Accurate temperature regulation and control method and system for co-pyrolysis reactor

Abstract

The invention discloses an accurate temperature regulation and control method and system for a co-pyrolysis reactor, and relates to the technical field of co-pyrolysis reactor temperature regulation. According to the specific implementation scheme, mixed plastic co-pyrolysis multi-dimensional state analysis is conducted, plastic co-pyrolysis reaction process recognition is conducted on the basis of the collected mixed plastic co-pyrolysis multi-dimensional state analysis result, and temperature regulation and control strategies corresponding to all mixed plastic co-pyrolysis reaction stages are executed on the basis of the plastic co-pyrolysis reaction process recognition result. In the execution process of the temperature regulation and control strategy, co-pyrolysis gas emission safety monitoring is carried out, and whether an intervention instruction with the highest priority is generated or not is judged based on the obtained co-pyrolysis gas emission safety monitoring result. According to the technology, the problems that dechlorination of the mixed plastic waste is not thorough, and the temperature control accuracy of the mixed plastic waste in the pyrolysis reactor is low are solved.

Description

Technical Field

[0001] This invention relates to the field of temperature control technology for co-pyrolysis reactors, and particularly to a method and system for precise temperature control of a co-pyrolysis reactor. Background Technology

[0002] Co-pyrolysis technology, as a resource recovery method that converts organic materials into high-value-added products such as fuels and chemicals through heating under anaerobic or hypoxic conditions, has become an important direction for solving plastic pollution and achieving a circular economy when applied to the treatment and resource recovery of mixed plastic waste. The efficiency of co-pyrolysis technology highly depends on the precise control of the temperature field within the co-pyrolysis reactor, such as controlling the unique decomposition temperature windows (i.e., the specific reaction temperature range corresponding to effective thermal decomposition and the generation of target products) and their reaction pathways (i.e., the specific process sequence of thermochemical bond breaking, intermediate generation and recombination, until the final product is formed within a specific reaction temperature range). Among these, co-pyrolysis... The co-pyrolysis reactor is the core equipment for this process. It provides the environment required for the thermal decomposition of the mixed plastics through direct or indirect heating. Its main components include co-pyrolysis zone heaters, a multi-channel temperature sensor array, a material feeding and carrier gas conveying unit, a thyristor regulator, an exhaust valve position actuator, and a comprehensive control system that integrates various actuators. Among them, the thyristor regulator and the exhaust valve position actuator (or frequency converter) are used to receive commands and directly regulate the thermal energy and medium flow. The heater is the terminal equipment that ultimately converts electrical or chemical energy into thermal radiation or convective heat transfer. The main power controller acts as the energy distribution center, responsible for receiving the total power command and decomposing it to each zone of the co-pyrolysis reactor according to a global strategy.

[0003] In the context of co-pyrolysis technology for treating mixed wastes (such as biomass and waste plastics) to achieve resource utilization, precise temperature control is the core of process success. This is not only because different materials have specific and mutually influential optimal reaction temperature windows, which directly determine the yield and selectivity of the target product (such as high-quality bio-oil), but also because improper temperature control during co-pyrolysis of chlorine-containing feedstocks can easily lead to the formation of highly toxic dioxins, posing a serious threat to the environment and safety. Current technologies typically achieve temperature control in pyrolysis reactors by first deploying thermocouples or infrared sensors at key locations inside the reactor (such as the reactor bed and outlet). The sensor continuously monitors and acquires real-time temperature data. The acquired temperature signal is then converted into a standard electrical signal and transmitted to the central controller of the pyrolysis reaction. During temperature control, the controller's built-in algorithm compares the received measured temperature value with a preset target temperature curve or setpoint that may include multiple stages (such as a low-temperature dechlorination stage and a high-temperature high-efficiency pyrolysis stage). The temperature deviation is calculated, and a corresponding adjustment command is generated based on the set control logic. Finally, the adjustment command is sent to the actuator (such as a proportional control valve) to dynamically adjust the power supply, heat transfer medium flow rate, or cooling air volume of the heater in the pyrolysis reactor, thereby changing the thermal energy input to the reactor.

[0004] For example, Chinese invention patent CN117093032B discloses a reactor temperature control method, system, electronic device, and storage medium, which includes: acquiring multiple real-time temperatures at multiple points in the reactor and multiple output status values ​​of temperature transmitters; determining an effective temperature based on the real-time temperatures, output status values, and preset threshold information, wherein the threshold information includes a first state threshold, an upper temperature limit, and a lower temperature limit; calculating the average temperature of the reactor based on the effective temperature; and controlling the reactor temperature based on the average temperature.

[0005] Existing technologies maintain overall or zone-specific temperature stability in co-pyrolysis reactors through statistical average feedback control based on multi-point temperature measurement and state screening during temperature control.

[0006] The above-mentioned technology has at least the following technical problems: In the temperature control process of co-pyrolysis resource recovery of mixed plastic waste, different plastic components, such as PVC (Polyvinyl Chloride), PE (Polyethylene), and PP (Polypropylene), have significantly different pyrolysis temperature windows and reaction pathways. Existing technologies typically employ a single temperature field or simple zoned heating methods. Furthermore, the large internal heat capacity of the co-pyrolysis reactor leads to significant temperature inertia; changes in material distribution and load easily cause localized temperature unevenness; and the dynamic response of heat source adjustment struggles to match the rapidly changing reaction pathway in real time, resulting in a common problem of temperature gradient response lag. These factors collectively prevent the co-pyrolysis reactor from dynamically adapting to and accurately switching the low-temperature dechlorination section (i.e., for chlorinated plastics such as PVC, releasing HCl in a lower temperature range, such as 200-350℃). The co-pyrolysis reactor consists of a pretreatment stage (where chlorine is separated from polyolefins) and a high-temperature, high-efficiency pyrolysis stage (the main reaction stage, which requires deep pyrolysis at temperatures above 450°C to fully convert polyolefins such as PE and PP into target products). Consequently, when generating temperature control commands for the co-pyrolysis reactor, the commands are often based on lagging global temperature averages and lack prediction of future reaction trends. This results in a delayed and limited response from the co-pyrolysis reactor, only able to change the overall or partial total heat energy input to the reactor, failing to achieve precise and targeted energy supply matching specific chemical reaction requirements. This may lead to the inability to promptly and completely remove hydrogen chloride released from chlorinated plastics (such as PVC) at mismatched temperatures. If these chlorinated substances enter the pyrolysis reactor, they may generate highly toxic dioxins and other persistent organic pollutants under the action of metal catalysts (such as copper, iron, and their ions). Simultaneously, the conversion rate of PE and PP components may be low due to the environment not reaching the high temperatures required for efficient pyrolysis. Ultimately, this leads to incomplete dechlorination of mixed plastic waste and low accuracy of temperature control within the pyrolysis reactor. Summary of the Invention

[0007] This invention provides a method and system for precise temperature control in a co-pyrolysis reactor, which can achieve complete dechlorination of mixed plastic waste and improve the accuracy of temperature control of mixed plastic waste within the pyrolysis reactor. The technical solution provided by this application is as follows: According to a first aspect of this application, a method for precise temperature control of a co-pyrolysis reactor is provided. The method includes: performing multi-dimensional state analysis of the co-pyrolysis of mixed plastics, and identifying the co-pyrolysis reaction process based on the collected multi-dimensional state analysis results; executing a temperature control strategy corresponding to each stage of the co-pyrolysis reaction based on the results of the co-pyrolysis reaction process identification; continuously monitoring the concentration of characteristic pollutants in the exhaust gas from the co-pyrolysis reactor for co-pyrolysis gas emission safety during the execution of the temperature control strategy, and determining whether to generate a highest-priority intervention command based on the obtained co-pyrolysis gas emission safety monitoring results. If so, the overall temperature setpoint of the co-pyrolysis reactor is forcibly switched and stabilized at a preset low-risk setpoint, and continuous monitoring of hazardous gases from co-pyrolysis is performed; otherwise, a toxic gas warning is issued.

