Synthetic latex polymerization reaction temperature optimization control method

Abstract

The invention relates to the field of polymerization reactions. A synthetic latex polymerization reaction temperature optimization control method comprises the steps that temperature detection data of a reaction kettle in synthetic latex polymerization reaction are obtained, and the temperature detection data comprise polymerization reaction area real-time distribution temperature, reaction kettle temperature distribution data and heat transfer medium flow data; obtaining a thermal stress index value according to the real-time distribution temperature of the polymerization reaction zone, and generating a reaction zone parameter compensation amount according to the thermal stress index value; and obtaining the uniformity index of the temperature field of the reaction kettle according to the temperature distribution data of the reaction kettle. Through real-time acquisition and coupling analysis of multi-source data such as temperature deviation of a polymerization reaction zone, uniformity of a temperature field in a kettle, flow fluctuation of a heat transfer medium and the like, a multi-dimensional coupling matrix of thermal stress, uniformity and flow fluctuation is constructed, and the limitation of traditional single-parameter control is broken through; and comprehensive evaluation of the reaction heat state, the stirring effect and the heat exchange stability is realized.

Description

Technical Field

[0001] The present application relates to the field of polymerization reaction, and in particular to a method for optimizing and controlling the temperature of a synthetic latex polymerization reaction. Background Art

[0002] The polymerization reaction of synthetic latex (such as styrene-butadiene latex, acrylate latex, etc.) is a typical highly exothermic nonlinear process. Temperature, as the core process parameter, directly affects the polymerization rate, molecular weight distribution, latex stability and product performance.

[0003] Existing technologies for polymerization reactions exhibit phased heat release (e.g., significant differences in heat release rates between the initiation, chain growth, and termination phases). These processes are also influenced by multiple factors, including mixing efficiency and the stability of the heat transfer medium. Traditional single-loop PID control relies solely on single-point temperature feedback in the reactor, unable to address the combined effects of reaction thermal stress, temperature field inhomogeneity, and heat transfer medium fluctuations, easily leading to localized overheating or incomplete reactions. Summary of the Invention

[0004] The present application provides a method for optimizing the control of the temperature of a synthetic latex polymerization reaction to solve the problems of uneven distribution of thermal stress, uncontrolled coupling of heat transfer medium fluctuation and temperature field uniformity in traditional control.

[0005] In a first aspect, the present application provides a method for optimizing and controlling the temperature of a synthetic latex polymerization reaction, which is applied to a reactor and a heat transfer medium flow regulating valve, and the method comprises: Acquiring temperature detection data of the reactor during the polymerization reaction of synthetic latex, wherein the temperature detection data includes real-time distribution temperature of the polymerization reaction zone, temperature distribution data of the reactor, and flow data of the heat transfer medium; Obtaining a thermal stress index value according to the real-time distribution temperature of the polymerization reaction zone, and generating a reaction zone parameter compensation amount according to the thermal stress index value; Obtaining a temperature field uniformity index of the reactor according to the reactor temperature distribution data; obtaining a heat transfer medium flow dynamic index according to the heat transfer medium flow data; Constructing a multi-dimensional coupling matrix based on the reaction zone parameter compensation amount, the reactor temperature field uniformity index, and the heat transfer medium flow dynamic index; Acquiring a temperature control fluctuation value according to the multi-dimensional coupling matrix; Dynamic adjustment information is acquired according to the temperature control fluctuation value, and the heat transfer medium flow regulating valve is adjusted according to the dynamic adjustment information.

[0006] Optionally, the step of obtaining a thermal stress index value according to the real-time distributed temperature of the polymerization reaction zone and generating a reaction zone parameter compensation amount according to the thermal stress index value includes: Acquire real-time temperature distribution data of the material according to the real-time temperature distribution of the polymerization reaction zone, wherein the real-time temperature distribution data of the material includes the real-time temperature value of the material at the uppermost position and the real-time temperature value of the material at the lowermost position; Obtaining a first temperature deviation and a second temperature deviation according to the real-time temperature value of the material at the uppermost position and the real-time temperature value of the material at the lowermost position; Obtaining a first fluctuation rate and a second fluctuation rate corresponding to the polymerization reaction according to the first temperature deviation and the second temperature deviation; Obtaining a temperature fluctuation distortion rate according to the first fluctuation rate and the second fluctuation rate; Obtaining a thermal stress index value according to the temperature fluctuation distortion rate; Obtain the preset heat transfer efficiency of the reactor's external jacket; A reaction zone parameter compensation amount is generated according to the thermal stress index value and a preset heat exchange efficiency.

[0007] Optionally, the step of obtaining a temperature field uniformity index of the reactor according to the temperature distribution data of the reactor includes: Acquire the temperature value of the bottom of the reactor, the temperature value of the middle of the reactor, and the temperature value of the top of the reactor according to the temperature distribution data of the reactor; Obtain an average temperature value according to the temperature value at the bottom of the reactor, the temperature value in the middle of the reactor, and the temperature value at the top of the reactor, and obtain a first kettle body temperature deviation value, a second kettle body temperature deviation value, and a third kettle body temperature deviation value corresponding to the temperature value at the bottom of the reactor, the temperature value in the middle of the reactor, and the temperature value at the top of the reactor according to the average temperature value; Get the preset kettle body temperature difference threshold; The temperature field uniformity index of the reactor is obtained according to the preset reactor body temperature difference threshold, the first reactor body temperature deviation value, the second reactor body temperature deviation value and the third reactor body temperature deviation value.

[0008] Optionally, the step of obtaining a heat transfer medium flow dynamic index according to the heat transfer medium flow data includes: Obtain the number of fluctuations per minute and the maximum offset of the heat transfer medium according to the heat transfer medium flow data; Obtaining an average flow deviation rate according to the heat transfer medium flow data; generating a flow fluctuation factor according to the average flow deviation rate, the number of fluctuations and the maximum offset; Normalizing the flow fluctuation factor to obtain a processed flow fluctuation factor; A heat transfer medium flow dynamic index is obtained according to the processing flow fluctuation factor.

[0009] Optionally, the step of constructing a multi-dimensional coupling matrix according to the reaction zone parameter compensation amount, the reactor temperature field uniformity index, and the heat transfer medium flow dynamic index includes: Obtaining a first coupling coefficient according to a reaction zone parameter compensation amount and a reactor temperature field uniformity index; Obtaining a second coupling coefficient according to the reaction zone parameter compensation amount and the heat transfer medium flow dynamic index; Obtaining a third coupling coefficient according to the reactor temperature field uniformity index and the heat transfer medium flow dynamic index; A multi-dimensional coupling matrix is ​​constructed according to the first coupling coefficient, the second coupling coefficient, and the third coupling coefficient.

[0010] Optionally, the step of obtaining the temperature control fluctuation value according to the multi-dimensional coupling matrix includes: Performing eigenvalue decomposition on the multi-dimensional coupling matrix to obtain the temperature fluctuation eigenvalues ​​and corresponding fluctuation eigenvectors of the multi-dimensional coupling matrix; Obtaining a main eigenvector based on the temperature fluctuation eigenvalue and the corresponding fluctuation eigenvector, and generating a comprehensive eigenvector through linear combination; Obtaining a preset temperature control vector in the aggregation stage, and obtaining cosine similarity based on the preset temperature control vector and the comprehensive feature vector; Get the temperature control fluctuation value based on cosine similarity.

