and ensures the reliability of oil reflux temperature control.

[0067] In a preferred embodiment of the present invention, the maximum temperature control capability of the return flow temperature control device for each branch pipeline is specifically achieved as follows: a large number of return flow temperature control tests are conducted on each branch pipeline, heat transfer oil at different temperatures is input, the temperature is controlled using the return flow temperature control device, and the output heat transfer oil temperature after the actual temperature control test is calculated.

[0068] The actual temperature control range corresponding to the temperature control test of each return flow temperature control device is obtained by calculating the difference between the temperature of the input heat transfer oil and the temperature of the output heat transfer oil.

[0069] The maximum temperature control capacity of each branch pipeline's return flow temperature control equipment is obtained by averaging the actual temperature control amplitudes corresponding to the temperature control tests of each return flow temperature control equipment.

[0070] In a preferred embodiment, when analyzing the maximum temperature control capability of the return flow temperature control equipment in each branch pipeline, the effects of heat loss in the branch pipeline and oil flow rate fluctuations on the control effect are also considered.

[0071] It should be noted that this invention optimizes the target temperature and implements targeted control to avoid a decrease in circulation efficiency or equipment damage caused by excessive temperature differences in the return oil, thereby extending the system's service life and improving the controllability of the return oil collection temperature.

[0072] The centralized heating correction module determines whether the initial heating temperature of the main heating pipe needs to be adjusted based on the temperature control dataset. If so, it outputs the adjusted initial heating temperature.

[0073] In a preferred embodiment of the present invention, the specific method for determining whether the initial heating temperature of the main heating pipe needs to be adjusted is as follows: extract the temperature control dataset and obtain the temperature control direction and temperature control amplitude corresponding to each temperature control dataset.

[0074] The average temperature control amplitude is calculated by averaging the temperature control amplitudes of each temperature control dataset. This average amplitude is then compared with a preset threshold. If the average temperature control amplitude is greater than the preset threshold, it is determined that the initial heating temperature of the main heating pipe needs to be adjusted; otherwise, it is determined that the initial heating temperature of the main heating pipe does not need to be adjusted.

[0075] It should be explained that the temperature control amplitude of each temperature control dataset reflects the actual temperature difference that each branch needs to adjust at the input or output end, and its average value can represent the overall temperature control load of the system. If the average temperature control amplitude is greater than the preset threshold, it indicates that most branches require a large temperature adjustment, indirectly indicating that the initial heating temperature of the main pipeline is poorly matched with the actual needs of each branch. In this case, the deviation needs to be reduced from the source by adjusting the initial temperature of the main pipeline. Conversely, if the average amplitude is lower than the threshold, it indicates that the overall temperature control load is small, and the initial temperature of the main pipeline basically matches the needs of each branch, without the need for additional adjustment.

[0076] In a preferred embodiment, an analysis process is provided for setting a temperature control amplitude threshold based on historical operating data statistics: First, the temperature control amplitude of each temperature control dataset during stable system operation is collected, extreme outliers are removed, and the average temperature control amplitude for different time periods is calculated and a distribution range is formed. The maximum average amplitude value under more than 90% normal operating conditions is statistically analyzed, and this is used as a benchmark, with an additional 10%-20% redundancy added as a preset threshold. During comparison, if the current average temperature control amplitude exceeds this threshold, it indicates that the initial temperature of the main pipeline has decreased in match with the branch demand, and adjustment is required; otherwise, no adjustment is needed. This avoids frequent adjustments and ensures that the system is stable and efficient under most historical operating conditions.

[0077] In a preferred embodiment of the present invention, the specific method for adjusting the initial heating temperature after output is as follows: calculate the average temperature rise amplitude of the temperature control dataset with the temperature control direction of rising, calculate the average temperature drop amplitude of the temperature control dataset with the temperature control direction of falling, and compare the average temperature rise amplitude with the average temperature drop amplitude.

[0078] If the average temperature rise range is greater than the average temperature fall range, the difference between the average temperature rise range and the average temperature fall range is used as the initial heating temperature correction amount. Then, the initial heating temperature and the initial heating temperature correction amount are summed to calculate the adjusted initial heating temperature.

[0079] If the average temperature rise range is less than the average temperature fall range, the difference between the average temperature rise range and the average temperature fall range is used as the initial heating temperature correction amount. Then, the difference between the initial heating temperature and the initial heating temperature correction amount is used to calculate the adjusted initial heating temperature.

[0080] It should be noted that the present invention dynamically adjusts the temperature of the main pipeline based on actual temperature control data through a centralized heating correction module, reducing ineffective temperature control operations and lowering energy consumption; at the same time, the system can be adapted to the needs of different sized branches and equipment, and has strong versatility.

[0081] It should be noted that while secondary oil temperature control can be performed, temperature control capability analysis can also be conducted. However, in actual operation, considering that secondary oil temperature control is close to the initial main pipeline oil heating operation, the situation of being unable to perform secondary oil temperature control beyond the limit is generally unlikely. Therefore, this invention does not list it. However, in actual production, if the secondary oil temperature control capability exceeds the limit due to usage time and mechanical aging, the relevant equipment can be analyzed and warnings can be issued separately.