[0008] According to another aspect of this application, a precise temperature control system for a co-pyrolysis reactor is provided, comprising: a multi-dimensional state monitoring module for co-pyrolysis of mixed plastics, a co-pyrolysis reactor temperature control module, and a co-pyrolysis gas emission safety monitoring module. The multi-dimensional state monitoring module for co-pyrolysis of mixed plastics is used to perform multi-dimensional state analysis of the co-pyrolysis of mixed plastics, and based on the collected multi-dimensional state analysis results, to identify the co-pyrolysis reaction process and generate a co-pyrolysis reaction process identification result. The co-pyrolysis reactor temperature control module is used to execute co-pyrolysis reactions of each mixed plastic based on the co-pyrolysis reaction process identification result. The temperature control strategy corresponds to each stage; the co-pyrolysis gas emission safety monitoring module is used to continuously monitor the concentration of characteristic pollutants in the exhaust gas of the co-pyrolysis reactor during the execution of the temperature control strategy. Based on the acquired co-pyrolysis gas emission safety monitoring results, it determines whether to generate the highest priority intervention command. If generated, the overall temperature setpoint of the co-pyrolysis reactor is forcibly switched and stabilized at a preset low-risk setpoint with lower risk. Continuous monitoring of co-pyrolysis hazardous gases is conducted to confirm whether the risk of co-pyrolysis hazardous gas emissions continues to exist. If not generated, a toxic gas warning is issued.

[0009] The beneficial effects of the technical solutions provided in the embodiments of the present invention include at least the following: 1. By conducting multidimensional state analysis of the co-pyrolysis of mixed plastics and identifying the co-pyrolysis reaction process based on the collected results, this approach fundamentally overcomes the defect of existing technologies where control logic and chemical reaction processes are disconnected. It enables the co-pyrolysis reactor to perceive, rather than simply measure, the actual reaction stage within the reactor in real time. This provides accurate decision-making basis for subsequent implementation of precise energy supply that matches the essential needs of the reaction, thereby reducing the risk of various chemical reaction runaways caused by misjudging the co-pyrolysis reaction stage and placing all mixed plastic waste under a single, compromise temperature. Based on the results of the plastic co-pyrolysis reaction process identification, temperature control strategies corresponding to each stage of the co-pyrolysis reaction of mixed plastics are implemented. This helps to achieve proactive and precise adaptation of the temperature field to the reaction paths of different plastic components, allowing chlorinated plastics to fully and stably remove HCl and be removed immediately within a dedicated low-temperature window. This helps to suppress corrosion and dioxin production in the co-pyrolysis reactor. The generation of precursors ensures that components such as polyolefins can obtain sufficient energy for pyrolysis within their dedicated high-temperature windows. This addresses a series of interconnected technical issues in both temporal and spatial dimensions, including incomplete dechlorination, low yield and selectivity of target products, high energy consumption, and significant secondary pollution risks. During the execution of the temperature control strategy, the concentration of characteristic pollutants in the exhaust gas from the co-pyrolysis reactor is continuously monitored for co-pyrolysis gas emission safety. Based on the obtained co-pyrolysis gas emission safety monitoring results, a decision is made on whether to generate a highest-priority intervention command to forcibly switch and stabilize the overall temperature setpoint of the co-pyrolysis reactor at a preset low-risk setpoint. Continuous monitoring of hazardous gases during co-pyrolysis is also conducted. Conversely, a toxic gas warning is issued if hazardous gases are detected. This helps ensure the thoroughness of the dechlorination process and the safety of the final pollutant emissions, improving the overall accuracy and reliability of temperature control. Ultimately, this achieves complete dechlorination of mixed plastic waste and improves the accuracy of temperature control of mixed plastic waste within the pyrolysis reactor.

[0010] 2. When the highest probability value in the probability distribution of the co-pyrolysis reaction stage obtained in the plastic co-pyrolysis reaction process identification of this scheme corresponds to a reaction stage confidence level that is not greater than a preset confidence threshold, it indicates that the classification model in the plastic co-pyrolysis reaction process identification of this scheme is insufficient in judging the current co-pyrolysis reaction stage of the mixed plastic. At this time, it is necessary to activate an alternative scheme for plastic co-pyrolysis reaction process identification. The preset classification model used in the first embodiment is marked as the main classification model, and other preset classification models that do not include the main classification model are marked as calibration classification models. This helps to provide dual-model intelligent decision-making when facing complex or atypical working conditions and when a single model is insufficient, thereby fundamentally reducing errors triggered by model misjudgment. The temperature control strategy prevents potential reaction process chaos, energy efficiency degradation, or increased safety risks, significantly improving the reliability and robustness of state identification throughout the co-pyrolysis reaction stage. Based on the probability distribution and calibration probability distribution of the co-pyrolysis reaction stage output in the first embodiment, reaction stage process calibration is performed. This facilitates a more accurate and reliable final determination of the reaction stage through multi-model cross-validation and arbitration mechanisms. This process effectively filters out random errors or local blind spots that may exist in single models in existing technologies, ensuring that subsequent temperature control commands are always based on a highly reliable understanding of the reaction process, guaranteeing that the entire co-pyrolysis reaction process achieves both high efficiency and inherent safety.

[0011] 3. When processing mixed plastics containing a large amount of easily meltable plastics such as PET or PA that produce sticky tar, continuous high-intensity exhaust may cause tar to adhere too quickly to the exhaust pipes or valves, leading to blockage risks. A targeted alternative implementation scheme, prioritizing dechlorination and constant temperature control, is adopted. When the hydrogen chloride concentration is monitored to be no greater than the preset first HCl concentration threshold but greater than the preset second HCl concentration threshold, the co-pyrolysis reactor temperature control center controls the exhaust valve actuator to perform repeated on / off pulse actions at a fixed frequency and preset high amplitude for a preset exhaust duration. This helps ensure that hydrogen chloride is effectively removed to meet dechlorination and safety requirements. While simultaneously addressing the issue, the periodically generated high-speed, short-duration strong airflow actively scours and disturbs the inner wall of the pipe, effectively stripping and removing the already adhering sticky tar precursors. This transforms the passive approach to clogging in existing technologies into an active online self-cleaning process, significantly reducing the risk and frequency of tar accumulation in the exhaust system. This ensures the long-term smooth operation and reliability of the exhaust system during the dechlorination stage, reduces unplanned downtime maintenance, and minimizes the decrease in exhaust efficiency caused by increased duct resistance. Ultimately, this achieves a dual optimization effect of highly efficient dechlorination and long-term stable operation of the equipment in the co-pyrolysis process of high-viscosity mixed plastics.