[0011] Optionally, the step of acquiring dynamic adjustment information according to the temperature control fluctuation value includes: Obtaining the proportional factor adjustment amplitude of the controller according to the temperature control fluctuation value; Obtain the change trend based on the temperature control fluctuation value; Obtaining a delay time according to the heat transfer medium flow regulating valve; Generate a flow rate proportional adjustment amplitude and adjustment time according to the change trend, proportional factor adjustment amplitude, and corresponding time; Dynamic adjustment information is obtained according to the flow ratio adjustment amplitude and adjustment time.

[0012] The present invention also discloses a synthetic latex polymerization reaction temperature optimization control system, which is applied to a reaction kettle and a heat transfer medium flow regulating valve, comprising: A data acquisition module is used to obtain temperature detection data of the reactor during the polymerization reaction of synthetic latex, wherein the temperature detection data includes real-time distribution temperature of the polymerization reaction zone, temperature distribution data of the reactor, and flow data of the heat transfer medium; a thermal stress analysis module, configured to obtain a thermal stress index value according to the real-time temperature distribution of the polymerization reaction zone, and generate a reaction zone parameter compensation value according to the thermal stress index value; A uniformity evaluation module is used to obtain a temperature field uniformity index of the reactor based on the temperature distribution data of the reactor; A flow dynamic analysis module, configured to obtain a heat transfer medium flow dynamic index based on the heat transfer medium flow data; A coupling matrix construction module is used to construct a multi-dimensional coupling matrix according to the reaction zone parameter compensation amount, the reactor temperature field uniformity index and the heat transfer medium flow dynamic index; A fluctuation acquisition module, configured to acquire a temperature control fluctuation value according to the multi-dimensional coupling matrix; The valve control module is used to obtain dynamic adjustment information according to the temperature control fluctuation value, and adjust the heat transfer medium flow control valve according to the dynamic adjustment information.

[0013] Optionally, the thermal stress analysis module includes: a temperature distribution acquisition unit, configured to acquire real-time temperature distribution data of the material according to the real-time temperature distribution of the polymerization reaction zone, wherein the real-time temperature distribution data of the material includes the real-time temperature value of the material at the uppermost position and the real-time temperature value of the material at the lowermost position; A temperature deviation calculation unit, configured to obtain a first temperature deviation and a second temperature deviation according to the real-time temperature value of the material at the uppermost position and the real-time temperature value of the material at the lowermost position; A fluctuation rate calculation unit, configured to obtain a first fluctuation rate and a second fluctuation rate corresponding to the polymerization reaction according to the first temperature deviation and the second temperature deviation; a distortion rate calculation unit, configured to obtain a temperature fluctuation distortion rate according to the first fluctuation rate and the second fluctuation rate; a thermal stress calculation unit, configured to obtain a thermal stress index value according to the temperature fluctuation distortion rate; A heat exchange efficiency acquisition unit, used to acquire a preset heat exchange efficiency of the outer jacket of the reactor; The compensation generating unit is used to generate a reaction zone parameter compensation amount according to the thermal stress index value and a preset heat exchange efficiency.

[0014] Optionally, the uniformity assessment module includes: A kettle body temperature acquisition unit is used to acquire the temperature value of the bottom of the reactor, the temperature value of the middle of the reactor, and the temperature value of the top of the reactor according to the temperature distribution data of the reactor; a deviation value calculation unit, configured to obtain an average temperature value according to the reactor bottom temperature value, the reactor middle temperature value, and the reactor top temperature value, and obtain a first kettle body temperature deviation value, a second kettle body temperature deviation value, and a third kettle body temperature deviation value corresponding to the reactor bottom temperature value, the reactor middle temperature value, and the reactor top temperature value according to the average temperature value; A temperature difference threshold value obtaining unit is used to obtain a preset kettle body temperature difference threshold value; The uniformity calculation unit is used to obtain the reactor temperature field uniformity index according to the preset reactor body temperature difference threshold, the first reactor body temperature deviation value, the second reactor body temperature deviation value and the third reactor body temperature deviation value.

[0015] Compared with related technologies, the method for optimizing and controlling the temperature of a synthetic latex polymerization reaction provided by this application has at least the following technical effects: Through real-time collection and coupled analysis of multi-source data such as temperature deviation in the polymerization reaction zone, uniformity of the temperature field in the kettle, and fluctuations in the flow rate of the heat transfer medium, a multi-dimensional coupling matrix of thermal stress, uniformity, and flow fluctuations is constructed, breaking through the limitations of traditional single-parameter control, achieving a comprehensive evaluation of the reaction thermal state, stirring effect, and heat transfer stability, accurately locating the root cause of temperature anomalies, and realizing automated decision-making from temperature anomaly detection to the generation of adjustment instructions, reducing manual intervention and improving production efficiency.

[0016] The details of one or more embodiments of the present application are set forth in the following drawings and description to make other features, objects, and advantages of the present application more readily apparent. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] The drawings described herein are used to provide a further understanding of the present application and constitute a part of the present application. The illustrative embodiments of the present application and their descriptions are used to explain the present application and do not constitute an improper limitation on the present application. In the drawings: Figure 1 This is a flow chart of a method for optimizing the control of polymerization temperature of a synthetic latex according to an exemplary embodiment; Figure 2 It is a system diagram of a method for optimizing the control of the polymerization reaction temperature of synthetic latex according to an exemplary embodiment. DETAILED DESCRIPTION

[0018] In order to make the purpose, technical solutions and advantages of this application more clearly understood, the present application is described and illustrated below in conjunction with the accompanying drawings and examples. It should be understood that the specific embodiments described herein are merely used to explain this application and are not intended to limit this application. Based on the embodiments provided in this application, all other embodiments obtained by those of ordinary skill in the art without making any creative efforts are within the scope of protection of this application.

[0019] Obviously, the drawings described below are merely examples or embodiments of the present application. Those skilled in the art can, without inventive effort, apply the present application to other similar scenarios based on these drawings. Furthermore, it is also understood that, although the effort involved in such a development process may be complex and lengthy, for those skilled in the art related to the content disclosed in this application, changes in design, manufacturing, or production based on the technical content disclosed in this application are merely conventional technical means and should not be construed as an insufficiency of the content disclosed in this application.

[0020] References to "embodiments" in this application mean that a particular feature, structure, or characteristic described in connection with the embodiment may be included in at least one embodiment of the application. The appearance of this phrase in various places in the specification does not necessarily refer to the same embodiment, nor does it refer to independent or alternative embodiments that are mutually exclusive of other embodiments. It is understood, both explicitly and implicitly, by those skilled in the art that the embodiments described in this application may be combined with other embodiments unless there is a conflict.