[0082] The above content is merely an example and illustration of the concept of the present invention. Those skilled in the art can make various modifications or additions to the specific embodiments described, or use similar methods to replace them, as long as they do not deviate from the concept of the invention or exceed the scope defined by the present invention, and all such modifications and additions should fall within the protection scope of the present invention.

Claims

1. A centralized oil supply and temperature control system for a plastic pipe production workshop, characterized in that, include: The centralized oil heating module analyzes the initial heating temperature of the main pipeline based on the required temperature of each distributed device and the pre-constructed pipeline size-temperature loss mapping relationship, and uses the heating equipment to heat the heat transfer oil in the main pipeline to the initial heating temperature. The secondary oil temperature control module sets up temperature control devices in the branch pipelines near the oil input direction of each distributed device. It performs input temperature control based on the measured input oil temperature, records and builds a temperature control dataset in real time, which specifically includes the temperature control direction and temperature control amplitude. The oil reflux temperature control module installs reflux temperature control devices on each branch pipeline near the oil collection point. Based on the measured output oil temperature, it identifies the target temperature of the oil collection and calibrates the branch pipelines that need output temperature control, and performs oil reflux temperature control on them. The centralized heating correction module determines whether the initial heating temperature of the main heating pipe needs to be adjusted based on the temperature control dataset. If so, it outputs the adjusted initial heating temperature. The specific analysis method for the initial heating temperature of the centralized heating main pipeline is as follows: The initial heating temperature correction amount for each branch pipeline is obtained by matching the pipeline size with the pipeline size-temperature loss mapping relationship. The initial required temperature of each branch pipeline is obtained by summing the initial heating temperature correction of each branch pipeline with the required temperature of the corresponding distributed equipment. Arrange the initial required temperatures of each branch pipeline from largest to smallest, and select the median as the initial heating temperature of the centralized heating main pipeline. The specific method for identifying the target temperature of the oil collection is as follows: Obtain the measured output oil temperature of each branch pipeline, take the measured output oil temperature of any branch pipeline as the reference output oil temperature, and calculate the sum of the actual temperature adjustment spans of other branch pipelines adjusted to the reference output oil temperature. Calculate the sum of the actual temperature adjustment spans corresponding to the measured output oil temperature of each branch pipeline as the reference output oil temperature; The sum of each actual temperature adjustment span is compared, and the reference output oil temperature corresponding to the smallest sum of actual temperature adjustment spans is selected as the target temperature for oil collection. When performing oil reflux temperature control, it is necessary to determine whether the reflux temperature control equipment has temperature control capability. The specific analysis method is as follows: A1. Calculate the difference between the measured output oil temperature of each branch pipeline and the reference output oil temperature, and then compare it with the maximum temperature control capability of the return flow temperature control equipment of each branch pipeline. A2. If the calculated difference between the measured output oil temperature and the reference output oil temperature of all branch pipelines is less than the maximum temperature control capability of the corresponding reflux temperature control device, the reflux temperature control device is deemed to have temperature control capability. A3. If the calculated difference between the measured output oil temperature and the reference output oil temperature in any branch pipeline is greater than the maximum temperature control capacity of the corresponding reflux temperature control device, then adjust the reference output oil temperature. A4. Re-analyze based on the adjusted reference output oil temperature until the reference output oil temperature is equal to half of the sum of the maximum measured output oil temperature and the minimum measured output oil temperature. If the calculated difference between the measured output oil temperature and the reference output oil temperature of any branch pipeline is still greater than the maximum temperature control capability of the corresponding reflux temperature control device, then it is determined that the reflux temperature control device does not have temperature control capability. B1. Compare the measured output oil temperatures of each branch pipeline, and calculate the difference between the maximum and minimum measured output oil temperatures to obtain the measured output oil temperature range. B2. The maximum temperature control capability is obtained by summing the maximum measured output oil temperature and the minimum measured output oil temperature. B3. Compare the measured output oil temperature range with the maximum temperature control capability limit. If the measured output oil temperature range is greater than the maximum temperature control capability limit, it is determined that the reflux temperature control device does not have temperature control capability; otherwise, it is determined that the reflux temperature control device has temperature control capability.

2. The centralized oil supply and temperature control system for a plastic pipe production workshop as described in claim 1, characterized in that: The specific method for constructing the pipeline size-temperature loss mapping relationship is as follows: Collect pipeline dimension information for each branch pipeline in the plastic pipe production workshop, including key parameters such as pipe length, diameter, and material thickness; Different sizes of branch pipes were selected as test objects. Heat transfer oil at a preset temperature was introduced at the starting point of each test branch pipe, and the oil flow rate was kept stable. Temperature detection devices are installed at the end of each test pipeline to monitor and record the actual temperature of the oil after it flows through the pipeline in real time. The difference between the starting temperature and the ending temperature is calculated to obtain the temperature loss value corresponding to the pipeline size. Replace the test pipes of different sizes, repeat the above operations of inputting preset temperature oil, monitoring the endpoint temperature and calculating temperature loss, and accumulate multiple sets of data on pipeline size and corresponding temperature loss; The collected data were organized to establish the correspondence between pipeline size parameters and temperature loss values, forming a pipeline size-temperature loss mapping relationship.