[0012] It should be understood that the description in this section is not intended to identify key or essential features of the embodiments of this disclosure, nor is it intended to limit the scope of this disclosure. Other features of this disclosure will become readily apparent from the following description. Attached Figure Description

[0013] The accompanying drawings are provided for a better understanding of this solution and do not constitute a limitation of this application. Wherein: Figure 1 This is a flowchart of a method for precise temperature control of a co-pyrolysis reactor provided in an embodiment of the present invention; Figure 2 This is a flowchart outlining a method for precise temperature control of a co-pyrolysis reactor, as provided in an embodiment of the present invention. Figure 3 This is a response curve of a multi-stage adaptive temperature control of a co-pyrolysis reactor, provided by an embodiment of the present invention, for a precise temperature control method of a co-pyrolysis reactor. Figure 4 This is a schematic diagram of a precise temperature control system for a co-pyrolysis reactor provided in an embodiment of the present invention. Detailed Implementation

[0014] The following description, in conjunction with the accompanying drawings, illustrates exemplary embodiments of this application, including various details to aid understanding. These should be considered merely exemplary. Therefore, those skilled in the art will recognize that various changes and modifications can be made to the embodiments described herein without departing from the scope and spirit of this application. Similarly, for clarity and brevity, descriptions of well-known functions and structures are omitted in the following description.

[0015] Example 1 provides a method for precise temperature control of a co-pyrolysis reactor. For example... Figure 1 The flowchart shown illustrates a method for precise temperature control in a co-pyrolysis reactor. This method includes the following steps: First, multi-dimensional state monitoring of mixed plastic co-pyrolysis is performed. During the temperature control process for resource recovery from the co-pyrolysis of mixed plastic waste, multi-dimensional state analysis of the mixed plastic co-pyrolysis is conducted to identify the plastic co-pyrolysis reaction process within the reactor. Based on the collected multi-dimensional state analysis results, the plastic co-pyrolysis reaction process is identified, generating a plastic co-pyrolysis reaction process identification result. This process identification is used to determine the current dominant reaction stage of co-pyrolysis. Multi-dimensional state monitoring of mixed plastic co-pyrolysis helps transform discrete temperature, gas concentration, and material signals into a real-time, interpretable digital representation of a continuous chemical reaction sequence during the co-pyrolysis reaction, laying the data foundation for the entire precise control and intelligent decision-making process.

[0016] Secondly, regarding the temperature control of the co-pyrolysis reactor, based on the results of the identification of the plastic co-pyrolysis reaction process, temperature control strategies corresponding to each stage of the mixed plastic co-pyrolysis reaction are implemented. The results of the plastic co-pyrolysis reaction process identification include the low-temperature dechlorination-dominant period, the heating transition period, and the high-temperature pyrolysis-dominant period. The temperature control strategies include isothermal control prioritizing dechlorination for the low-temperature dechlorination-dominant period to achieve efficient dechlorination and immediate removal of hydrogen chloride in the co-pyrolysis reactor; heating transition control for the heating transition period to achieve rapid and stable heating of the co-pyrolysis reactor and overcome its own thermal inertia; and high-temperature pyrolysis control. The high-temperature steady-state control corresponding to the pyrolysis-dominant phase is used to achieve high-temperature steady-state control and safety assessment of toxic gases in the co-pyrolysis reaction. By controlling the temperature of the co-pyrolysis reactor, it is helpful to decouple the unified energy input into a series of sub-strategies that are precisely linked in time and directionally distributed in space. This systematically transforms the complex co-pyrolysis reaction stages (low-temperature dechlorination stage, heating transition stage, and high-temperature steady-state pyrolysis stage) into a series of automatically executable, optimizable, and mutually coordinated control actions, realizing a fundamental shift from static and extensive thermal management to dynamic and refined adaptive thermal management.

[0017] Finally, the safety monitoring of co-pyrolysis gas emissions involves continuously monitoring the concentration of characteristic pollutants in the exhaust gas from the co-pyrolysis reactor during the temperature control strategy execution. This monitoring is used to assess the safety of co-pyrolysis gas emissions. Based on the monitoring results, it is determined whether to generate a high-priority intervention command. If generated, the overall temperature setpoint of the co-pyrolysis reactor is forcibly switched and stabilized at a preset low-risk setpoint. Continuous monitoring of co-pyrolysis hazardous gases is also conducted to confirm whether the risk of hazardous gas emissions persists. If no such risk is generated, a toxic gas warning is issued. Through this safety monitoring, it is possible to ensure that the operating boundaries are strictly limited to a preset environmental safety range when dealing with any abnormal conditions such as raw material fluctuations or model uncertainties during the co-pyrolysis reaction. This provides unparalleled safety protection for the continuous and stable operation of the co-pyrolysis reaction.

[0018] It should be noted that the method for precise temperature control of a co-pyrolysis reactor provided in this application requires the construction and maintenance of a parameter and knowledge database to support the operation of the system before implementation.

[0019] The database draws from diverse sources: it includes fundamental setpoints directly defined by experts based on reaction mechanisms and equipment specifications, such as preset total hydrogen chloride release thresholds, preset confidence thresholds, and preset low-temperature dechlorination constant values; it also integrates reference data sets from historical operations and experimental verifications, such as typical multidimensional feature vector samples under different mixed plastic ratios, successful temperature control program curves, and records of contaminant concentrations corresponding to safety incidents. This data provides empirical evidence for the rationality of static parameters. In terms of data management architecture, a hybrid storage strategy can be adopted. A relational database is used to store structured setpoints and relationships, while a non-relational database or time-series database is used to efficiently store and retrieve massive amounts of unstructured process history sequence data and feature maps. Technical personnel can adapt to constantly changing raw material characteristics and process optimization needs based on newly added co-pyrolysis operation data and control effect feedback.

[0020] As described above, multi-dimensional state monitoring of co-pyrolysis of mixed plastics, temperature control of the co-pyrolysis reactor, and safety monitoring of co-pyrolysis gas emissions help to construct a complete closed-loop control system that integrates real-time perception, intelligent decision-making, adaptive temperature control, and safety constraints on co-pyrolysis gas emissions. This system collaboratively addresses the core technical challenges intertwined in the co-pyrolysis of mixed plastics, such as difficulty in adapting reaction paths, coarse temperature control, and uncontrollable safety risks. Among these, multi-dimensional state monitoring of co-pyrolysis of mixed plastics serves as the basis for perception and decision-making. Its output of the current reaction stage of co-pyrolysis directly determines the precise triggering and switching of the temperature control strategy. Temperature control of the co-pyrolysis reactor is the core execution unit, and its control effect directly determines whether the reaction path can be accurately guided and the quality and yield of the final product. Safety monitoring of co-pyrolysis gas emissions serves as the highest-level independent safety protection layer. Its monitoring results can provide real-time supervision and mandatory intervention for the control of the co-pyrolysis reactor. These three elements constitute a deeply coupled and dynamically feedback-based intelligent control system driven by the chemical reaction process, controlled by the temperature field, and bounded by environmental safety.

