A temperature and pressure control method for a phenolic resin synthesis reaction kettle

Abstract

The application provides a temperature and pressure control method of a phenolic resin synthesis reaction kettle, relates to the field of industrial process automatic control, and acquires a reaction kettle temperature and pressure deviation and carries out dimensionless processing, constructs a two-dimensional temperature and pressure coupling deviation field and determines a coupling instability region mark, and then according to the region mark, carries out dynamic weight configuration and coupling redistribution on a jacket cooling water valve and a pressure relief valve and then outputs to an actuator. The method fully considers the strong coupling correlation between temperature and pressure in the polycondensation reaction, changes the temperature regulation loop and the pressure regulation loop from independent parallel operation to coordinated control based on the cooperative instability state, overcomes the technical defects that the regulation actions interfere with each other and the response lags behind the double-parameter synchronous instability evolution in the single-loop control, and thus significantly improves the temperature and pressure control precision and response timeliness under the condition of multiple disturbances.

Description

Technical Field

[0001] This invention relates to the field of industrial process automation control, and more specifically, to a method for controlling the temperature and pressure of a phenolic resin synthesis reactor. Background Technology

[0002] Phenolic resin is a polymer material synthesized from phenolic and aldehyde compounds through a condensation reaction under the action of a catalyst. Due to its excellent heat resistance, electrical insulation, and mechanical strength, it is widely used in molding compounds, coatings, adhesives, and composite materials. The condensation reaction is typically carried out in batches in a reactor equipped with a jacketed heating / cooling system and a stirring device. The reaction process includes multiple stages such as heating, isothermal condensation, vacuum dehydration, and cooling. This reaction is exothermic; the condensation of phenol and formaldehyde releases approximately 586.1 kJ / kg of heat, and the reaction rate increases exponentially with increasing temperature. Simultaneously, the water vapor generated in the reaction, together with unreacted formaldehyde vapor, causes the pressure inside the reactor to rise. Temperature and pressure are core process variables characterizing the reaction progress and safety status; their control precision directly affects product quality indicators such as resin molecular weight distribution, viscosity, and free phenol content.

[0003] Current temperature and pressure control in phenolic resin polycondensation reactors primarily employs relatively independent single-loop regulation strategies. For temperature control, industrial sites commonly use Pt100 resistance thermometers to detect the reactor temperature. A PID temperature controller uses the process setpoint temperature curve as a setpoint and adjusts the flow rate of jacket heating steam or cooling water to achieve temperature tracking control. To address the strong nonlinearity and time-varying characteristics of the polycondensation reaction, research has incorporated fuzzy control, intelligent predictive control, and combined intelligent control methods into the temperature control loop. For pressure control, safety valves or regulating pressure relief valves are typically used as actuators, opening to release pressure when the reactor pressure exceeds the process setpoint pressure curve or a safety threshold. Some solutions use condensate reflux ratio adjustment as an auxiliary pressure regulation method. Furthermore, some solutions interlock the reactor temperature and pressure with the jacket cooling water inlet valve and emergency cooling system.

[0004] However, the aforementioned existing technologies treat temperature control and pressure control as independent regulation loops—the temperature loop adjusts the cooling water valve only based on temperature deviation, and the pressure loop adjusts the pressure relief valve only based on pressure deviation, failing to fully consider the strong coupling relationship between temperature and pressure in the phenolic resin polycondensation reaction. Specifically, an increase in temperature accelerates the exothermic rate of the polycondensation reaction, leading to a non-linear increase in the exothermic rate, which in turn drives a rapid rise in the vapor pressure inside the reactor; the pressure increase, in turn, affects the composition of the reaction liquid phase through gas-liquid balance, feeding back into temperature changes. When disturbances such as raw material ratio fluctuations, jacket cooling water temperature drift, or changes in stirring conditions cause abnormal exothermic rates, single-loop control faces a dual dilemma: First, the adjustment actions of the temperature PID loop and the pressure PID loop interfere with each other—increasing the cooling water flow to suppress temperature may reduce the steam condensation and reflux effect, indirectly affecting the pressure; opening the pressure relief valve to reduce pressure may alter the thermal balance of the reaction system due to the discharge of gaseous components. Second, the independent response of each loop lags behind the evolution rate of synchronous temperature and pressure instability, often only starting to adjust after the deviation has significantly deviated from the process window. This leads to temperatures exceeding the allowable process range, causing uncontrolled resin molecular weight distribution, or frequent pressure triggering of safety valves, resulting in decreased product yield and volatile organic compound emissions. Although some advanced control schemes mention the "coupling relationship between temperature, pressure, and yield" or use decoupled control algorithms, they lack a specialized control architecture for the temperature and pressure co-instability mechanism of polycondensation reactions, and have not established a judgment mechanism that can quantify the degree of co-deviation between temperature and pressure deviations, nor a corresponding coordination and allocation strategy for dual actuators. Summary of the Invention

[0005] To address the aforementioned technical problems, this invention provides a method for controlling the temperature and pressure of a phenolic resin synthesis reactor. This method addresses, to some extent, the existing control methods that use independent temperature PID loops and pressure PID loops to adjust the opening of the jacket cooling water valve and the pressure relief valve, respectively. These methods do not consider the coupling relationship between temperature and pressure in exothermic reactions. When fluctuations in the raw material ratio or drifts in the cooling water temperature cause abnormal exothermic rates, the single-loop control response lags and the adjustment actions interfere with each other, leading to temperatures exceeding the process window or pressure frequently triggering the pressure relief threshold.

[0006] According to one aspect of the present invention, a method for controlling the temperature and pressure of a phenolic resin synthesis reactor is provided, comprising: The internal temperature and pressure of the reactor at the current sampling time are obtained and compared with the process set temperature curve and process set pressure curve at the corresponding time to obtain the normalized value of temperature deviation and the normalized value of pressure deviation. A temperature-pressure coupling deviation field is constructed based on the normalized values ​​of the temperature deviation and the pressure deviation, and a coupled instability region identifier characterizing the coordinated deviation state of temperature deviation and pressure deviation is determined in the temperature-pressure coupling deviation field. Based on the identification of the coupling instability region, the gain coefficients of the jacket cooling water valve opening and the pressure relief valve opening are dynamically weighted and configured. The temperature regulation requirement and pressure regulation requirement are coupled and redistributed according to the dynamic weight configuration result to obtain the adjustment amount of the jacket cooling water valve opening and the adjustment amount of the pressure relief valve opening. The adjustment amount of the jacket cooling water valve opening and the adjustment amount of the pressure relief valve opening are respectively output to the corresponding actuators, and the current coupling control cycle is updated according to the adjusted reactor temperature and reactor pressure.