[0021] Unless otherwise defined, technical or scientific terms used herein shall have the ordinary meaning as understood by persons of ordinary skill in the art to which this application belongs. The terms "a," "an," "an," "the," and similar expressions used herein do not denote quantitative limitations and may refer to either the singular or the plural. The terms "comprise," "include," "have," and any variations thereof, used herein, are intended to cover non-exclusive inclusions. For example, a process, method, system, product, or apparatus comprising a series of steps or modules (units) is not limited to the listed steps or units but may also include steps or units not listed, or may include other steps or units inherent to the process, method, product, or apparatus. The terms "connected," "connected," "coupled," and similar expressions used herein are not limited to physical or mechanical connections but may include electrical connections, whether direct or indirect. As used herein, "plurality" means two or more. "And / or" describes an association between associated objects, indicating that three possible relationships exist. For example, "A and / or B" may mean: A exists alone; A and B exist simultaneously; or B exists alone. The character " / " generally indicates that the objects before and after are in an "or" relationship. The terms "first", "second", "third", etc. involved in this application are only used to distinguish similar objects and do not represent a specific order for the objects.

[0022] Example 1 An embodiment of the present invention provides a method for optimizing and controlling the temperature of a synthetic latex polymerization reaction. Figure 1is a flow chart of a method according to an exemplary embodiment. Applied to a reactor and a heat transfer medium flow regulating valve, such as Figure 1 As shown, the method includes: Step S101, obtaining temperature detection data of a reactor during a synthetic latex polymerization reaction, wherein the temperature detection data includes real-time distribution temperature of the polymerization reaction zone, temperature distribution data of the reactor, and flow data of a heat transfer medium; Step S102: obtaining a thermal stress index value according to the real-time temperature distribution of the polymerization reaction zone, and generating a reaction zone parameter compensation amount according to the thermal stress index value; Step S103, obtaining a temperature field uniformity index of the reactor according to the temperature distribution data of the reactor; Step S104: obtaining a heat transfer medium flow dynamic index according to the heat transfer medium flow data; Step S105: constructing a multi-dimensional coupling matrix according to the reaction zone parameter compensation amount, the reactor temperature field uniformity index, and the heat transfer medium flow dynamic index; Step S106: obtaining a temperature control fluctuation value according to the multi-dimensional coupling matrix; Step S107: acquiring dynamic adjustment information according to the temperature control fluctuation value, and adjusting the heat transfer medium flow regulating valve according to the dynamic adjustment information.

[0023] In summary, the present invention first obtains temperature detection data of the reactor during the synthetic latex polymerization reaction, including the real-time distribution temperature of the polymerization reaction zone, the reactor temperature distribution data, and the heat transfer medium flow rate data. The real-time distribution temperature of the polymerization reaction zone is collected by thermocouples at different heights of the material layer in the reactor, which is used to reflect the temperature state of the core reaction area; the reactor temperature distribution data is obtained by temperature sensors at the bottom, middle, and top of the reactor body, which is used to evaluate the material temperature uniformity and stirring and mixing effect; the heat transfer medium flow rate data is monitored by an electromagnetic flowmeter on the jacket or coil pipe, which reflects the flow stability of media such as thermal oil and cooling water, and is directly related to the heat exchange efficiency; Next, the thermal stress index is calculated based on the real-time temperature distribution of the polymerization reaction zone, and compensation for the reaction zone parameters is generated. The upper and lower material temperatures are extracted from the real-time temperature distribution, and their deviation from the process setpoint temperature for the corresponding stage is calculated. This deviation is then converted into a fluctuation rate. The difference in fluctuation rates is analyzed to determine the temperature fluctuation distortion rate. A higher distortion rate indicates a more unstable reaction thermal state. Combined with the preset heat transfer efficiency of the reactor jacket (determined by factors such as jacket cleanliness and medium flow rate), an algorithm is used to generate compensation for the reaction zone parameters, which are then used to adjust subsequent control parameters to address thermal stress.

[0024] The temperature field uniformity index is then calculated based on the reactor temperature distribution data. The bottom, middle, and top temperatures are extracted and averaged to obtain the deviations from the average for each location. A preset reactor temperature difference threshold (set according to the process stage) is introduced to calculate the uniformity index using a formula. A lower index indicates a more uneven temperature distribution, which may require improvement, such as adjusting the stirring speed.

[0025] The flow dynamics index is then generated based on the heat transfer medium flow data. The number of flow fluctuations per minute and the maximum offset are counted, and the deviation rate between the average flow rate and the rated flow rate is calculated. The deviation rate, number of fluctuations, and offset are then combined to form a flow fluctuation factor. After normalization, the flow dynamics index is obtained and used to evaluate flow stability.

[0026] A multidimensional coupling matrix is ​​then constructed, integrating the reaction zone parameter compensation, temperature field uniformity index, and flow dynamic index. The first coupling coefficient between reaction thermal stress and uniformity, the second coupling coefficient between thermal stress and flow fluctuation, and the third coupling coefficient between uniformity and flow fluctuation are calculated. These three coefficients are combined with the identity matrix to form a coupling matrix, which is used to analyze the interactions of multidimensional data.

[0027] The temperature control fluctuation value is obtained by performing eigenvalue decomposition on the coupling matrix. The main eigenvector is extracted and a comprehensive eigenvector is generated. The cosine similarity is calculated with the preset temperature control vector (set during the aggregation phase). The similarity reflects the difference between the current state and the target state. The temperature control fluctuation value is then calculated based on this similarity. A larger fluctuation value indicates a larger adjustment is required.

[0028] Finally, dynamic adjustment information is generated based on the temperature control fluctuation value. The controller proportional factor adjustment range is determined based on the fluctuation value, and the integral time constant is adjusted according to the fluctuation trend. The flow proportional adjustment range and adjustment time are generated based on the control valve response time. The adjustment information is converted into a command to control the control valve, achieving dynamic temperature regulation.

[0029] In one embodiment, step S102 specifically includes: Step S1021: acquiring real-time temperature distribution data of the material according to the real-time temperature distribution of the polymerization reaction zone, wherein the real-time temperature distribution data of the material includes the real-time temperature value of the material at the uppermost position and the real-time temperature value of the material at the lowermost position; Step S1022: obtaining a first temperature deviation and a second temperature deviation according to the real-time temperature value of the material at the uppermost position and the real-time temperature value of the material at the lowermost position; Step S1023, obtaining a first fluctuation rate and a second fluctuation rate corresponding to the polymerization reaction according to the first temperature deviation and the second temperature deviation; Step S1024: Obtain a temperature fluctuation distortion rate according to the first fluctuation rate and the second fluctuation rate; Step S1025: obtaining a thermal stress index value according to the temperature fluctuation distortion rate; Step S1026: Obtain the preset heat exchange efficiency of the outer jacket of the reactor; Step S1027: generating a reaction zone parameter compensation amount according to the thermal stress index value and the preset heat exchange efficiency.

[0030] The present invention first obtains the real-time temperature distribution data of the material in the real-time distribution temperature of the polymerization reaction zone through a preset temperature sensor network in the reactor in step S1021. The data specifically includes the real-time temperature value of the material at the uppermost position and the real-time temperature value of the material at the lowermost position in the reactor. These two positions usually correspond to the area below the material liquid surface and close to the bottom of the reactor, respectively, and are used to capture the temperature distribution characteristics in the vertical direction of the reaction zone, providing a basis for analyzing the difference in thermal states between the upper and lower layers.