[0021] like Figure 2 The diagram shown is a general overview flowchart of a method for precise temperature control of a co-pyrolysis reactor provided in an embodiment of the present invention. Figure 2It can be seen that: by performing multidimensional state analysis of the co-pyrolysis of mixed plastics and obtaining the confidence level of the reaction stage corresponding to the highest probability value in the probability distribution of the co-pyrolysis reaction stages, if the confidence level of the reaction stage corresponding to the highest probability value is greater than the preset confidence threshold, then the reaction stage corresponding to the current highest probability value is determined to be the currently dominant co-pyrolysis reaction stage of the mixed plastics. If the co-pyrolysis reaction stage of the mixed plastics is the low-temperature dechlorination-dominated period, then dechlorination-priority isothermal control is initiated. If the co-pyrolysis reaction stage of the mixed plastics is the heating transition period, then co-pyrolysis heating and heat compensation control is initiated. If the co-pyrolysis reaction stage of the mixed plastics is the high-temperature pyrolysis-dominated period, then high-temperature steady-state control is initiated, and dechlorination-priority isothermal control is implemented, including synchronous... High-precision constant temperature control and hydrogen chloride concentration discrimination are performed. Co-pyrolysis heating and heat compensation regulation is implemented, and global power allocation and output are performed. At the same time, the heating lag time of the co-pyrolysis reactor and the deviation value of the heating rate of each zone are obtained. It is determined whether the heating lag time of the co-pyrolysis reactor is greater than the preset heating lag time threshold and whether the deviation value of the heating rate of each zone is greater than the preset heating lag temperature threshold. If so, the zone of the co-pyrolysis reactor is marked as the heating lag zone of the co-pyrolysis reactor, and the directional compensation heating of the co-pyrolysis zone is started. Otherwise, the co-pyrolysis heating and heat compensation regulation continues. The high-temperature steady-state regulation is simultaneously implemented with multivariable decoupled steady-state control and co-pyrolysis gas emission safety monitoring.

[0022] Furthermore, the specific process of multidimensional state analysis of co-pyrolysis of mixed plastics is as follows: Acquiring multi-source sensor data streams from the co-pyrolysis reactor, including: spatiotemporal distribution data of the co-pyrolysis temperature field, obtained through multiple sets of thermocouples arranged at key axial and radial positions of the co-pyrolysis reactor, used to characterize the internal thermal state of the co-pyrolysis reactor; release data of key gaseous products from co-pyrolysis, acquired through online mass spectrometry or Fourier transform infrared spectroscopy, including concentration values ​​of hydrogen chloride, methane, ethylene, and carbon monoxide, used to characterize the co-pyrolysis reaction path and process of the mixed plastics; and co-pyrolysis process data of the mixed plastics, representing the carrier gas flow rate monitored by the mass flow controller.

[0023] Furthermore, the process of plastic co-pyrolysis reaction is identified. The specific steps are as follows: Step 1, based on the acquired multi-source sensor data stream from the co-pyrolysis reactor, parameters for evaluating the state of plastic co-pyrolysis are extracted. These extracted parameters are then combined and normalized to obtain a multi-dimensional feature vector reflecting the current overall reaction state of plastic co-pyrolysis. The parameters for evaluating the state of plastic co-pyrolysis include the temperature gradient change rate, which reflects the heat transfer and global activity of the plastic co-pyrolysis process; the cumulative release rate of hydrogen chloride, which reflects the progress of the PVC dechlorination stage; and the pyrolysis product formation index, which reflects the intensity of the deep pyrolysis reaction of polyolefins. The temperature gradient change rate is represented by the difference operation of the average temperature difference between different monitoring points along the axial direction of the co-pyrolysis reactor. Its magnitude and sign indicate the spatial movement rate of the exothermic / endothermic reaction region. The cumulative release rate of hydrogen chloride is obtained by multiplying the carrier gas flow rate by the hydrogen chloride concentration value and integrating it over time. The cumulative mass of hydrogen chloride released from the start of the co-pyrolysis reaction to the current moment is calculated. This cumulative mass of hydrogen chloride released is then expressed as a ratio to a preset total hydrogen chloride release threshold, which is set in advance by designated personnel. The cracking product formation index is expressed as the ratio of the concentration of typical cracking products (such as ethylene) to the concentration of background gaseous products (such as methane and carbon monoxide). The acquired plastic co-pyrolysis state assessment parameters (temperature gradient change rate, cumulative hydrogen chloride release rate, and cracking product formation index) are combined and normalized in a predetermined order into a multidimensional array to form an original feature vector. Subsequently, the values ​​of each parameter in the original feature vector are normalized. Normalization means mapping the values ​​of each parameter to a uniform, dimensionless numerical range (e.g., between 0 and 1 or a standard normal distribution) through preset scaling rules (such as minimum-maximum scaling, Z-score normalization, etc.).

[0024] Step 2: Input the multidimensional feature vector of plastic co-pyrolysis into a pre-trained classification model (such as a random forest or feedforward neural network model). The classification model takes the multidimensional feature vector of plastic co-pyrolysis as input and outputs the probability distribution of the current co-pyrolysis reaction stage of the mixed plastic, indicating whether it is in the low-temperature dechlorination-dominated stage, the heating transition stage, or the high-temperature pyrolysis-dominated stage. The specific training process of the classification model is as follows: Collect historical co-pyrolysis experimental or production data, covering different mixed plastic ratios and operating conditions; for each time segment in the data, label the stage according to the synchronously recorded process parameters and product analysis results using stage discrimination rules, thereby constructing a labeled training dataset. The classification model is trained based on the training dataset until the model converges.

[0025] For example, a significant decrease in the hydrogen chloride release rate and a continuous increase in ethylene concentration are used as indicators of the transition to the heating transition period, and the corresponding actual plastic co-pyrolysis reaction stage is labeled accordingly; this constitutes a high-quality training dataset; a selected machine learning algorithm is used to learn from this dataset, optimize the model parameters, and enable the model to accurately map the corresponding reaction stage probability from the input multidimensional feature vector.

[0026] Step 3: Send a control prompt to the co-pyrolysis reactor temperature control center. Based on the probability distribution of the co-pyrolysis reaction stages and the corresponding confidence level of the reaction stages of the mixed plastics co-pyrolysis, determine the current co-pyrolysis reaction stage of the mixed plastics. The specific determination process is as follows: Obtain the confidence level of the reaction stage corresponding to the highest probability value in the probability distribution of the co-pyrolysis reaction stages. If the confidence level of the reaction stage is greater than the preset confidence threshold, then the reaction stage of the mixed plastics co-pyrolysis corresponding to the current highest probability value is determined as the currently dominant co-pyrolysis reaction stage of the mixed plastics. If the currently dominant co-pyrolysis reaction stage of the mixed plastics is determined to be the low-temperature dechlorination dominant period, then the co-pyrolysis reactor temperature control center will stabilize the temperature within a low-temperature window of 200-350℃ to maximize HC... If the removal efficiency is the primary control target, dechlorination-priority isothermal control is initiated. If the current dominant stage of the mixed plastic co-pyrolysis reaction is determined to be a heating transition period, the co-pyrolysis reactor temperature control center prioritizes a stable and rapid increase in the overall reactor temperature field to the high-temperature pyrolysis zone, initiating co-pyrolysis heating and heat compensation control. If the current dominant stage of the mixed plastic co-pyrolysis reaction is determined to be a high-temperature pyrolysis-dominant period, the co-pyrolysis reactor temperature control center prioritizes maintaining the temperature precisely at the high-temperature pyrolysis target temperature and optimizing the polyolefin pyrolysis selectivity and target product yield, initiating high-temperature steady-state control. The high-temperature pyrolysis target temperature means that the co-pyrolysis reactor temperature control center will precisely maintain the temperature above 450℃.