[0007] Furthermore, the normalized values ​​of the temperature deviation and pressure deviation are determined according to the following formulas: , in, hour, This is the normalized value of the temperature deviation. These represent the filtered reactor temperature, process set temperature, rate of change of the process set temperature curve, allowable operating width of the temperature process, standard deviation of historical temperature stability fluctuation, and equivalent response time of the temperature measurement and control link, respectively. hour, This is the normalized value of the pressure deviation. The corresponding values ​​represent the filtered pressure inside the vessel, the process set pressure, the rate of change of the process set pressure curve, the allowable operating width of the pressure process, the standard deviation of the historical stable fluctuation of the pressure, and the equivalent response time of the pressure measurement and regulation link.

[0008] Furthermore, the identification of the coupling instability region includes at least one of the following: cooperative deviation direction, dominant deviation object, and degree of coupling reinforcement; The cooperative deviation direction is determined based on the quadrant positions of the normalized temperature deviation value and the normalized pressure deviation value in the temperature-pressure coupling deviation field. The dominant deviation object is determined based on the relative relationship between the temperature deviation component and the pressure deviation component. The degree of coupling enhancement is determined based on the coupling strength and its changing trend.

[0009] Furthermore, the coupling strength is determined according to the following formula: , in, This represents the coupling strength value at the current sampling moment; This is the temperature-pressure coupling coefficient; This is a dimensionless trend correction coefficient; The sampling period is This is the normalized value of the temperature deviation. This is the normalized value of the pressure deviation. This represents the normalized deviation rate of temperature. This represents the rate of change of normalized pressure deviation.

[0010] Furthermore, when the historical stable samples are insufficient to calculate the temperature-pressure coupling coefficient, the system enters the cold start coupling coefficient initialization mode. In this mode, the temperature-pressure coupling coefficient is initialized to a conservative initial value. After the stable operation batch passes the product index inspection, the actual coupling statistics are calculated based on the correlation between the normalized temperature deviation rate and the normalized pressure deviation rate in the stable operation segment, the lag relationship between the pressure response and the temperature change, and the current charge quantity correction result. The temperature-pressure coupling coefficient is then updated using an exponentially weighted moving average method.

[0011] Furthermore, the dynamic weighting configuration of the gain coefficients for the jacket cooling water valve opening and the pressure relief valve opening includes: When the coupling instability region indicates that the temperature deviation and pressure deviation are increasing in the same direction, the coupling portion of the pressure regulation demand will be allocated to the jacket cooling water valve opening adjustment amount. When the coupling instability region identifier indicates that the pressure deviation is the dominant deviation object, increase the configuration weight of the pressure relief valve opening gain coefficient, and retain the suppression effect of the jacketed cooling water valve on the exothermic reaction. When the coupling instability region indicates that the temperature deviation is the dominant deviation and the pressure deviation does not increase in the same direction, the configuration weight of the jacket cooling water valve opening gain coefficient is increased, and the unnecessary increase of the pressure relief valve opening is suppressed.

[0012] Furthermore, the adjustment amount of the jacket cooling water valve opening and the adjustment amount of the pressure relief valve opening are determined according to the following relationship: , in, This refers to the adjustment amount of the jacket cooling water valve opening. This refers to the adjustment amount of the pressure relief valve opening. For temperature regulation needs, To meet pressure regulation requirements, The configuration weights for the gain coefficient of the jacket cooling water valve opening. The configuration weights for the pressure relief valve opening gain coefficient. The temperature-pressure coupling coefficient is... The membership degree is the region where temperature deviation and pressure deviation increase in the same direction. The degree of pressure dominance, This indicates that the calculation results can be projected onto the current actuator within the operating domain.

[0013] According to another aspect of the present invention, a temperature and pressure control system for a phenolic resin synthesis reactor is provided, comprising: The deviation normalization module is used to obtain the internal temperature and pressure of the reactor at the current sampling time, and to obtain the normalized values ​​of temperature deviation and pressure deviation. The coupling deviation field construction module is used to construct a temperature-pressure coupling deviation field based on the normalized value of the temperature deviation and the normalized value of the pressure deviation, and to determine the identifier of the coupling instability region. The dynamic weight configuration module is used to dynamically configure the gain coefficients of the jacket cooling water valve opening and the pressure relief valve opening based on the coupling instability region identifier, and obtain the adjustment amount of the jacket cooling water valve opening and the adjustment amount of the pressure relief valve opening. The execution feedback module is used to output the adjustment amount of the jacket cooling water valve opening and the adjustment amount of the pressure relief valve opening to the corresponding actuators, and update the current coupling control cycle according to the adjusted reactor temperature and reactor pressure.

[0014] Compared with existing technologies, the temperature and pressure control method for a phenolic resin synthesis reactor provided by this invention acquires the temperature and pressure deviations of the reactor and performs dimensionless processing to construct a two-dimensional temperature-pressure coupled deviation field and identify coupled instability regions. Based on these region identifiers, the method dynamically weights and redistributes the coupling of the jacket cooling water valve and the pressure relief valve before outputting the results to the actuator. This method fully considers the strong coupling relationship between temperature and pressure in the polycondensation reaction, transforming the temperature and pressure regulation loops from independent parallel operation to coordinated control based on a cooperative instability state. It overcomes the technical defects of single-loop control, such as mutual interference of regulation actions and response lag behind the synchronous instability evolution of two parameters, thus significantly improving the accuracy and timeliness of temperature and pressure control under multiple disturbance conditions.

[0015] Meanwhile, this invention, through a coupled deviation field region identification and dynamic weight configuration mechanism, prioritizes enhancing cooling to suppress pressure rise at its source when temperature and pressure are synergistically amplified in the same direction, and increases the response weight of the pressure relief valve to ensure safety when pressure dominates the deviation. This strategy effectively reduces the frequency of unplanned safety valve tripping, minimizes material loss and volatile organic compound emissions, and precisely maintains the polycondensation temperature within the process window, significantly improving the consistency of resin molecular weight distribution and batch stability, thus achieving comprehensive optimization of production safety, product quality, and environmental benefits. Attached Figure Description

[0016] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort. In the drawings: Figure 1This is a flowchart of a method for controlling the temperature and pressure of a phenolic resin synthesis reactor according to an embodiment of the present invention.

[0017] Figure 2 This is a schematic diagram of the temperature and pressure coupling deviation field of the temperature and pressure control method for the phenolic resin synthesis reactor according to an embodiment of the present invention.

[0018] Figure 3 This is a time response curve of the temperature and pressure coupling control method for the phenolic resin synthesis reactor according to an embodiment of the present invention. Detailed Implementation

[0019] Hereinafter, exemplary embodiments according to the present invention will be described in detail with reference to the accompanying drawings. Obviously, the described embodiments are merely some embodiments of the present invention, and not all embodiments of the present invention. It should be understood that the present invention is not limited to the exemplary embodiments described herein.