[0031] In step S1022, the real-time temperatures of the uppermost and lowermost materials are compared with the set temperature for the current polymerization stage, and the difference between the two is calculated to obtain a first temperature deviation and a second temperature deviation. These two deviation indicators measure the absolute degree to which the temperatures of the upper and lower materials deviate from the process target. For example, if the upper temperature is higher than the set temperature, the first deviation is positive; otherwise, it is negative. The same applies to the lower temperature. The positive and negative values ​​and the magnitude of the values ​​can be used to directly determine whether the upper and lower temperatures are overheated or underheated, as well as the degree of deviation.

[0032] In step S1023, the first and second temperature deviations are converted into relative ratio indicators, namely, the first and second fluctuation ratios. Specifically, the respective deviations are divided by the process set temperature to obtain the fluctuation ratio relative to the set temperature. This conversion makes the deviations under different temperature settings comparable. For example, regardless of whether the set temperature is 50°C or 80°C, the fluctuation ratio can reflect the relative severity of the fluctuation, facilitating a unified assessment of temperature stability across different polymerization stages.

[0033] In step S1024, the temperature fluctuation distortion rate is calculated by analyzing the difference between the first fluctuation rate and the second fluctuation rate to obtain the preset process temperature value, wherein the calculation formula is: ,in, represents the temperature fluctuation distortion rate, represents the first volatility, represents the second volatility, Represents the preset process temperature value. Specifically, the absolute value of the difference between the two values ​​is calculated. A larger value indicates a more significant inconsistency in the temperature fluctuations of the upper and lower layers. This may indicate thermal stratification or poor stirring within the reactor, resulting in insufficient mixing and uneven heat distribution. For example, if the fluctuation rate of the upper layer is +5% and the lower layer is -3%, the distortion rate is 8%, indicating that attention should be paid to the stirring system or heat exchange efficiency.

[0034] In step S1025, a thermal stress index value is obtained based on the magnitude of the temperature fluctuation distortion rate using a pre-established correspondence. Generally, a higher distortion rate indicates a larger thermal stress index value, indicating a greater impact of reaction heat on system stability and requiring more significant control measures to maintain temperature balance. This index value is a key parameter for measuring the stability of the current reaction thermal state and provides a basis for subsequent compensation calculations.

[0035] In step S1026, the preset heat exchange efficiency of the external jacket of the reactor is obtained. This efficiency value is an inherent parameter reflecting the heat transfer capacity of the jacket and is affected by factors such as the cleanliness of the interior of the jacket, the flow rate of the heat transfer medium, and the contact area between the jacket and the material. It can be determined based on test data or historical operating data during the equipment commissioning phase and is used to correct the actual effect of thermal stress compensation. For example, a jacket with high heat exchange efficiency requires less compensation under the same thermal stress, while a jacket with low heat exchange efficiency requires a larger compensation.

[0036] In step S1027, the thermal stress index value is combined with the preset heat transfer efficiency to comprehensively calculate and generate the reaction zone parameter compensation amount. The specific process is to determine the direction and amplitude of the control parameter that needs to be adjusted based on the thermal stress index value, and then multiply it by the heat transfer efficiency coefficient to obtain the final compensation amount. For example, if the thermal stress index value shows that the cooling amount needs to be increased and the heat transfer efficiency is high, the compensation amount is relatively small; if the heat transfer efficiency is low, the compensation amount needs to be increased to overcome the insufficient heat transfer. This compensation amount will be used to adjust the subsequent fuzzy PID controller parameters, such as the proportional factor, integral time constant, etc., to achieve dynamic adjustment of the heat transfer medium flow or stirring speed to cope with the current abnormal thermal state.

[0037] Continue to refer to Figure 1 , after step S102, step S103 is performed, specifically as follows: Step S1031, obtaining the temperature value of the bottom of the reactor, the temperature value of the middle of the reactor, and the temperature value of the top of the reactor according to the temperature distribution data of the reactor; Step S1032: obtaining an average temperature value according to the reactor bottom temperature value, the reactor middle temperature value, and the reactor top temperature value, and obtaining a first kettle body temperature deviation value, a second kettle body temperature deviation value, and a third kettle body temperature deviation value corresponding to the reactor bottom temperature value, the reactor middle temperature value, and the reactor top temperature value according to the average temperature value; Step S1033, obtaining a preset kettle body temperature difference threshold; Step S1034: Obtaining a temperature field uniformity index of the reactor according to the preset reactor body temperature difference threshold, the first reactor body temperature deviation value, the second reactor body temperature deviation value, and the third reactor body temperature deviation value.

[0038] In step S1031 of the present invention, the temperature values ​​of the bottom, middle and top of the reactor are obtained through a temperature sensor network pre-arranged in the reactor. These sensors are usually installed at a certain distance from the bottom of the reactor body, at the geometric center of the middle, and at the top near the liquid surface. They are used to collect real-time material temperature data at different heights in the vertical direction of the reactor, providing basic data support for analyzing the uniformity of temperature distribution in the reactor.

[0039] In step S1032, an average temperature value is first calculated based on the acquired bottom, middle, and top temperature values. Specifically, the temperature values ​​at these three locations are added together and the arithmetic mean is taken. This average temperature value reflects the overall temperature level of the material within the reactor. Next, the temperature value at each location is subtracted from the average temperature value to obtain the corresponding first reactor body temperature deviation value (bottom), second reactor body temperature deviation value (middle), and third reactor body temperature deviation value (top). These deviation values ​​are used to measure the degree of deviation of the temperature at each location from the overall average temperature. A positive deviation indicates that the temperature at that location is above the average temperature, while a negative deviation indicates that the temperature is below the average temperature. The magnitude and sign of the deviation value can be used to intuitively determine whether there is local overheating or underheating within the reactor.

[0040] In step S1033, a preset kettle body temperature difference threshold is obtained. This threshold is pre-set based on the process requirements of different stages of the synthetic latex polymerization reaction. For example, during the latex particle formation stage, the threshold may be set to a lower value due to the high requirement for temperature uniformity. However, during the chain growth stage, the threshold may be appropriately relaxed based on the reaction characteristics. This threshold serves as a benchmark for determining whether the temperature distribution is uniform and is used in the subsequent calculation and evaluation of the uniformity index.

[0041] In step S1034, the reactor temperature field uniformity index is obtained according to the preset reactor body temperature difference threshold, the first reactor body temperature deviation value, the second reactor body temperature deviation value, and the third reactor body temperature deviation value. The reactor temperature field uniformity index is calculated as follows: ,in, Represents the temperature field uniformity index of the reactor, Indicates the temperature deviation value of the i-th kettle body, Represents the preset kettle temperature difference threshold. The specific process is to first calculate the squares of the three kettle temperature deviation values ​​and add them together to obtain the sum of the squared deviations, which reflects the overall degree of deviation of the temperature at each location from the average temperature. Then, the sum of the squared deviations is divided by three times the square of the preset kettle temperature difference threshold to obtain a normalized value. Finally, this value is subtracted from 1 to obtain the temperature field uniformity index. The uniformity index typically ranges from 0 to 1. Values ​​closer to 1 indicate a more uniform temperature distribution, while values ​​lower than 1 indicate greater temperature variability.