[0027] As described above, multidimensional state analysis of co-pyrolysis of mixed plastics helps to transform the complex and continuous chemical reaction process inside the co-pyrolysis reactor into clear, quantifiable, and decision-making digital stage information. This provides precise situational awareness for subsequent temperature control of the co-pyrolysis reactor, improving the dynamic adaptability, response speed, and product selectivity guidance of the entire control system to the co-pyrolysis reaction of mixed plastics. It realizes the shift from blind adjustment based on single temperature feedback to intelligent control based on the chemical nature of the reaction.

[0028] Example 2 provides an alternative scheme for identifying the co-pyrolysis reaction process of plastics. When the highest probability value in the probability distribution of the co-pyrolysis reaction stage obtained in this scheme does not correspond to a confidence level greater than a preset confidence threshold, it indicates that the classification model in this scheme is insufficient in judging the current co-pyrolysis reaction stage of the mixed plastics. In this case, it is necessary to activate the alternative scheme for identifying the co-pyrolysis reaction process of plastics. The specific process is as follows: The preset classification model used in Example 1 is marked as the main classification model, and other preset classification models not containing the main classification model are marked as calibration classification models. The multidimensional feature vector of plastic co-pyrolysis is input into the calibration classification model, and the calibration probability distribution of the co-pyrolysis reaction stage corresponding to the current co-pyrolysis reaction stage of the mixed plastic being in the low-temperature dechlorination dominant stage, the heating transition stage, or the high-temperature pyrolysis dominant stage is output. Based on the co-pyrolysis reaction stage probability distribution and the calibration probability distribution of the co-pyrolysis reaction stage output in Example 1, the reaction stage process is calibrated. The specific process is as follows: If the co-pyrolysis reaction stage of the mixed plastic corresponding to the highest probability value determined by the main classification model and the calibration classification model is consistent, then the current reaction stage is determined to be the co-pyrolysis reaction stage of the mixed plastic; if the main classification model and the calibration classification model are consistent, then the current reaction stage is determined to be the co-pyrolysis reaction stage of the mixed plastic; if the highest probability value determined by the main classification model and the calibration classification model is consistent, then the current reaction stage is determined to be the co-pyrolysis reaction stage of the mixed plastic; if the highest probability value determined by the main classification model and the calibration classification model is consistent, then the current reaction stage is determined to be the co-pyrolysis reaction stage of the mixed plastic; if the highest probability value determined by the main classification model and the calibration classification model is consistent, then the current reaction stage is determined to be the co-pyrolysis reaction stage of the mixed plastic; if the highest probability value determined by the main classification model and the calibration classification model are ... If the reaction stages of the mixed plastic co-pyrolysis reaction determined by the class models are inconsistent, it is determined whether the confidence levels of the reaction stages corresponding to the highest probability values ​​of the main classification model and the calibration classification model are both greater than the preset confidence threshold. If so, a reaction stage confidence judgment based on the classification model is performed; otherwise, a model inconsistency prompt is sent. The reaction stage confidence judgment based on the classification model means determining whether the confidence level of the reaction stage corresponding to the highest probability value of the main classification model is greater than the confidence level of the reaction stage corresponding to the highest probability value of the calibration classification model. If so, the reaction stage corresponding to the highest probability value of the main classification model is determined to be the mixed plastic co-pyrolysis reaction stage; otherwise, the reaction stage corresponding to the highest probability value of the calibration classification model is determined to be the mixed plastic co-pyrolysis reaction stage.

[0029] As described above, the plastic co-pyrolysis reaction process identification based on dual-model cross-validation provided in Example 2 introduces key decision redundancy and error correction capabilities for the precise temperature adjustment of the entire mixed plastic co-pyrolysis reaction, improves the robustness of the state identification of the mixed plastic co-pyrolysis reaction stage, reduces the risk of the entire temperature control strategy failing due to accidental misjudgment by a single model, enhances the credibility of the decision through consensus in most cases, and can promptly trigger model inconsistency prompts when fundamental disagreements occur between models.

[0030] Furthermore, the specific process of dechlorination-priority isotropic control is as follows: First, the target temperature of the co-pyrolysis reactor is set to a preset low-temperature dechlorination constant value, which serves as the basis for isotropic control. The preset low-temperature dechlorination constant value represents a temperature value pre-set by personnel within the range of 200-350℃. Second, high-precision isotropic control is initiated, specifically as follows: The co-pyrolysis heating temperature deviation value is obtained to reflect the degree of deviation between the actual temperature of plastic co-pyrolysis and the target temperature. The co-pyrolysis heating temperature deviation value is the result of calculating the deviation between the average value of temperature measurements monitored by thermocouples and the target temperature. This indicates that the output power of the heater in the co-pyrolysis reactor is dynamically adjusted based on an incremental proportional-integral control algorithm. Specifically, the co-pyrolysis heating temperature deviation value is input into the incremental proportional-integral control algorithm, which outputs a heating power adjustment amount. This heating power adjustment amount is then sent to the heater's power regulation unit (such as a silicon controlled rectifier voltage regulator), thereby changing the actual heating power of the co-pyrolysis reactor heater to offset temperature fluctuations caused by material endothermic reactions or environmental heat dissipation. During the high-precision constant temperature control process, hydrogen chloride concentration is simultaneously used to monitor the safety and dechlorination efficiency of the plastic waste co-pyrolysis reaction in real time.

[0031] Furthermore, the specific process for determining the hydrogen chloride concentration is as follows: The hydrogen chloride concentration value is obtained from an online gas analyzer (such as a Fourier transform infrared spectrometer); when the hydrogen chloride concentration value is not greater than the preset second HCl concentration threshold, the dechlorination-priority isothermal control continues; otherwise, the strong exhaust dynamic control is initiated, specifically as follows: First, when the hydrogen chloride concentration value is greater than the preset first HCl concentration threshold, the temperature control center of the co-pyrolysis reactor outputs a step increment command; the step increment command is a control signal acting on the exhaust valve actuator (or exhaust fan frequency converter) on the exhaust pipe of the co-pyrolysis reactor, aiming to instantaneously increase its opening or speed by a preset fixed amplitude to quickly increase the system exhaust intensity and remove peak concentration HCl. The preset fixed amplitude is pre-set by the pre-set personnel.

[0032] To achieve precise matching between exhaust intensity and real-time dehydrogenation requirements, and to avoid over-adjustment or insufficient response that may result from a single step control, the exhaust gas is dynamically adjusted when the hydrogen chloride concentration is not greater than the preset first HCl concentration threshold but greater than the preset second HCl concentration threshold. The specific adjustment process is as follows: the hydrogen chloride concentration adjustment deviation value is obtained and used as the proportional adjustment input to the feedback control module in the dynamic control loop of the forced exhaust gas, to accurately calculate the required fine-tuning of the exhaust volume; the hydrogen chloride concentration adjustment deviation value is represented by the result of deviation calculation between the hydrogen chloride concentration value and the preset second HCl concentration threshold; the preset second HCl concentration threshold is less than the preset first HCl concentration threshold, and the preset second HCl concentration threshold is used to define the target level for fine-tuning, represented by the average value of hydrogen chloride concentration values ​​over a historical period; the preset first HCl concentration threshold is used to trigger emergency responses and is preset by designated personnel.