[0020] Figure 1 This is a flowchart illustrating a method for controlling the temperature and pressure of a phenolic resin synthesis reactor according to an embodiment of the present invention. Figure 1 As shown, the temperature and pressure control method in the phenolic resin synthesis reactor includes: S1. The reactor coupling control unit reads the real-time measured values ​​of the reactor's internal temperature and pressure according to the control sampling cycle, and compares the real-time measured values ​​with the process set temperature curve and process set pressure curve at the corresponding time to obtain the internal temperature deviation and internal pressure deviation. Then, based on the process allowable operating boundary, equipment calibration data, and historical stable operating condition data, the two types of deviations are dimensionless processed, and the normalized values ​​of temperature deviation and pressure deviation are output.

[0021] Specifically, the reactor coupling control unit can be installed in the DCS system, PLC control system, or industrial computer in the production workshop, and multiple reactors can be processed separately using the reactor number as a data index. For each reactor, at the current sampling time... The reactor coupling control unit reads the temperature measurement value output by the temperature sensor inside the reactor. Pressure measurement value output by the pressure sensor inside the vessel Temperature measurements can be taken in degrees Celsius, and pressure measurements can be taken in MPa, kPa, or other pressure units, but all units should be standardized to the same engineering unit system before being used in subsequent calculations. Sampling period. The scanning cycle of the control system and the thermal inertia of the reactor can be determined together. For example, it can be selected based on the response time of the temperature sensor, the response time of the pressure transmitter, the action time of the jacket cooling water valve, and the position feedback time of the pressure relief valve, so that two consecutive sampling values ​​can reflect the actual evolution of the working conditions, rather than just the instrument noise.

[0022] After reading the real-time measurement values, the reactor coupling control unit can first perform a routine measurement validity verification. This verification does not rely on fixed human values ​​as the basis for judgment, but rather determines the reliability of the measurement value based on the sensor range, sensor calibration curve, instrument diagnostic status, the physically achievable change at adjacent sampling points, and the reactor's thermal inertia. For temperature data, a physically achievable temperature rise or fall range can be determined by combining the reactor's maximum heat exchange capacity, material specific heat, current charge amount, and jacket cooling water temperature difference. For pressure data, a physically achievable pressure change range can be determined by combining the reactor's vapor phase space volume, historical stable distribution of steam generation rate, pressure transmitter response time, and the current opening of the pressure relief valve. If a sampled value exceeds the physically achievable range and the sensor diagnostic status is abnormal, the sampled value can be marked as invalid, and the trend extrapolation value of the same reactor at adjacent valid sampling points can be used in the current cycle calculation. At the same time, this status is written to the control log. If the sensor status is normal but the sampled value changes rapidly, the sampled value is retained so that the subsequent coupling deviation field can identify the early state of abnormally increased heat release rate.

[0023] Furthermore, the process set temperature curve is a curve showing the temperature change over reaction time given in the formulation document or batch process sheet, and may include a heating section, a holding section, a cooling section, or a segmented isothermal section. The process set pressure curve is a pressure reference curve matching the same formulation, charge quantity, and reaction stage; it can be a pressure target curve or a process operation reference curve located below the safety release point. For cases where the curve does not directly provide the sampling time value, the reactor coupling control unit uses piecewise linear interpolation, spline interpolation, or an existing curve reading interface of the process system to obtain the current process set temperature. and process setting pressure For reactors in the planned heating or cooling phase, the first-order rate of change of the process setpoint temperature profile is... It is also retained to distinguish between deviations caused by planned process changes and those caused by abnormal exothermic reactions; similarly, it is retained for pressure curves. .

[0024] After obtaining the current measured value and the corresponding set curve value, the reactor coupling control unit calculates the temperature deviation. and pressure deviation .in, and These are the temperature and pressure values ​​after validity verification and necessary filtering. The filtering can employ first-order low-pass filtering or finite-window mid-range filtering, but the length of the filtering window should be less than the main response time of the jacket cooling water valve and pressure relief valve to avoid smoothing out the actual rapid heating or pressurization process. Positive deviation indicates that the actual value is higher than the process curve, and negative deviation indicates that the actual value is lower than the process curve. Because temperature and pressure have different dimensions and different sensitivities to resin polycondensation runaway, they are not directly compared in this step. and Instead, it first performs normalization processing consistent with the process window and historical stable fluctuations.

[0025] In one implementation, the normalized values ​​of temperature deviation and pressure deviation can be determined according to the following formula: , in, hour, These represent the filtered reactor temperature, process set temperature, rate of change of the process set temperature curve, allowable operating width of the temperature process, standard deviation of historical temperature stability fluctuation, and equivalent response time of the temperature measurement and control link, respectively. At that time, the corresponding values ​​are: filtered pressure inside the vessel, process set pressure, rate of change of process set pressure curve, allowable operating width of pressure process, standard deviation of historical pressure stability fluctuation, and equivalent response time of pressure measurement and regulation link. and Having the same units, when the deviation is positive, The distance between the current set value and the upper limit of the process allowable value can be taken; when the deviation is negative, The distance between the current setpoint and the lower limit of the process allowable pressure can be used. For polycondensation reaction scenarios where only the upper limit of the pressure has major control significance, positive deviation normalization can use the distance between the set pressure and the upper limit of the process allowable pressure, while negative deviation normalization can use the lower fluctuation range in the stable operating sample of the same formulation or the effective operating range in the calibrated range of the pressure transmitter.

[0026] In the above formula, It is a dimensionless fusion coefficient, with a value ranging from 0 to 1. It can be derived from the commissioning data of similar reactors under the same or similar formulas, or from stable segments in historical batches that are "product qualified and have not experienced actuator saturation" after offline calibration and online fine-tuning. Reflects the allowable operating space of the process. This reflects the natural fluctuations of the reactor in stable batches. This reflects the reasonable deviation caused by changes in the setpoint curve itself within a regulation response time. Since both the numerator and denominator have the same physical dimensions, the resulting... and All values ​​are dimensionless and can be used as coordinates for the subsequent two-dimensional coupled deviation field. By simultaneously introducing the process allowable operating width, historical stable fluctuations, and the set curve change rate, this step can avoid misjudging reasonable deviations in the planned heating stage as abnormalities, and can also avoid underestimating deviations due to relying solely on a fixed range when cooling water temperature drifts or raw material ratio fluctuations.