[0042] In terms of data synergy, the bottom, middle, and top temperature values ​​are the basic inputs. The overall temperature benchmark is determined by calculating the average temperature value. The deviation value at each location reveals the difference between the local temperature and the overall temperature. The preset temperature difference threshold of the kettle body provides a standard for judging whether the difference is reasonable. The uniformity index is a quantitative evaluation result obtained by integrating these data. For example, in a certain polymerization reaction stage, if the bottom temperature value is low and the middle and top temperature values ​​are high, the calculated average temperature value may be close to the process set temperature, but the deviation value at each location is large, resulting in a large sum of squared deviations, which in turn leads to a low uniformity index. This indicates that although the overall temperature meets the requirements, the vertical temperature distribution is uneven, which may be caused by poor stirring effect or uneven distribution of heat transfer medium. At this time, the system can trigger corresponding adjustment measures based on the uniformity index, such as increasing the stirring speed to promote material mixing, or adjusting the heat transfer medium flow rate to improve local heat exchange, thereby improving the temperature field uniformity index and ensuring that the reaction proceeds in a uniform temperature environment.

[0043] Continue to refer to Figure 1 , after step S103, step S104 is performed, specifically as follows: Step S1041: Obtain the number of fluctuations per minute and the maximum offset of the heat transfer medium according to the heat transfer medium flow data; Step S1042: obtaining an average flow deviation rate according to the heat transfer medium flow data; Step S1043: Generate a flow fluctuation factor according to the average flow deviation rate, the number of fluctuations, and the maximum offset; Step S1044: normalize the flow fluctuation factor to obtain a processed flow fluctuation factor; Step S1045: Obtain a heat transfer medium flow dynamic index according to the processing flow fluctuation factor.

[0044] The present invention first collects flow data in real time in step S1041 using an electromagnetic flowmeter installed on the heat transfer medium pipeline. This data monitors flow rate variations per unit time and extracts the number of fluctuations per minute and the maximum offset. Fluctuations are calculated based on how often the flow curve crosses a preset baseline, typically set at the rated flow rate, with each crossing considered a fluctuation. The maximum offset is calculated by comparing the absolute value of the difference between the real-time flow rate and the rated flow rate, reflecting the maximum degree to which the flow rate deviates from the process setpoint during fluctuations. Together, these two parameters characterize the frequency and amplitude of flow fluctuations.

[0045] In step S1042, the average flow rate is calculated based on the continuously collected flow data over a period of time and compared with the rated flow rate. The average flow rate deviation rate is calculated by calculating the ratio of the difference between the two to the rated flow rate. This deviation rate is used to assess the overall deviation trend of the flow rate over a longer period of time. If the deviation rate is positive, it means that the average flow rate is higher than the rated value, which may lead to excessive heat transfer; if it is negative, it means that the average flow rate is insufficient, which may cause untimely cooling or heating. This parameter can be used to preliminarily determine the overall balance of the flow supply.

[0046] In step S1043, the average flow deviation rate, number of fluctuations, and maximum offset are comprehensively processed to generate a flow fluctuation factor. Specifically, the number of fluctuations and maximum offset are first standardized to have the same dimension as the average flow deviation rate. Then, weights are assigned to each parameter based on the sensitivity of the polymerization reaction to each fluctuation factor at different stages. For example, in the early stages of the reaction, when flow deviation is more sensitive, the weight of the average flow deviation rate can be increased. Finally, the weighted sum of the parameters is used to generate the flow fluctuation factor. This factor integrates multi-dimensional flow fluctuation characteristics and quantifies the comprehensive impact of flow fluctuations.

[0047] In step S1044, the generated flow fluctuation factor is normalized to obtain a processed flow fluctuation factor. The purpose of normalization is to eliminate dimensional differences in data between different production batches or different devices, making the fluctuation factors comparable. Specifically, the maximum and minimum values ​​of the flow fluctuation factor are determined based on historical production data. The currently calculated fluctuation factor is converted to a range of 0 to 1 through linear mapping. The converted processed flow fluctuation factor can intuitively reflect the severity of the current flow fluctuation relative to historical fluctuations, facilitating the standardization of evaluation criteria.

[0048] In step S1045, a heat transfer medium flow dynamics index is obtained based on the process flow fluctuation factor. This index directly reflects the fluctuation state of the heat transfer medium flow and is positively correlated with the process flow fluctuation factor. The process flow fluctuation factor can typically be used directly as the flow dynamics index or generated through a simple linear transformation. The flow dynamics index, the final evaluation result, is input into the control system. When the index exceeds a preset threshold, the system triggers appropriate regulatory measures, such as adjusting pump speed, switching to a backup pump group, or adjusting valve opening, to stabilize the heat transfer medium flow and ensure that the polymerization reaction proceeds in a stable thermal environment.

[0049] Continue to refer to Figure 1 , after step S104, step S105 is performed, specifically as follows: Step S1051: obtaining a first coupling coefficient according to the reaction zone parameter compensation amount and the reactor temperature field uniformity index; Step S1052: Obtain a second coupling coefficient based on the reaction zone parameter compensation amount and the heat transfer medium flow dynamic index; Step S1053: obtaining a third coupling coefficient according to the temperature field uniformity index of the reactor and the heat transfer medium flow dynamic index; Step S1054: construct a multi-dimensional coupling matrix according to the first coupling coefficient, the second coupling coefficient, and the third coupling coefficient.

[0050] The present invention constructs a multi-dimensional parameter coupling analysis framework in steps S1051 to S1054, providing a basis for collaborative optimization of the system by quantifying the interactions between different control factors. In step S1051, the system correlates the reaction zone parameter compensation amount with the reactor temperature field uniformity index. The reaction zone parameter compensation amount is derived from the results of the previous thermal stress assessment and reflects the adjustment required to the control parameters to balance the reaction heat. The reactor temperature field uniformity index quantifies the degree of temperature balance within the reactor. By mathematically correlating the two, a first coupling coefficient is obtained. This coefficient is used to measure the intensity of the mutual influence between the thermal stress compensation operation and the temperature field uniformity. If the uniformity index decreases while the compensation amount increases, it indicates that the current thermal compensation strategy may exacerbate the uneven temperature distribution and the compensation method needs to be re-evaluated.

[0051] In step S1052, the system performs a coupling analysis on the reaction zone parameter compensation amount and the heat transfer medium flow dynamic index. The heat transfer medium flow dynamic index reflects the fluctuation state of the heat transfer medium flow. By correlating it with the reaction zone parameter compensation amount, a second coupling coefficient is obtained. This coefficient reveals the intrinsic connection between the thermal stress compensation demand and the stability of the heat transfer medium. If both increase at the same time, it means that the instability of the heat transfer medium flow may affect the thermal compensation effect, and it is necessary to prioritize stabilizing the flow to improve control accuracy.