[0033] Furthermore, the product of the hydrogen chloride concentration adjustment deviation and the preset proportional coefficient is used as the exhaust valve position adjustment amount. This helps to ensure that the control output (exhaust valve position adjustment amount) is proportional to the current control deviation (hydrogen chloride concentration adjustment deviation value), thereby ensuring that the exhaust valve position adjustment force matches the deviation magnitude, achieving rapid response and stable convergence. The preset proportional coefficient is used to linearly map the unit quantity of the hydrogen chloride concentration adjustment deviation value (e.g., ppm) to the control quantity unit of the actuator (exhaust valve) (e.g., opening percentage), thus establishing a proportional relationship for feedback control. This is preset by the personnel. The amplitude corresponding to the exhaust valve position adjustment amount is used as the adjustment step size, and the valve opening of the exhaust valve actuator is adjusted step by step in the direction of decreasing hydrogen chloride concentration adjustment deviation value (after each adjustment of the exhaust valve actuator's valve opening, the hydrogen chloride concentration is re-acquired). The system monitors the hydrogen chloride concentration and determines whether it exceeds the preset second HCl concentration threshold. If so, it uses the adjusted valve position of the exhaust valve actuator as the initial value for the next adjustment, continuously adjusting it step by step in the direction of decreasing the hydrogen chloride concentration deviation. It also continuously outputs corresponding exhaust valve position control signals to precisely maintain the exhaust volume, ensuring that the released hydrogen chloride is discharged from the co-pyrolysis reactor immediately and continuously, thereby maximizing the removal efficiency of hydrogen chloride while maintaining the optimal dechlorination temperature. The system continuously monitors the hydrogen chloride concentration. When the hydrogen chloride concentration is not greater than the preset second HCl concentration threshold, the exhaust volume is maintained at the valve position determined in the previous adjustment cycle, entering a steady-state maintenance phase. Otherwise, it continues to perform dynamic adjustment of the hydrogen chloride exhaust. When the number of times the dynamic adjustment of the hydrogen chloride exhaust is executed exceeds the preset maximum number of adjustments, a failure message for the dynamic adjustment of the hydrogen chloride exhaust is sent.

[0034] As described above, the dechlorination-priority isothermal control helps maximize dechlorination efficiency from the source, reduces the risk of residual chlorine entering the subsequent high-temperature stage, fundamentally inhibits the preconditions for equipment corrosion and the formation of highly toxic dioxins, and creates clean and safe pre-pyrolysis conditions for the subsequent deep pyrolysis of non-chlorinated components such as PE and PP, ensuring the continuity of the overall co-pyrolysis reaction and the purity of the final product. Therefore, this dechlorination-priority isothermal control solves the problem of chlorinated plastic treatment and lays a crucial foundation for the safe and efficient operation of the entire co-pyrolysis process by dividing the plastic co-pyrolysis reaction process.

[0035] Example 3 provides another implementation scheme for dechlorination-priority isostatic control. When processing mixed plastics containing a large amount of easily meltable plastics such as PET or PA that produce sticky tar, continuous high-intensity exhaust may cause tar to adhere too quickly to the exhaust pipes or valves, leading to a risk of blockage. A targeted alternative implementation scheme for dechlorination-priority isostatic control is adopted, and the specific process is as follows: When the monitored hydrogen chloride concentration value is not greater than the preset first HCl concentration threshold, but greater than the preset second HCl concentration threshold, a strong exhaust prompt is sent to the co-pyrolysis reactor temperature control center. The strong exhaust prompt indicates that the co-pyrolysis reactor temperature control center is using the control of the exhaust valve actuator to perform repeated opening and closing pulse actions at a fixed frequency and preset high amplitude for a preset exhaust duration. The preset high amplitude indicates the maximum opening command value reached by the exhaust valve actuator within a single pulse cycle (e.g., exhaust valve). The valve is operated at 90% of its opening capacity to drive it to near full opening in a very short time, generating a powerful high-speed airflow. The preset exhaust duration indicates the duration (e.g., 0.5-2 seconds) during a single pulse cycle when the exhaust valve actuator maintains a preset high amplitude. This ensures that the generated high-speed airflow has sufficient energy to purge and remove sticky tar adhering to the pipe wall. The preset high amplitude is set in advance by the operator. The high-speed airflow generated during the pulse action effectively purges any sticky substances that may be adhering. During the interval between two adjacent high-amplitude pulse actions, the system automatically switches to and maintains a preset medium-level exhaust volume. The high-amplitude pulse is responsible for periodic, powerful online self-cleaning, while the medium-level exhaust during the pulse interval continues to ensure the HCl removal efficiency, reducing system blockage and maintenance frequency. The preset medium-level exhaust volume is also set in advance by the operator.

[0036] As described above, the temperature control for dechlorination priority of viscous materials provided in Example 3 upgrades the traditional function of removing gas at a constant flow rate into an intelligent action that combines functional execution and equipment maintenance. It breaks down the single, continuous strong airflow into a pulse mode that alternates between short-term high-speed impact and basic maintenance exhaust. Thus, without sacrificing the efficiency of immediate hydrogen chloride removal, the periodically generated high-speed airflow forms an active mechanical scouring and shearing effect on the inner wall of the pipeline. This helps to resolve the inherent contradiction between dechlorination exhaust and anti-clogging maintenance of high-viscosity mixed plastics, transforming the passive cleaning of blockage risk after the fact into active online prevention during operation. It reduces the frequency of unplanned shutdowns and physical cleaning of the co-pyrolysis reactor due to tar accumulation, ensures long-term stable operation of the dechlorination stage, and improves the adaptability of the entire co-pyrolysis system to complex raw materials.

[0037] Furthermore, the specific process of co-pyrolysis heating and heat compensation control is as follows: The first step is to predict the co-pyrolysis heating curve. Specifically, the prediction process involves inputting the multi-dimensional feature vector of plastic co-pyrolysis into a pre-defined thermal dynamics model, such as an LSTM (Long Short-Term Memory) hybrid neural network model, to output the target heating curve of co-pyrolysis (a dynamic predicted temperature-time series). The specific training process of the pre-defined thermal dynamics model is as follows: A large amount of time-series data corresponding to the multi-dimensional feature vector of plastic co-pyrolysis during historical co-pyrolysis processes, as well as the actual optimal temperature-time series within that period, are collected as training samples. The LSTM hybrid neural network model is trained through supervised learning, enabling it to learn from the input features and predict the optimal heating trajectory. The second step is to calculate the co-pyrolysis reference power to overcome the thermal inertia of the co-pyrolysis reactor based on the co-pyrolysis heating curve.