[0027] For example, in the later stage of polycondensation heating in a certain reactor, the current filter temperature The temperature is 92.4℃, corresponding to the process set temperature. The current forward temperature process allows for an operating width of 90.0℃. The standard deviation of the historical stable temperature fluctuation for the same formulation is 4.0℃. The equivalent response time of the temperature link is 0.6℃. The process temperature change rate is set to 1 minute. Given a flow rate of 0.5℃ / min and (eta_T) = 0.7, the normalized denominator for temperature is: The temperature is approximately 3.03℃, and the normalized temperature deviation is approximately 0.79. If the filter pressure at the same time... The pressure is 0.182 MPa, corresponding to the process setting pressure. The pressure is 0.170 MPa, the allowable operating width of the positive pressure process is 0.060 MPa, the standard deviation of historical stable pressure fluctuation is 0.004 MPa, the pressure curve change rate is 0.002 MPa / min, and the equivalent response time of the pressure link is 1 min. If the value is 0.7, the normalized pressure deviation value is approximately 0.28. This example is only for illustrating the normalization process and does not limit the specific values ​​of temperature, pressure, time, or fusion coefficient.

[0028] When historical stable samples are insufficient to establish a statistical fluctuation baseline for the current reactor, current formulation, and current reaction stage, the reactor coupling control unit enters a cold start normalization mode. Specifically, this cold start normalization mode does not rely on historical stable samples. Instead, the initial normalized reference is formed based on the rated operating boundary of the equipment. For temperature variables, the rated operating boundary of the equipment can be jointly defined by the design allowable temperature range of the reactor, the allowable temperature window of the formulation process, and the effective range of the temperature sensor; for pressure variables, the rated operating boundary of the equipment can be jointly defined by the design allowable pressure range of the reactor, the upper limit of the process allowable pressure, the effective range of the pressure transmitter, and the allowable operating pressure range of the pressure relief system. During the cold start phase, the initial stable fluctuation reference for temperature or pressure can be taken as one-quarter of the width of the corresponding rated operating boundary of the equipment, i.e., based on... As The initial replacement amount, of which It has the same dimensions as the corresponding variable. This value is derived from a conservative division of the equipment's operational space. Its purpose is to avoid missing normalization denominators when the sample pool is empty, and to avoid masking early deviations with an excessively large normalization benchmark. After the first batch or several batches of stable operating data pass the product indicator verification and it is confirmed that the actuator has not been at the operating boundary for a long time, the reactor coupling control unit uses an exponentially weighted moving average method to gradually switch the cold start benchmark to the actual statistical benchmark. For example, the stable fluctuation statistics obtained from the current batch are merged and updated with the benchmark of the previous period according to the forgetting factor, so that the normalization benchmark smoothly transitions from the equipment's rated boundary source to the actual operating distribution of this reactor and this formula.

[0029] S2. The reactor coupling control unit constructs a temperature and pressure coupling deviation field using the normalized values ​​of temperature deviation and pressure deviation as two-dimensional coordinates. Based on the current coordinate position, coordinate change trend, and the adaptive field boundary formed by the historical stable operating conditions of the same formula, the coupling instability region identifier is determined. The coupling instability region identifier is used to characterize the cooperative deviation direction, dominant deviation object, and coupling enhancement degree of the temperature deviation and pressure deviation in the current reactor.

[0030] Specifically, the temperature-pressure coupling deviation field is based on As the x-axis, with The first quadrant is a two-dimensional dimensionless plane with the vertical axis as the ordinate. The origin of this plane corresponds to the state where both temperature and pressure are consistent with the process setpoint curves. A positive horizontal axis indicates that the temperature is higher than the process setpoint temperature curve, and a positive vertical axis indicates that the pressure is higher than the process setpoint pressure curve. For the phenolic resin polycondensation reaction, a positive temperature deviation will accelerate the polycondensation reaction rate and increase the exothermic rate. At the same time, the generated water vapor and unreacted formaldehyde vapor will affect the pressure inside the reactor. Therefore, the coordinate points in the first quadrant not only indicate that both deviations are positive, but also indicate that there is a risk of simultaneous amplification of temperature and pressure. The second, third, and fourth quadrants are used to represent states such as low temperature and high pressure, low temperature and low pressure, and high temperature and low pressure, respectively, so that subsequent control strategies can distinguish whether to focus on jacket cooling, pressure relief, or suppressing excessive action of a certain actuator.

[0031] Furthermore, the reactor coupling control unit not only records the current coordinate point It also records the direction of motion of the coordinate points during continuous sampling time. The rate of change of the normalized temperature deviation can be expressed as... The rate of change of normalized pressure deviation can be expressed as: When the coordinate point continues to move away from the origin in the first quadrant, it indicates that both the positive temperature and positive pressure deviations are increasing. When the coordinate point moves towards the origin, it indicates that the current adjustment action has a suppressive effect on the coupling deviation. When the temperature coordinate decreases but the pressure coordinate increases, it indicates that simply enhancing cooling may not be sufficient to suppress the accumulation of gas phase pressure, and the participation of the pressure regulation loop needs to be increased subsequently. By combining the coordinate position and the direction of movement, this step can avoid judging the degree of coupling instability based solely on the current instantaneous deviation.

[0032] In one implementation, the reactor coupling control unit can first generate a temperature and pressure coupling coefficient based on historical stable operating conditions. The historical stable operating conditions can be selected from historical batches of the same reactor, resin brand, or similar formulation, where the temperature and pressure are within the allowable operating range, the jacket cooling water valves have not been at their opening limits for extended periods, the pressure relief valves have not frequently operated, and the final product indicators are qualified. Coupling coefficient The coefficient can be obtained from the correlation between the rate of change of temperature deviation and the rate of change of pressure deviation in stable data, the hysteretic response of temperature change to pressure change, and the correction of the current charge amount. The value can be limited to the range of 0 to less than 1 to ensure the positive definiteness of subsequent coupling distance calculations. If the new formula lacks sufficient historical data, the commissioning data of similar reactors can be used as the initial source, and updated recursively after each batch has completed stable operation. This allows the coefficient to reflect the influence of seasonal drift of cooling water temperature, changes in raw material moisture content, and reactor aging on the temperature-pressure coupling relationship.

[0033] In one embodiment, the coupling strength within the coupling deviation field can be determined according to the following formula: , in, This represents the coupling strength value at the current sampling moment, which is a dimensionless quantity. This is the temperature-pressure coupling coefficient, used to describe the degree of co-coupling between temperature deviation and pressure deviation in the current reaction system; It is a dimensionless trend correction coefficient that can be calibrated by known stable and abnormal segments in historical batches, so that the state where the coordinates are far from the origin can obtain a higher response in the coupling strength. The sampling period is represented by the unit [missing information]. , The time units are consistent throughout. The square root term in the formula represents the dimensionless distance after coupling correction, when... Furthermore, when both temperature and pressure deviations are positive, the distance is greater than the deviation reflected by the simple Euclidean distance; when one is positive and the other is negative, the cross term does not exaggerate the risk of instability in the same direction. The second term is the trend expansion term; the product term in parentheses indicates whether the current deviation coordinate has moved along the direction of deviation expansion. This is used to retain only deviations from the expanding trend, preventing a downward trend from being amplified further. Because... and The unit is the reciprocal of time, which becomes a dimensionless quantity after being multiplied by the sampling period. Therefore, the dimensions of the left and right sides of the formula are consistent.