[0052] In step S1053, the system focuses on the correlation between the reactor temperature field uniformity index and the heat transfer medium flow dynamic index. By analyzing the interaction between the two, the third coupling coefficient is obtained. This coefficient is used to evaluate the degree of coupling between the temperature distribution uniformity and the heat transfer medium flow stability. If the uniformity index is low when the flow fluctuation is large, it indicates that the unstable flow may lead to local uneven heat exchange, thereby affecting the overall temperature distribution.

[0053] In step S1054, the system integrates the first, second, and third coupling coefficients to construct a multi-dimensional coupling matrix. The matrix presents the interaction relationship between the three key parameters in a structured manner. The main diagonal elements of the matrix are all set to 1, indicating that the parameters themselves are completely correlated, while the non-diagonal elements are the corresponding coupling coefficients, reflecting the correlation strength between different parameters. By analyzing the numerical size of each element in the matrix, the key coupling relationship that dominates the behavior of the entire system can be identified.

[0054] During the entire data processing process, the three core parameters, namely the reaction zone parameter compensation, the reactor temperature field uniformity index, and the heat transfer medium flow dynamic index, are first obtained through the preliminary steps. Then, the coupling coefficients between them are calculated respectively. These coefficients not only quantify the degree of correlation between the parameters, but also indicate the direction of correlation through positive and negative values. For example, a positive coupling coefficient indicates that the change trends of the two parameters are consistent, while a negative coupling coefficient indicates that the change trends are opposite. Finally, these coefficients are organized into a matrix form, making the complex relationship between multi-dimensional parameters intuitive and easy to analyze.

[0055] Continue to refer to Figure 1 , after step S105, step S106 is performed, specifically as follows: Step S1061: Perform eigenvalue decomposition on the multi-dimensional coupling matrix to obtain the temperature fluctuation eigenvalues ​​and corresponding fluctuation eigenvectors of the multi-dimensional coupling matrix; Step S1062: Obtain a main eigenvector based on the temperature fluctuation eigenvalue and the corresponding fluctuation eigenvector, and generate a comprehensive eigenvector through linear combination; Step S1063: obtaining a preset temperature control vector in the aggregation stage, and obtaining cosine similarity based on the preset temperature control vector and the comprehensive feature vector; Step S1064: Obtain the temperature control fluctuation value according to the cosine similarity.

[0056] In the present invention, first in step S1061, the system performs eigenvalue decomposition on the multi-dimensional coupling matrix from step S1054. This process decomposes the matrix into a set of eigenvalues ​​and corresponding eigenvectors, where the eigenvalues ​​represent the energy intensity of each fluctuation mode, and the eigenvectors correspond to specific fluctuation modes. Through this decomposition, the system can extract potential sources of periodic or abnormal fluctuations from complex coupling relationships, providing a basis for subsequent analysis.

[0057] In step S1062, the system obtains the main eigenvector based on the eigenvalue decomposition result and generates a comprehensive eigenvector. The main eigenvector is the eigenvector corresponding to the largest eigenvalue, which represents the dominant fluctuation mode. The system will select the first several main eigenvectors, calculate the weight coefficient according to the size of their eigenvalues, and then generate a comprehensive eigenvector through weighted linear combination. The vector integrates multi-dimensional fluctuation information, can comprehensively describe the fluctuation characteristics of the system, and provide a unified representation for subsequent comparison with the ideal control mode.

[0058] In step S1063, the system obtains the preset temperature control vector of the polymerization stage and compares it with the comprehensive feature vector. The preset temperature control vector is set based on the polymerization process standard and represents the ideal temperature fluctuation pattern. The system measures the degree of matching between the actual fluctuation pattern and the ideal control pattern by calculating the cosine similarity of the two vectors. The cosine similarity is calculated by the dot product of the vectors. The closer its value is to 1, the more consistent the directions of the two vectors are, that is, the more the actual fluctuation pattern is in line with expectations.

[0059] In step S1064, the system obtains the temperature control fluctuation value based on the cosine similarity. This process maps the cosine similarity into an intuitive fluctuation index. By subtracting the cosine similarity from 1, the difference obtained is the temperature control fluctuation value. The smaller the value, the closer the actual fluctuation is to the ideal state and the better the performance of the control system. Through this mapping, the system converts the abstract vector similarity into a quantitative index that can be directly used for control decision-making.

[0060] During the entire data processing process, the multi-dimensional coupling matrix is ​​first converted into a series of physically meaningful fluctuation patterns through eigenvalue decomposition. Each pattern is described by an eigenvalue and an eigenvector. Then, by selecting the main eigenvectors and weighted combination, the complex multi-dimensional fluctuation information is integrated into a single comprehensive eigenvector. This process not only simplifies the data representation, but also retains the most important fluctuation characteristics. Then, through the cosine similarity calculation with the preset temperature control vector, the system can evaluate the degree of match between the current fluctuation pattern and the ideal pattern. This evaluation method does not rely on the specific amplitude of the fluctuation, but focuses on the pattern characteristics of the fluctuation. Finally, through a simple mapping operation, the similarity is converted into an intuitive fluctuation value, providing a clear control basis for the control system.

[0061] Continue to refer to Figure 1 , after step S106, step S107 is performed, specifically as follows: Step S1071, obtaining the proportional factor adjustment amplitude of the controller according to the temperature control fluctuation value; Step S1072: Obtain a change trend according to the temperature control fluctuation value; Step S1073, obtaining a delay time according to the heat transfer medium flow regulating valve; Step S1074: Generate a flow rate proportional adjustment amplitude and adjustment time according to the change trend, proportional factor adjustment amplitude, and corresponding time; Step S1075: Acquire dynamic adjustment information according to the flow ratio adjustment amplitude and adjustment time.

[0062] In the present invention, first, in step S1071, the system obtains the proportional factor adjustment amplitude of the controller based on the temperature control fluctuation value obtained in step S1064. This process is achieved by establishing a mapping relationship between the fluctuation value and the proportional factor adjustment amplitude. The larger the fluctuation value, the larger the corresponding proportional factor adjustment amplitude, thereby enhancing the system's response capability to temperature fluctuations and enabling the controller to dynamically adjust the control parameters according to the degree of fluctuation.

[0063] In step S1072, the system analyzes the changing trend of the temperature control fluctuation value, and obtains the changing trend information by collecting the fluctuation values ​​at multiple consecutive time points and calculating their slopes. This information is used to predict the development direction of the fluctuation. If the trend is positive, it means that the fluctuation is tending to intensify, and the system needs to take intervention measures in advance. If the trend is negative, the adjustment force can be appropriately slowed down to avoid over-adjustment.

[0064] In step S1073, the system obtains the response time of the heat transfer medium flow control valve. This process is based on the historical operation data of the control valve, analyzes the relationship between the change in valve opening and the response time, and establishes a response time model. The model quantifies the inertia delay characteristics of the control valve, provides a basis for the subsequent calculation of the adjustment time, and ensures that the system can take into account the physical limitations of the actuator and avoid overshoot or undershoot of adjustment due to response delay.