[0038] Specifically, the co-pyrolysis reference power is represented by multiplying the total equivalent heat capacity of the co-pyrolysis reactor (including internal materials and components) by the target co-pyrolysis heating rate. The total equivalent heat capacity quantifies the total heat absorbed by the entire co-pyrolysis reactor to raise its temperature by one unit and is preset by designated personnel. The target co-pyrolysis heating rate is represented by performing a time differential operation on the target co-pyrolysis heating curve. The third step involves obtaining the co-pyrolysis heating power used to overcome the thermal inertia of the co-pyrolysis reactor and provide steady-state thermal compensation. The co-pyrolysis heating power is calculated by multiplying the co-pyrolysis reference power by a preset heat loss power... The result of the summation operation indicates that the preset heat loss power is used to compensate for the heat continuously lost by the co-pyrolysis reactor to the environment through the shell, pipes, etc., to ensure that all the net energy input to the reactor is used for effective heating. This is set in advance by the preset personnel. The co-pyrolysis heating power is sent to the co-pyrolysis reactor temperature control center to generate a co-pyrolysis heating power command, which is then sent to the main power controller of the co-pyrolysis reactor for global power allocation and output. In the fourth step, the temperature of each zone of the co-pyrolysis reactor is monitored in parallel, and the co-pyrolysis zone directional compensation heating is initiated in the lag zone of the co-pyrolysis reactor.

[0039] Furthermore, the temperature of each zone in the co-pyrolysis reactor is monitored in parallel, and directional compensation heating is initiated for the lag zone of the co-pyrolysis reactor. The specific process is as follows: The heating rate of the co-pyrolysis reactor zone used to evaluate the spatial uniformity of the internal temperature field and determine whether there is a lag in the heating of each zone is continuously monitored; the heating rate of the co-pyrolysis reactor zone is represented by the temperature change of that zone during the co-pyrolysis heating time period; the heating rate of the co-pyrolysis reactor zone is compared with the target heating rate. When the heating lag time of the co-pyrolysis reactor exceeds a preset heating lag time threshold, and the deviation value of the zone heating rate is greater than the preset heating lag temperature threshold, then that zone of the co-pyrolysis reactor is marked as a lag zone. The preset heating lag time threshold is represented by the average value of the heating lag time of the co-pyrolysis reactor over a historical time period, and the preset heating lag temperature threshold is represented by the average value of the zone heating rate deviation values ​​over a historical time period. The heating lag time of the co-pyrolysis reactor represents a certain... The duration for which the heating rate of a co-pyrolysis reactor zone is lower than the target heating rate; the deviation value of the zone heating rate is represented by quantifying the deviation between the target heating rate and the zone heating rate of the co-pyrolysis reactor; based on the heating lag zone of the co-pyrolysis reactor, directional compensation heating of the co-pyrolysis zone is initiated, and the specific process is as follows: a lag compensation heating command is sent to the heater in the heating lag zone of the co-pyrolysis reactor; the lag compensation heating command represents the additional power used for the heating lag zone of the co-pyrolysis reactor, and the lag compensation heating power value of the lag compensation heating command is represented by multiplying the zone heating rate deviation value with a preset compensation ratio coefficient; the preset compensation ratio coefficient is used to convert the dimension of rate deviation (°C / min) into the dimension of power (W), thereby realizing proportional power compensation for the lag zone, and the preset ratio coefficient is set in advance by preset personnel; co-pyrolysis heating and heat compensation control are continuously performed until the temperature of the core area of ​​the co-pyrolysis reactor reaches the preset high-temperature pyrolysis stage inlet temperature threshold (e.g., 420°C), indicating that the transition stage is completed.

[0040] As described above, co-pyrolysis heating and heat compensation regulation helps to achieve precise, proactive, and energy-optimal feedforward-driven control of the heating process. This effectively overcomes the temperature response lag (thermal inertia) problem caused by the huge heat capacity of large co-pyrolysis reactors, enabling the actual heating curve to closely track the preset optimal target trajectory. This avoids the heating rate fluctuations, overshoot, or lag caused by post-correction in traditional feedback control. At the same time, combined with real-time monitoring and dynamic balancing of the zoned temperatures of the co-pyrolysis reactor, it ensures that the internal temperature field of the co-pyrolysis reactor maintains a high degree of spatial uniformity during rapid heating, reducing local overheating or incomplete reaction caused by uneven material distribution or heat transfer differences.

[0041] Furthermore, the specific process of high-temperature steady-state control is as follows: First, the temperature control center switches and locks the high-temperature target temperature setpoint at a preset high-temperature target temperature above 450℃. This preset high-temperature target temperature is determined by the preset personnel based on the temperature range with the highest yield of the target product (such as ethylene and propylene) in historical data. Second, multivariable decoupled steady-state control is initiated based on the high-temperature target temperature. The specific process is as follows: Based on the decoupled control algorithm, the power output of the heaters in each zone of the co-pyrolysis reactor is adjusted independently and collaboratively to simultaneously achieve the overall temperature steady state of the co-pyrolysis reactor and the temperature uniformity of each zone, providing a precise and stable thermal environment for the cracking reaction.

[0042] Given that the high-temperature steady-state control stage is a critical period where deep pyrolysis reactions and the potential formation of highly toxic dioxin-like pollutants coexist, safety monitoring of co-pyrolysis gas emissions is conducted simultaneously during the high-temperature steady-state control process. The specific process is as follows: The toxicity equivalent of dioxin-like substances is obtained to assess the safety of co-pyrolysis gas emissions and provide a basis for deciding whether safety intervention is necessary during high-temperature steady-state control; it is determined whether the toxicity equivalent of dioxin-like substances exceeds the preset dioxin risk threshold. If so, a toxic gas warning is issued; otherwise, the temperature control center generates a high-priority intervention command, forcibly switching the overall temperature setpoint of the co-pyrolysis reactor. The system stabilizes at a preset low-risk setpoint and continuously monitors the co-pyrolysis hazardous gases to confirm whether the emission risk persists. The specific process is as follows: If the toxic equivalent of dioxin-like substances is not greater than the preset dioxin risk threshold within the preset observation time, high-temperature steady-state control continues. If the toxic equivalent of dioxin-like substances is still greater than the preset dioxin risk threshold within the preset observation time, a toxic gas warning is issued. The preset dioxin risk threshold is represented by the average toxic equivalent of dioxin-like substances over a historical period. Both the preset low-risk setpoint and the preset observation time are set in advance by the preset personnel.

[0043] As described above, high-temperature steady-state control and co-pyrolysis gas emission safety monitoring create a uniform and stable high-temperature environment for the deep pyrolysis reaction, thereby maximizing the yield and selectivity of high-value chemicals (such as olefins and aromatics). Co-pyrolysis gas emission safety monitoring, as an independent protection layer operating in parallel with the highest decision-making authority, will instantly trigger the highest level of intervention once a potential risk of excessive co-pyrolysis gas emissions is identified, forcibly switching to a safe mode until the risk is eliminated. This achieves a sustainable and efficient production operation mode under strict safety constraints.