[0034] Furthermore, the reactor coupling control unit determines the coupling instability region identifier based on the coordinate quadrant, dominant deviation direction, and coupling strength profile in the coupling deviation field. The coupling instability region identifier can consist of three parts: the first part indicates the deviation direction, such as "increasing in the same direction," "temperature rise and pressure drop," "temperature drop and pressure rise," or "decreasing in the same direction"; the second part indicates the dominant deviation object, such as "temperature dominant," "pressure dominant," or "equilibrium deviation"; and the third part indicates the coupling strength level, such as "stable offset," "transitional coupling," "coupled strengthening," or "approaching the operating boundary." The dominant deviation direction can be determined based on the angle between the current point and the temperature axis and pressure axis. The boundary of this angle is not a fixed, artificially given value, but is determined by the unit opening response of the jacket cooling water valve to temperature, the unit opening response of the pressure relief valve to pressure, and the slope of their cross-influence. For example, when the cooling water valve has a significantly stronger effect on reducing temperature than the pressure relief valve on reducing pressure under the same opening degree change, the temperature-dominant sector can be appropriately narrowed to avoid too many states being assigned to the temperature loop; when pressure accumulation is more sensitive to the impact on product yield and environmental emissions, the pressure-dominant sector can be adjusted accordingly based on equipment operating boundaries and emission constraints.

[0035] The coupling strength profile can be automatically formed from the distribution of historical stable samples with the same or similar formulations in the coupling deviation field. Specifically, the reactor coupling control unit will use the stable samples... Coordinates and their corresponding The values ​​are stored in the sample pool, and several closed or approximately closed field boundaries are formed based on the sample quantile distribution, median absolute deviation, and the process allowable operating boundary. The field boundary closest to the origin corresponds to the stable offset region, the outer field boundary corresponds to the transition coupling region, and the outermost field boundary corresponds to the coupling enhancement region. When the coordinate point approaches the operating boundary determined by the upper limit of the process allowable temperature, the upper limit of the process allowable pressure, and the maximum compensation capability of the actuator, it is marked as the operating boundary approximation region. The above field boundaries are updated iteratively with historical stable samples, current batch feedback results, and equipment status, thus adapting to raw material batch fluctuations, jacket cooling water temperature drift, and sensor calibration changes.

[0036] For example, following the example in S1, if the current , The temperature normalization bias and pressure normalization bias at the previous sampling time respectively make , The sampling period is 10s, and the temperature-pressure coupling coefficient is... Trend correction coefficient Then the square root term of the coupling strength is approximately The trend extension term is approximately 0.99; The value is approximately 0.003, which yields... Approximately 0.99. If the stable offset field boundaries formed by historical stable samples of the same formulation are concentrated within a small coupling strength range, and the current coordinate point is already located in the first quadrant and close to the outer coupling profile, then a coupling instability region identifier of "same direction increase - temperature dominance - coupling enhancement" can be output. This example is only used to illustrate the process of determining coupling strength and region identifiers, and does not limit the number of field boundaries, region names, or sample statistical methods.

[0037] Historical stable samples are insufficient to calculate the temperature-pressure coupling coefficient. At this time, the reactor coupling control unit enters the cold start coupling coefficient initialization mode. In this mode, the coupling coefficient... Instead of being calculated based on historical correlation, a conservative initial value of 0.2 is used and limited to a positive value to reflect the fundamental physical relationship that temperature increases in the phenolic resin polycondensation reaction typically promote exothermic reactions and increases in gas phase pressure. This avoids overestimating the coupling strength between temperature and pressure when actual samples are lacking. The 0.2 is a dimensionless initial coupling value used only for constructing the coupling deviation field during the cold start phase. Once the first batch of stable operating data passes product quality inspection and the corresponding operating segment does not exhibit actuator saturation, frequent pressure release, or sensor malfunctions, the reactor coupling control unit calculates the actual coupling statistics based on the correlation between the normalized temperature deviation rate and the normalized pressure deviation rate in that stable operating segment, the hysteresis relationship between pressure response and temperature change, and the current charge quantity correction result. This is then updated using an exponentially weighted moving average method. In this way, the coupling coefficient gradually transitions from a conservative initial value during the cold start phase to an actual coupling value that reflects the current state of the reactor, the formula, and the equipment, thus avoiding the inability to construct the coupling deviation field due to an empty sample pool.

[0038] S3. The reactor coupling control unit dynamically adjusts the configuration weights of the jacket cooling water valve opening gain coefficient and the pressure relief valve opening gain coefficient based on the coupling instability region identifier, the normalized value of temperature deviation, the normalized value of pressure deviation, and the coupling strength. Based on the configuration weights, it redistributes the opening correction requirements given by the temperature regulation loop and the pressure regulation loop to obtain the jacket cooling water valve opening adjustment amount and the pressure relief valve opening adjustment amount.

[0039] Specifically, the reactor coupling control unit can retain the original temperature and pressure regulation loops as basic regulators, but will no longer directly and independently apply the outputs of the two basic regulators to the corresponding valves. The temperature regulation loop generates basic temperature correction requirements based on the temperature deviation, the rate of change of temperature deviation, and the cumulative amount of temperature deviation. The pressure regulation loop generates the basic pressure correction requirement based on the pressure deviation, the rate of change of pressure deviation, and the cumulative pressure deviation. .in, This can be expressed as the percentage increase in jacket cooling water valve opening required to reduce positive temperature deviation. This can represent the percentage increase in pressure relief valve opening required to reduce positive pressure deviation; when the deviation is negative, the corresponding basic correction requirement can be negative, indicating a reduction in cooling water valve opening or a reduction in pressure relief valve opening. The basic regulator can employ existing PID, incremental PID, or loop algorithms already validated in industrial control systems. The focus of this invention is on cross-loop weighting and cross-compensation of the two basic correction requirements based on the temperature-pressure coupled deviation field.