[0065] In step S1074, the system integrates the proportional factor adjustment amplitude, change trend and control valve response time to generate the flow proportional adjustment amplitude and adjustment time. The calculation of the flow proportional adjustment amplitude combines the proportional factor adjustment amplitude and change trend, so that the adjustment amplitude can be dynamically adjusted according to the development trend of the fluctuation. The calculation of the adjustment time is based on the control valve response time model, and takes into account the influence of the change trend. When the fluctuation intensifies, the adjustment time is appropriately extended to balance the response speed and stability.

[0066] In step S1075, the system integrates the flow ratio adjustment amplitude and adjustment time into dynamic adjustment information. This process converts the calculated abstract parameters into directly executable control instructions for the regulating valve, including information such as valve ID, adjustment amplitude, adjustment time and execution timestamp, forming a complete control scheme for the regulating valve, which is used to drive the actuator to achieve precise adjustment of the heat transfer medium flow.

[0067] Example 2 Example 2 of the present invention provides a synthetic latex polymerization reaction temperature optimization control system. Figure 2 FIG. 1 is a system block diagram according to an exemplary embodiment. Figure 2 As shown, a synthetic latex polymerization reaction temperature optimization control system comprises: Data acquisition module 1, used to obtain temperature detection data of the reactor during the polymerization reaction of synthetic latex, wherein the temperature detection data includes real-time distribution temperature of the polymerization reaction zone, temperature distribution data of the reactor, and flow data of the heat transfer medium; Thermal stress analysis module 2, used to obtain a thermal stress index value according to the real-time temperature distribution of the polymerization reaction zone, and generate a reaction zone parameter compensation value according to the thermal stress index value; A uniformity evaluation module 3 is used to obtain a temperature field uniformity index of the reactor based on the temperature distribution data of the reactor; A flow dynamic analysis module 4 is used to obtain a heat transfer medium flow dynamic index based on the heat transfer medium flow data; A coupling matrix construction module 5 is used to construct a multi-dimensional coupling matrix according to the reaction zone parameter compensation amount, the reactor temperature field uniformity index and the heat transfer medium flow dynamic index; Fluctuation acquisition module 6, used to obtain temperature control fluctuation value according to the multi-dimensional coupling matrix; The valve control module 7 is configured to obtain dynamic adjustment information according to the temperature control fluctuation value, and adjust the heat transfer medium flow regulating valve according to the dynamic adjustment information.

[0068] In one embodiment, the thermal stress analysis module 2 includes: a temperature distribution acquisition unit, configured to acquire real-time temperature distribution data of the material according to the real-time temperature distribution of the polymerization reaction zone, wherein the real-time temperature distribution data of the material includes the real-time temperature value of the material at the uppermost position and the real-time temperature value of the material at the lowermost position; A temperature deviation calculation unit, configured to obtain a first temperature deviation and a second temperature deviation according to the real-time temperature value of the material at the uppermost position and the real-time temperature value of the material at the lowermost position; A fluctuation rate calculation unit, configured to obtain a first fluctuation rate and a second fluctuation rate corresponding to the polymerization reaction according to the first temperature deviation and the second temperature deviation; a distortion rate calculation unit, configured to obtain a temperature fluctuation distortion rate according to the first fluctuation rate and the second fluctuation rate; a thermal stress calculation unit, configured to obtain a thermal stress index value according to the temperature fluctuation distortion rate; A heat exchange efficiency acquisition unit, used to acquire a preset heat exchange efficiency of the outer jacket of the reactor; The compensation generating unit is used to generate a reaction zone parameter compensation amount according to the thermal stress index value and a preset heat exchange efficiency.

[0069] In one embodiment, the uniformity assessment module 3 includes: A kettle body temperature acquisition unit is used to acquire the temperature value of the bottom of the reactor, the temperature value of the middle of the reactor, and the temperature value of the top of the reactor according to the temperature distribution data of the reactor; a deviation value calculation unit, configured to obtain an average temperature value according to the reactor bottom temperature value, the reactor middle temperature value, and the reactor top temperature value, and obtain a first kettle body temperature deviation value, a second kettle body temperature deviation value, and a third kettle body temperature deviation value corresponding to the reactor bottom temperature value, the reactor middle temperature value, and the reactor top temperature value according to the average temperature value; A temperature difference threshold value obtaining unit is used to obtain a preset kettle body temperature difference threshold value; The uniformity calculation unit is used to obtain the reactor temperature field uniformity index according to the preset reactor body temperature difference threshold, the first reactor body temperature deviation value, the second reactor body temperature deviation value and the third reactor body temperature deviation value.

Claims

1. A method for optimizing and controlling the temperature of a synthetic latex polymerization reaction, applied to a reactor and a heat transfer medium flow regulating valve, characterized in that: The method comprises: Acquiring temperature detection data of the reactor during the polymerization reaction of synthetic latex, wherein the temperature detection data includes real-time distribution temperature of the polymerization reaction zone, temperature distribution data of the reactor, and flow data of the heat transfer medium; Obtaining a thermal stress index value according to the real-time distribution temperature of the polymerization reaction zone, and generating a reaction zone parameter compensation amount according to the thermal stress index value; Obtaining a temperature field uniformity index of the reactor according to the reactor temperature distribution data; obtaining a heat transfer medium flow dynamic index according to the heat transfer medium flow data; Constructing a multi-dimensional coupling matrix based on the reaction zone parameter compensation amount, the reactor temperature field uniformity index, and the heat transfer medium flow dynamic index; Acquiring a temperature control fluctuation value according to the multi-dimensional coupling matrix; Dynamic adjustment information is acquired according to the temperature control fluctuation value, and the heat transfer medium flow regulating valve is adjusted according to the dynamic adjustment information.

2. The method for optimizing and controlling the polymerization reaction temperature of synthetic latex according to claim 1, wherein: The step of obtaining a thermal stress index value according to the real-time distributed temperature of the polymerization reaction zone and generating a reaction zone parameter compensation amount according to the thermal stress index value comprises: Acquire real-time temperature distribution data of the material according to the real-time temperature distribution of the polymerization reaction zone, wherein the real-time temperature distribution data of the material includes the real-time temperature value of the material at the uppermost position and the real-time temperature value of the material at the lowermost position; Obtaining a first temperature deviation and a second temperature deviation according to the real-time temperature value of the material at the uppermost position and the real-time temperature value of the material at the lowermost position; Obtaining a first fluctuation rate and a second fluctuation rate corresponding to the polymerization reaction according to the first temperature deviation and the second temperature deviation; Obtaining a temperature fluctuation distortion rate according to the first fluctuation rate and the second fluctuation rate; Obtaining a thermal stress index value according to the temperature fluctuation distortion rate; Obtain the preset heat transfer efficiency of the reactor's external jacket; A reaction zone parameter compensation amount is generated according to the thermal stress index value and a preset heat exchange efficiency.