3. The centralized oil supply and temperature control system for a plastic pipe production workshop as described in claim 1, characterized in that: The specific method for input-side temperature control is as follows: Compare the measured input oil temperature of each branch pipeline with the required temperature of each distributed equipment. If the relative deviation between the measured input oil temperature and the required temperature of the distributed equipment exceeds the limit, it is determined that input end temperature control is required. If the measured input oil temperature is greater than the required temperature of the distribution equipment, the temperature control direction is determined to be cooling, and the difference between the measured input oil temperature and the required temperature of the distribution equipment is recorded as the temperature control amplitude of the corresponding input end temperature control. If the measured input oil temperature is lower than the required temperature of the distribution equipment, the temperature control direction is determined to be heating. The difference between the required temperature of the distribution equipment and the measured input oil temperature is recorded as the temperature control amplitude of the corresponding input terminal temperature control.

4. The centralized oil supply and temperature control system for a plastic pipe production workshop as described in claim 1, characterized in that: The specific method for calibrating the branch that requires output temperature control is as follows: Compare the measured output oil temperature of each branch pipeline with the reference output oil temperature to determine whether the deviation between the measured output oil temperature of each branch pipeline and the reference output oil temperature exceeds the limit. If the measured output oil temperature of a branch pipeline deviates from the reference output oil temperature beyond the limit, then the branch pipeline is marked as a branch pipeline that requires output end temperature control; otherwise, it is determined that output end temperature control is not required. The specific method for determining whether the deviation between the measured output oil temperature and the reference output oil temperature of each branch pipeline exceeds the limit is as follows: calculate the absolute difference between the measured output oil temperature and the reference output oil temperature of each branch pipeline, compare the result with the preset output oil temperature deviation threshold, and if the result is greater than the output oil temperature deviation threshold, it is determined that the deviation between the measured output oil temperature and the reference output oil temperature of the branch pipeline exceeds the limit; otherwise, it is determined that the deviation between the measured output oil temperature and the reference output oil temperature of the branch pipeline does not exceed the limit.

5. A centralized oil supply and temperature control system for a plastic pipe production workshop as described in claim 1, characterized in that: The maximum temperature control capacity of the return flow temperature control equipment for each branch pipeline is determined as follows: Extensive temperature control tests were conducted on the reflux temperature control equipment for each branch pipeline. Heat transfer oil at different temperatures was input, and the temperature was controlled using the reflux temperature control equipment. The output temperature of the heat transfer oil after the actual temperature control test was calculated. The actual temperature control range corresponding to the temperature control test of each return flow temperature control device is obtained by calculating the difference between the temperature of the input heat transfer oil and the temperature of the output heat transfer oil. The maximum temperature control capacity of each branch pipeline's return flow temperature control equipment is obtained by averaging the actual temperature control amplitudes corresponding to the temperature control tests of each return flow temperature control equipment.

6. A centralized oil supply and temperature control system for a plastic pipe production workshop as described in claim 1, characterized in that: The specific method for determining whether the initial heating temperature of the main heating pipeline needs to be adjusted is as follows: Extract the temperature control dataset and obtain the temperature control direction and temperature control amplitude corresponding to each temperature control dataset; The average temperature control amplitude is calculated by averaging the temperature control amplitudes of each temperature control dataset. This average amplitude is then compared with a preset threshold. If the average temperature control amplitude is greater than the preset threshold, it is determined that the initial heating temperature of the main heating pipe needs to be adjusted; otherwise, it is determined that the initial heating temperature of the main heating pipe does not need to be adjusted.

7. A centralized oil supply and temperature control system for a plastic pipe production workshop as described in claim 6, characterized in that: The specific method for adjusting the initial heating temperature after output regulation is as follows: Calculate the average temperature rise amplitude of the temperature control dataset with the temperature control direction of heating, and calculate the average temperature drop amplitude of the temperature control dataset with the temperature control direction of cooling. Compare the average temperature rise amplitude with the average temperature drop amplitude. If the average temperature rise range is greater than the average temperature fall range, the difference between the average temperature rise range and the average temperature fall range is used as the initial heating temperature correction amount. Then, the initial heating temperature and the initial heating temperature correction amount are summed to calculate the adjusted initial heating temperature. If the average temperature rise range is less than the average temperature fall range, the difference between the average temperature rise range and the average temperature fall range is used as the initial heating temperature correction amount. Then, the difference between the initial heating temperature and the initial heating temperature correction amount is used to calculate the adjusted initial heating temperature.

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