[0040] Furthermore, the reactor coupling control unit first calculates the relative proportions of the temperature and pressure components in the current deviation. The temperature proportion can be determined by... Compared to The proportion is determined, and the pressure ratio can be determined by... The proportion relative to this total is determined; when both are close to zero, the proportion of the previous stable sampling period can be used or the current valve opening can be maintained directly to avoid meaningless minor fluctuations. Then, the reactor coupling control unit reads the coupling instability region identifier output by S2. If the region identifier is "increasing in the same direction" and the coupling coefficient is high, it means that the pressure increase is at least partly due to the exothermic reaction and steam generation caused by the temperature increase. At this time, part of the pressure correction demand should be transferred to the jacket cooling water valve so that the cooling action prioritizes the suppression of the source of continued pressure increase, while reducing the frequent operation of the pressure relief valve. If the region identifier shows "pressure dominant" and the pressure deviation change rate is consistently positive, it means that the pressure accumulation can no longer be eliminated in time by the cooling action alone. At this time, the configuration weight of the pressure relief valve opening gain coefficient should be increased, and the necessary cooling gain should be retained to prevent the temperature from continuing to push the pressure up again after the pressure is released. If the region identifier is "temperature rise and pressure drop", it means that temperature regulation should be prioritized, and the pressure relief valve can be maintained or converged to a smaller action; if the region identifier is "temperature drop and pressure rise", it means that the pressure loop should receive more response, while avoiding further increasing the cooling and causing the temperature to fall below the process window.

[0041] In one implementation, the configuration weights and valve opening adjustment amounts can be determined according to the following formula:

[0042]

[0043] , in, The configuration weights for the gain coefficient of the jacket cooling water valve opening. The configuration weights are the pressure relief valve opening gain coefficients, both of which are dimensionless and sum to 1; and These are the percentages of temperature deviation and pressure deviation, respectively. and These represent the positive expansion portions of the normalized deviation rate of temperature and the normalized deviation rate of pressure, respectively. This indicates whether the current region belongs to a region where temperature and pressure both increase in the same direction, and can be represented by a region membership degree between 0 and 1. This indicates the degree of pressure dominance in the current region identifier, or it can be represented by a region membership degree between 0 and 1. All parameters are dimensionless and can be calibrated jointly using reactor commissioning data, historical batch control effects, and actuator action costs. They can also be recursively corrected after the batch is completed based on convergence time, number of depressurization actions, and product quality results. The exponential function in the formula converts dimensionless features from different sources into smooth configuration weights, allowing the weights to change continuously near the region switching area, reducing regulation interference caused by valve opening switching between the two loops.

[0044] In the second matrix above, the top left item represents the proportion of temperature correction demand allocated to the jacket cooling water valve, and the bottom right item represents the proportion of pressure correction demand allocated to the pressure relief valve. The top right item indicates that when there is a "same-direction increase" and significant temperature-pressure coupling, a portion of the pressure correction demand is assigned to the jacket cooling water valve to suppress further pressure increases from the sources of heat release and steam generation. The bottom left item indicates that when pressure is dominant and the same-direction temperature-pressure coupling is not significant, the pressure relief valve is allowed to compensate for a portion of the pressure risk caused by temperature deviation. Thus, the regulation of the two valves is not generated by two independent loops unrelated to each other, but rather configured jointly by the area identifier and coupling strength given by the coupling deviation field. This means projecting the calculated valve opening adjustment amount onto the operating domain achievable by the current actuator. This operating domain is jointly determined by the valve's current opening, maximum and minimum opening, allowable opening change per unit time, cooling water supply capacity of the main pipe, pressure relief pipeline discharge capacity, and the permissible status of on-site safety interlocks. If any remaining adjustment amount cannot be executed after projection, it can be used as an anti-integral saturation correction amount for the base regulator in the next sampling period, preventing the controller from accumulating excessive internal output when the actuator is constrained.

[0045] For example, the current region is identified as "simultaneous increase - temperature-dominant - coupling enhancement", taking... Therefore, the temperature deviation accounts for approximately 0.74%, and the pressure deviation accounts for approximately 0.26%. , , The sampling period is 10 seconds. , And assuming that it was obtained through historical batch calibration Substituting into the above formula, we can obtain that the configuration weight of the jacketed cooling water valve is approximately 0.78, and the configuration weight of the pressure relief valve is approximately 0.22. If a base temperature correction is required... To increase the cooling water valve opening by 8 percentage points, the base pressure correction requirement... To increase the pressure relief valve opening by 6 percentage points, the adjustment range of the jacket cooling water valve, within the operating range of the actuator, is approximately... Approximately 9.2 percentage points; the pressure relief valve adjustment range is approximately... This is approximately 1.3 percentage points. This treatment indicates that the coupling portion of the pressure rise is preferentially suppressed by increasing the cooling water flow rate, rather than immediately and proportionally increasing the pressure relief valve actuation. This example is only for illustrating the dynamic weighting configuration and opening redistribution process and does not limit parameter values ​​or specific valve openings.

[0046] Optionally, when multiple reactors in the production workshop share a cooling water header or a tail gas treatment pipeline, the operating domain... It may also include constraints on public works resources. The reactor coupling control unit can prioritize and allocate cooling and depressurization resources based on the coupling strength of each reactor, the proximity of the operating boundary, and the current reaction stage. For reactors in the "same-direction rise-coupling enhancement" region and close to the operating boundary, priority is given to ensuring the adjustment of their jacket cooling water valves; for reactors where pressure is dominant and the depressurization pipeline capacity is limited, necessary depressurization capacity is retained while cooling compensation is increased simultaneously. This resource allocation does not change the coupling control logic of a single reactor, but rather coordinates the physical feasibility of the adjustment amounts of multiple reactors before the actuator outputs.

[0047] S4. The reactor coupling control unit outputs the jacket cooling water valve opening adjustment amount to the jacket cooling water flow control actuator and the pressure relief valve opening adjustment amount to the pressure relief valve position control actuator. At the same time, after outputting, it continuously collects the reactor temperature and pressure and repeatedly calculates the normalized deviation and coupling state. When the temperature deviation and pressure deviation within the continuous monitoring time window return to the convergence area formed by the historical stable operating conditions and process operation boundary, and the coupling deviation field coordinates no longer expand outward, the current coupling control cycle ends.

[0048] Specifically, the opening adjustment amount of the jacket cooling water valve The flow control actuator for the jacket cooling water can be sent via analog output, fieldbus commands, or DCS control block writing. The actuator may include a regulating valve, an electric valve, a pneumatic valve, and its valve positioner. When outputting the valve opening adjustment amount, the reactor coupling control unit records the current valve opening, the target opening, the allowable rate of change, and the valve positioner feedback status. If there is a continuous deviation between the target opening and the positioner feedback opening, this deviation is fed back as actuator hysteresis or jamming information to the operating domain projection of the next control cycle. (Pressure relief valve opening adjustment amount) Similarly, the output is sent to the pressure relief valve position control actuator. When outputting, the operating status of the exhaust gas treatment system, the back pressure of the pressure relief pipeline, and the feedback from the pressure relief valve positioner are combined to ensure that the calculated adjustment amount can be converted into the actual valve position action.