3. The method for optimizing and controlling the polymerization temperature of synthetic latex according to claim 1, wherein: The step of obtaining the reactor temperature field uniformity index according to the reactor temperature distribution data includes: Acquire the temperature value of the bottom of the reactor, the temperature value of the middle of the reactor, and the temperature value of the top of the reactor according to the temperature distribution data of the reactor; Obtain an average temperature value according to the temperature value at the bottom of the reactor, the temperature value in the middle of the reactor, and the temperature value at the top of the reactor, and obtain a first kettle body temperature deviation value, a second kettle body temperature deviation value, and a third kettle body temperature deviation value corresponding to the temperature value at the bottom of the reactor, the temperature value in the middle of the reactor, and the temperature value at the top of the reactor according to the average temperature value; Get the preset kettle body temperature difference threshold; The temperature field uniformity index of the reactor is obtained according to the preset reactor body temperature difference threshold, the first reactor body temperature deviation value, the second reactor body temperature deviation value and the third reactor body temperature deviation value.

4. The method for optimizing and controlling the polymerization reaction temperature of synthetic latex according to claim 1, wherein: The step of obtaining a heat transfer medium flow dynamic index according to the heat transfer medium flow data includes: Obtain the number of fluctuations per minute and the maximum offset of the heat transfer medium according to the heat transfer medium flow data; Obtaining an average flow deviation rate according to the heat transfer medium flow data; generating a flow fluctuation factor according to the average flow deviation rate, the number of fluctuations and the maximum offset; Normalizing the flow fluctuation factor to obtain a processed flow fluctuation factor; A heat transfer medium flow dynamic index is obtained according to the processing flow fluctuation factor.

5. The method for optimizing and controlling the polymerization reaction temperature of synthetic latex according to claim 1, wherein: The step of constructing a multi-dimensional coupling matrix according to the reaction zone parameter compensation amount, the reactor temperature field uniformity index, and the heat transfer medium flow dynamic index includes: Obtaining a first coupling coefficient according to a reaction zone parameter compensation amount and a reactor temperature field uniformity index; Obtaining a second coupling coefficient according to the reaction zone parameter compensation amount and the heat transfer medium flow dynamic index; Obtaining a third coupling coefficient according to the reactor temperature field uniformity index and the heat transfer medium flow dynamic index; A multi-dimensional coupling matrix is ​​constructed according to the first coupling coefficient, the second coupling coefficient, and the third coupling coefficient.

6. The method for optimizing and controlling the polymerization reaction temperature of synthetic latex according to claim 1, wherein: The step of obtaining the temperature control fluctuation value according to the multi-dimensional coupling matrix includes: Performing eigenvalue decomposition on the multi-dimensional coupling matrix to obtain the temperature fluctuation eigenvalues ​​and corresponding fluctuation eigenvectors of the multi-dimensional coupling matrix; Obtaining a main eigenvector based on the temperature fluctuation eigenvalue and the corresponding fluctuation eigenvector, and generating a comprehensive eigenvector through linear combination; Obtaining a preset temperature control vector in the aggregation stage, and obtaining cosine similarity based on the preset temperature control vector and the comprehensive feature vector; Get the temperature control fluctuation value based on cosine similarity.

7. The method for optimizing and controlling the polymerization reaction temperature of synthetic latex according to claim 1, wherein: The step of acquiring dynamic adjustment information according to the temperature control fluctuation value includes: Obtaining the proportional factor adjustment amplitude of the controller according to the temperature control fluctuation value; Obtain the change trend based on the temperature control fluctuation value; Obtaining a delay time according to the heat transfer medium flow regulating valve; Generate a flow rate proportional adjustment amplitude and adjustment time according to the change trend, proportional factor adjustment amplitude, and corresponding time; Dynamic adjustment information is obtained according to the flow ratio adjustment amplitude and adjustment time.

8. A synthetic latex polymerization reaction temperature optimization control system, applied to a reactor and a heat transfer medium flow regulating valve, characterized in that: include: A data acquisition module is used to obtain temperature detection data of the reactor during the polymerization reaction of synthetic latex, wherein the temperature detection data includes real-time distribution temperature of the polymerization reaction zone, temperature distribution data of the reactor, and flow data of the heat transfer medium; a thermal stress analysis module, configured to obtain a thermal stress index value according to the real-time temperature distribution of the polymerization reaction zone, and generate a reaction zone parameter compensation value according to the thermal stress index value; A uniformity evaluation module is used to obtain a temperature field uniformity index of the reactor based on the temperature distribution data of the reactor; A flow dynamic analysis module, configured to obtain a heat transfer medium flow dynamic index based on the heat transfer medium flow data; A coupling matrix construction module is used to construct a multi-dimensional coupling matrix according to the reaction zone parameter compensation amount, the reactor temperature field uniformity index and the heat transfer medium flow dynamic index; A fluctuation acquisition module, configured to acquire a temperature control fluctuation value according to the multi-dimensional coupling matrix; The valve control module is used to obtain dynamic adjustment information according to the temperature control fluctuation value, and adjust the heat transfer medium flow control valve according to the dynamic adjustment information.

9. The synthetic latex polymerization reaction temperature optimization control system according to claim 8, characterized in that: The thermal stress analysis module includes: a temperature distribution acquisition unit, configured to acquire real-time temperature distribution data of the material according to the real-time temperature distribution of the polymerization reaction zone, wherein the real-time temperature distribution data of the material includes the real-time temperature value of the material at the uppermost position and the real-time temperature value of the material at the lowermost position; A temperature deviation calculation unit, configured to obtain a first temperature deviation and a second temperature deviation according to the real-time temperature value of the material at the uppermost position and the real-time temperature value of the material at the lowermost position; A fluctuation rate calculation unit, configured to obtain a first fluctuation rate and a second fluctuation rate corresponding to the polymerization reaction according to the first temperature deviation and the second temperature deviation; a distortion rate calculation unit, configured to obtain a temperature fluctuation distortion rate according to the first fluctuation rate and the second fluctuation rate; a thermal stress calculation unit, configured to obtain a thermal stress index value according to the temperature fluctuation distortion rate; A heat exchange efficiency acquisition unit, used to acquire a preset heat exchange efficiency of the outer jacket of the reactor; The compensation generating unit is used to generate a reaction zone parameter compensation amount according to the thermal stress index value and a preset heat exchange efficiency.

10. The synthetic latex polymerization reaction temperature optimization control system according to claim 8, characterized in that: The uniformity evaluation module includes: A kettle body temperature acquisition unit is used to acquire the temperature value of the bottom of the reactor, the temperature value of the middle of the reactor, and the temperature value of the top of the reactor according to the temperature distribution data of the reactor; a deviation value calculation unit, configured to obtain an average temperature value according to the reactor bottom temperature value, the reactor middle temperature value, and the reactor top temperature value, and obtain a first kettle body temperature deviation value, a second kettle body temperature deviation value, and a third kettle body temperature deviation value corresponding to the reactor bottom temperature value, the reactor middle temperature value, and the reactor top temperature value according to the average temperature value; A temperature difference threshold value obtaining unit is used to obtain a preset kettle body temperature difference threshold value; The uniformity calculation unit is used to obtain the reactor temperature field uniformity index according to the preset reactor body temperature difference threshold, the first reactor body temperature deviation value, the second reactor body temperature deviation value and the third reactor body temperature deviation value.

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