[0049] Furthermore, the reactor coupling control unit does not consider the adjustment complete immediately after a single output, but instead enters a continuous monitoring process after the adjustment action is executed. The length of the continuous monitoring time window can be determined by the reactor system identification data, including the lag time of the jacket cooling water from valve actuation to the observable change in reactor temperature, the response time of gas phase pressure to the pressure relief valve actuation, the response time of temperature sensors and pressure transmitters, and the mixing time inside the reactor. For reactors with high thermal inertia, the continuous monitoring time window can cover multiple sampling periods to identify whether the pressure continues to accumulate after the temperature drops; for reactors with fast pressure response, the continuous monitoring time window can be determined by combining the pressure drop curve after the pressure relief valve actuation. This window length is derived from the dynamic response of the equipment, rather than being arbitrarily given.

[0050] Within the continuous monitoring time window, the reactor coupling control unit rereads and normalizes the temperature and pressure deviations according to S1, and recalculates the coupling strength and coupling instability region identifier according to S2. If the current coordinate point has returned to the stable offset region formed by historical stable samples, and the trend of the coupling strength change no longer shows a departure from the origin throughout the continuous monitoring time window, and the change direction of the temperature deviation and pressure deviation relative to their respective process setting curves is consistent with the control target, and the jacket cooling water valve and pressure relief valve are not continuously at the operating domain boundary, then it is determined that the current coupling adjustment has been completed. At this time, the reactor coupling control unit ends the current control cycle and writes the starting deviation, region identifier, configuration weight, valve adjustment amount, convergence time, and actuator feedback of this cycle into the batch data record for subsequent updates to the normalization benchmark, coupling coefficient, and field boundary.

[0051] If, within the continuous monitoring time window, the normalized values ​​of temperature deviation and pressure deviation decrease but the coupling deviation field coordinates remain in the transitional coupling region or the coupling enhancement region, the reactor coupling control unit does not end the control cycle. Instead, it returns the latest temperature and pressure measurements to S1 and enters the next round of coupling control. If the temperature deviation has decreased but the pressure deviation continues to rise, S2 updates the region identifier to a pressure-dominated or temperature-decreasing-pressure-increasing state. Based on this, S3 increases the weight of the pressure relief valve configuration and reduces the excessive burden on the cooling circuit for pressure correction. If the pressure deviation decreases but the temperature deviation continues to rise, S3 increases the weight of the jacket cooling water valve configuration and suppresses unnecessary pressure relief valve actions. Through this recursive update method based on the sampling period, the adjustment action can change with the changes in the temperature-pressure coupling relationship, rather than maintaining the same set of fixed opening gains throughout the entire abnormal process.

[0052] On the other hand, if the actuator cannot achieve the projected target opening degree due to valve failure, insufficient utility resources, or on-site safety interlock restrictions, the reactor coupling control unit will feed back the actual opening degree to the operating domain in S3 and recalculate the available adjustment capacity for the next cycle based on the actual opening degree. For cases where the jacket cooling water valve opening is close to its operating boundary but the temperature continues to rise, the system can increase the participation of the pressure loop to avoid frequent passive venting due to continued pressure accumulation caused by temperature rise. For cases where the pressure relief valve cannot continue to increase its opening due to tail gas treatment capacity constraints, the system can transfer more pressure correction requirements to the cooling water valve and reduce the heat release rate by decreasing the temperature rise curve tracking speed or maintaining the current temperature setpoint. The decrease in temperature rise curve tracking speed or maintenance of the temperature setpoint can be considered as an in-formula adjustment action allowed by the process control system, and its adjustment range is determined by the process's allowed operating boundary and product quality constraints.

[0053] Optionally, after the current coupling control cycle ends, the reactor coupling control unit can perform quality screening on the data for this cycle and add data segments that meet the stable operating conditions to the historical stable sample pool. Data added to the sample pool should meet the following requirements: the product process curve is in normal execution mode, the actuator has not been at the boundary of the operating domain for an extended period, the temperature and pressure measurement signals are valid, and the coupling strength has steadily decreased within a continuous time window. During updates, recursive averaging, variance updates with a forgetting factor, or quantile distribution updates can be used to adjust the values ​​in S1. Coupling coefficients in S2 And the boundary of the coupling deviation field. For abnormal segments caused by abnormal raw material ratio, large drift of cooling water temperature or equipment failure, they can be stored in the abnormal sample pool for subsequent alarm analysis, but not directly used as the normalization benchmark for updating stable samples, so as to avoid solidifying abnormal fluctuations into normal operation characteristics.

[0054] Through the aforementioned output, monitoring, feedback, and sample update process, S4 ensures that the coupling adjustment amount calculated by S1 to S3 can truly act on the reactor's field actuators, and that the adjustment result corrects the deviation normalization, region identification, and weight configuration for the next control cycle. The end of the current control cycle does not signify the end of the overall reaction process in the reactor, but rather that dynamic compensation for the current temperature and pressure coupling deviation has been completed. In subsequent polycondensation reactions, the reactor coupling control unit continues to operate according to the sampling cycle, and when temperature and pressure deviate again, S1 to S4 are re-executed.

[0055] In summary, the temperature and pressure control method for the phenolic resin synthesis reactor based on the embodiments of the present invention has been clarified. This method acquires the temperature and pressure deviations of the reactor and performs dimensionless processing to construct a two-dimensional temperature-pressure coupled deviation field and identify coupled instability regions. Then, based on these region identifiers, it dynamically weights and redistributes the coupling between the jacket cooling water valve and the pressure relief valve before outputting the results to the actuator. This method fully considers the strong coupling relationship between temperature and pressure in the polycondensation reaction, transforming the temperature and pressure regulation loops from independent parallel operation to coordinated control based on a cooperative instability state. This overcomes the technical defects of single-loop control, such as mutual interference of regulation actions and response lag behind the synchronous instability evolution of two parameters, thereby significantly improving the accuracy and timeliness of temperature and pressure control under multiple disturbance conditions.

[0056] Here, those skilled in the art will understand that the specific operations of each step in the temperature and pressure control system of the phenolic resin synthesis reactor described above have been referenced. Figures 1 to 3 The temperature and pressure control methods for the phenolic resin synthesis reactor have been described in detail in the previous section, and therefore, their repeated description will be omitted.

[0057] In summary, the temperature and pressure control system for the phenolic resin synthesis reactor based on the embodiments of the present invention has been clarified. It acquires the temperature and pressure deviations of the reactor and performs dimensionless processing to construct a two-dimensional temperature-pressure coupled deviation field and determine the identifier of the coupled instability region. Then, based on this region identifier, it dynamically weights and redistributes the coupling of the jacket cooling water valve and the pressure relief valve before outputting the results to the actuator. This method fully considers the strong coupling relationship between temperature and pressure in the polycondensation reaction, transforming the temperature and pressure regulation loops from independent parallel operation to coordinated control based on a cooperative instability state. This overcomes the technical defects of single-loop control, such as mutual interference of regulation actions and response lag compared to the synchronous instability evolution of two parameters, thereby significantly improving the accuracy and timeliness of temperature and pressure control under multiple disturbance conditions.

Claims

1. A temperature and pressure control method for a phenol resin synthesis reaction vessel, characterized by, include: The internal temperature and pressure of the reactor at the current sampling time are obtained and compared with the process set temperature curve and process set pressure curve at the corresponding time to obtain the normalized value of temperature deviation and the normalized value of pressure deviation. A temperature-pressure coupling deviation field is constructed based on the normalized values ​​of the temperature deviation and the pressure deviation, and a coupled instability region identifier characterizing the coordinated deviation state of temperature deviation and pressure deviation is determined in the temperature-pressure coupling deviation field. Based on the identification of the coupling instability region, the gain coefficients of the jacket cooling water valve opening and the pressure relief valve opening are dynamically weighted and configured. The temperature regulation requirement and pressure regulation requirement are coupled and redistributed according to the dynamic weight configuration result to obtain the adjustment amount of the jacket cooling water valve opening and the adjustment amount of the pressure relief valve opening. The adjustment amount of the jacket cooling water valve opening and the adjustment amount of the pressure relief valve opening are respectively output to the corresponding actuators, and the current coupling control cycle is updated according to the adjusted reactor temperature and reactor pressure.

2. The method for controlling the temperature and pressure of the phenolic resin synthesis reactor according to claim 1, characterized in that, The normalized values ​​of the temperature deviation and pressure deviation are determined according to the following formulas: ， in, hour, This is the normalized value of the temperature deviation. These represent the filtered reactor temperature, process set temperature, rate of change of the process set temperature curve, allowable operating width of the temperature process, standard deviation of historical temperature stability fluctuation, and equivalent response time of the temperature measurement and control link, respectively. hour, This is the normalized value of the pressure deviation. The corresponding values ​​represent the filtered pressure inside the vessel, the process set pressure, the rate of change of the process set pressure curve, the allowable operating width of the pressure process, the standard deviation of the historical stable fluctuation of the pressure, and the equivalent response time of the pressure measurement and regulation link.

3. The method for controlling the temperature and pressure of the phenolic resin synthesis reactor according to claim 2, characterized in that, The identification of the coupling instability region includes at least one of the following: cooperative deviation direction, dominant deviation object, and degree of coupling reinforcement. The cooperative deviation direction is determined based on the quadrant positions of the normalized temperature deviation value and the normalized pressure deviation value in the temperature-pressure coupling deviation field. The dominant deviation object is determined based on the relative relationship between the temperature deviation component and the pressure deviation component. The degree of coupling enhancement is determined based on the coupling strength and its changing trend.

4. The method for controlling the temperature and pressure of the phenolic resin synthesis reactor according to claim 3, characterized in that, The coupling strength is determined according to the following formula: ， in, This represents the coupling strength value at the current sampling moment; This is the temperature-pressure coupling coefficient; This is a dimensionless trend correction coefficient; The sampling period is This is the normalized value of the temperature deviation. This is the normalized value of the pressure deviation. This represents the normalized deviation rate of temperature. This represents the rate of change of normalized pressure deviation.

5. The method for controlling the temperature and pressure of the phenolic resin synthesis reactor according to claim 4, characterized in that, When there are insufficient historical stable samples to calculate the temperature-pressure coupling coefficient, the system enters the cold start coupling coefficient initialization mode, in which the temperature-pressure coupling coefficient is initialized to a conservative initial value. After the batch of products in stable operation passes the product index inspection, the actual coupling statistics are calculated based on the correlation between the normalized deviation change rate of temperature and the normalized deviation change rate of pressure in the stable operation segment, the lag relationship of pressure response relative to temperature change, and the current charge quantity correction result. The temperature-pressure coupling coefficient is then updated using an exponential weighted moving average method.

6. The method for controlling the temperature and pressure of the phenolic resin synthesis reactor according to claim 5, characterized in that, The dynamic weighting configuration of the gain coefficients for the jacket cooling water valve opening and the pressure relief valve opening includes: When the coupling instability region indicates that the temperature deviation and pressure deviation are increasing in the same direction, the coupling portion of the pressure regulation demand will be allocated to the jacket cooling water valve opening adjustment amount. When the coupling instability region identifier indicates that the pressure deviation is the dominant deviation object, increase the configuration weight of the pressure relief valve opening gain coefficient, and retain the suppression effect of the jacketed cooling water valve on the exothermic reaction. When the coupling instability region indicates that the temperature deviation is the dominant deviation and the pressure deviation does not increase in the same direction, the configuration weight of the jacket cooling water valve opening gain coefficient is increased, and the unnecessary increase of the pressure relief valve opening is suppressed.

7. The method for controlling the temperature and pressure of the phenolic resin synthesis reactor according to claim 6, characterized in that, The adjustment range of the jacket cooling water valve opening and the adjustment range of the pressure relief valve opening are determined according to the following relationship: ， in, This refers to the adjustment amount of the jacket cooling water valve opening. This refers to the adjustment amount of the pressure relief valve opening. For temperature regulation needs, To meet pressure regulation requirements, The configuration weights for the gain coefficient of the jacket cooling water valve opening. The configuration weights for the pressure relief valve opening gain coefficient. The temperature-pressure coupling coefficient is... The membership degree is the region where temperature deviation and pressure deviation increase in the same direction. The degree of pressure dominance, This indicates that the calculation results can be projected onto the current actuator within the operating domain.

8. A temperature and pressure control system for a phenolic resin synthesis reactor, characterized in that, include: The deviation normalization module is used to obtain the internal temperature and pressure of the reactor at the current sampling time, and to obtain the normalized values ​​of temperature deviation and pressure deviation. The coupling deviation field construction module is used to construct a temperature-pressure coupling deviation field based on the normalized value of the temperature deviation and the normalized value of the pressure deviation, and to determine the identifier of the coupling instability region. The dynamic weight configuration module is used to dynamically configure the gain coefficients of the jacket cooling water valve opening and the pressure relief valve opening based on the coupling instability region identifier, and obtain the adjustment amount of the jacket cooling water valve opening and the adjustment amount of the pressure relief valve opening. The execution feedback module is used to output the adjustment amount of the jacket cooling water valve opening and the adjustment amount of the pressure relief valve opening to the corresponding actuators, and update the current coupling control cycle according to the adjusted reactor temperature and reactor pressure.

9. A computer device comprising a memory and a processor, wherein the memory stores a computer program, characterized in that, When the processor executes the computer program, it implements the steps of the temperature and pressure control method for the phenolic resin synthesis reactor as described in any one of claims 1 to 7.

10. A computer-readable storage medium having a computer program stored thereon, characterized in that, When the computer program is executed by the processor, it implements the steps of the temperature and pressure control method for the phenolic resin synthesis reactor as described in any one of claims 1 to 7.

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