[0044] like Figure 3 The figure shown is a multi-stage adaptive temperature control response curve of a co-pyrolysis reactor, based on a precise temperature control method for a co-pyrolysis reactor provided in an embodiment of the present invention. Figure 3 As can be seen from the graph, with time (0-60 min) on the horizontal axis and temperature (0-500℃) on the vertical axis, the gray square line represents the target temperature, and the red broken line represents the temperature of the co-pyrolysis reactor. During the temperature control process of co-pyrolysis resource recovery of mixed plastic waste, the temperature change of the co-pyrolysis reactor over time exhibits a distinct three-stage characteristic, corresponding to the low-temperature dechlorination-dominated period (e.g., 20-30 min), the heating transition period (e.g., 30-50 min), and the high-temperature pyrolysis-dominated period (e.g., 50-60 min). The low-temperature dechlorination-dominated period... During the initial stage, the temperature of the co-pyrolysis reactor is maintained at a relatively low level (e.g., 300℃) to ensure the safe removal of chlorine. After entering the temperature rise transition period, the temperature shows a steady upward trend. The co-pyrolysis reactor adaptively adjusts the heating power to achieve the temperature transition from dechlorination to pyrolysis. During the high-temperature pyrolysis-dominant period, the temperature rises rapidly and stabilizes in the set high-temperature range (e.g., 480℃). At this time, the pyrolysis reaction is the dominant process. Throughout the process, the actual temperature of the co-pyrolysis reactor can closely follow the change of the target temperature, demonstrating the adaptability and precision of this method in multi-stage temperature control.

[0045] like Figure 4 The diagram shown is a schematic of a precise temperature control system for a co-pyrolysis reactor provided in an embodiment of the present invention. The system includes: a multi-dimensional state monitoring module for co-pyrolysis of mixed plastics, a co-pyrolysis reactor temperature control module, and a co-pyrolysis gas emission safety monitoring module. The multi-dimensional state monitoring module for co-pyrolysis of mixed plastics performs multi-dimensional state analysis of the co-pyrolysis of mixed plastics and identifies the co-pyrolysis reaction process based on the collected analysis results, generating a co-pyrolysis reaction process identification result. By monitoring the multi-dimensional state analysis results of the co-pyrolysis of mixed plastics, the system helps establish a real-time, dynamic chemical context perception capability for the entire co-pyrolysis reactor temperature control system. This transforms the complex physicochemical changes within the reactor into deterministic stage information that can be directly understood and utilized by subsequent modules, thus solving the problem of disconnect between perception and control caused by the inability of traditional control systems to understand the nature of the reaction, and laying the information foundation for intelligent decision-making throughout the system.

[0046] The temperature control module of the co-pyrolysis reactor is used to execute temperature control strategies corresponding to each stage of the co-pyrolysis reaction of mixed plastics based on the results of the identification of the co-pyrolysis reaction process. Through temperature control of the co-pyrolysis reactor, it helps to transform the cognitive information about the chemical reaction process output by the multi-dimensional state monitoring module of mixed plastic co-pyrolysis into a precise, stage-specific control sequence for the heating system of the co-pyrolysis reactor. This achieves active adaptation and precise matching between the temperature field and the dynamic chemical reaction path at the physical level, solving the fundamental problem of the disconnect between control commands and reaction requirements in the prior art, and improving the yield and selectivity of the target product.

[0047] The co-pyrolysis gas emission safety monitoring module is used to continuously monitor the concentration of characteristic pollutants in the exhaust gas from the co-pyrolysis reactor during the execution of the temperature control strategy. Based on the acquired co-pyrolysis gas emission safety monitoring results, it determines whether to generate a high-priority intervention command. If generated, the overall temperature setpoint of the co-pyrolysis reactor is forcibly switched and stabilized at a preset low-risk setpoint. Continuous monitoring of co-pyrolysis hazardous gases is conducted to confirm whether the risk of co-pyrolysis hazardous gas emissions persists. If no such risk is generated, a toxic gas warning is issued. By monitoring the co-pyrolysis gas emission safety monitoring results, it helps ensure that the operating boundaries of the precise temperature control system of the co-pyrolysis reactor are strictly constrained within the red line of environmental safety under any operating conditions, thereby endowing the co-pyrolysis process with verifiable inherent safety attributes and reducing the risk of secondary pollution.

[0048] As described above, the multi-dimensional state monitoring module for co-pyrolysis of mixed plastics, the temperature control module for the co-pyrolysis reactor, and the safety monitoring module for co-pyrolysis gas emissions help to build an intelligent architecture with clear division of labor, clear responsibilities, and closed-loop operation. This decomposes the complex task of precise temperature control into a systematic project completed collaboratively by three functional domains: perception and cognition, decision-making and execution, and supervision and arbitration. Specifically, the output of the multi-dimensional state monitoring module for co-pyrolysis of mixed plastics is the sole legal basis for the action of the temperature control module for the co-pyrolysis reactor, while the safety monitoring module for co-pyrolysis gas emissions has the highest supervisory authority over all the actions of the former two. The three modules, based on the principles of perception-driven execution and safety constraints, form an organic whole with data flow as the link, chemical reaction optimization as the goal, and safety and environmental protection as the red line, achieving a leap from local optimization to system optimization.

[0049] It should be noted that the order of the embodiments described above is merely for descriptive purposes and does not represent the superiority or inferiority of the embodiments. Furthermore, the above description focuses on specific embodiments of this application. Other embodiments are within the scope of the appended claims. In some cases, the actions or steps described in the claims can be performed in a different order than that shown in the embodiments and still achieve the desired results. Additionally, the processes depicted in the drawings do not necessarily require a specific or sequential order to achieve the desired results. In some implementations, multitasking and parallel processing are also possible or may be advantageous.

[0050] The various embodiments in this application are described in a progressive manner. Similar or identical parts between embodiments can be referred to mutually. Each embodiment focuses on describing the differences from other embodiments. In particular, the device, equipment, and storage medium embodiments are basically similar to the method embodiments, so the descriptions are relatively simple; relevant parts can be referred to the descriptions of the method embodiments.

[0051] The specific embodiments described above do not constitute a limitation on the scope of protection of this application. Those skilled in the art should understand that various modifications, combinations, sub-combinations, and substitutions can be made according to design requirements and other factors. Any modifications, equivalent substitutions, and improvements made within the spirit and principles of this application should be included within the scope of protection of this application.

Claims

1. A method for precise temperature control of a co-pyrolysis reactor, characterized in that, The method comprises: Performing mixed plastic co-pyrolysis multi-dimensional state analysis, and based on the collected mixed plastic co-pyrolysis multi-dimensional state analysis results, performing plastic co-pyrolysis reaction process identification to generate plastic co-pyrolysis reaction process identification results; Based on the plastic co-pyrolysis reaction process identification results, executing temperature control strategies corresponding to each mixed plastic co-pyrolysis reaction stage; During the execution of the temperature control strategy, the concentration of characteristic pollutants in the exhaust gas of the co-pyrolysis reactor is continuously monitored for co-pyrolysis gas emission safety, and based on the obtained co-pyrolysis gas emission safety monitoring results, it is judged whether to generate the highest priority intervention instruction, if yes, the overall temperature set point of the co-pyrolysis reactor is forcibly switched and stabilized at the preset low-risk set point, and co-pyrolysis hazardous gas continuous monitoring is performed, if not, a toxic gas warning is issued.

2. The method of claim 1, wherein the temperature of the co-pyrolysis reactor is precisely controlled by adjusting the temperature of the heating element. The specific process of the mixed plastic co-pyrolysis multi-dimensional state analysis is as follows: Obtain multi-source sensing data stream of the co-pyrolysis reactor; Performing plastic co-pyrolysis reaction process identification, the specific steps are: Step one, based on the obtained multi-source sensing data stream of the co-pyrolysis reactor, perform plastic co-pyrolysis state evaluation parameter extraction, and based on the extracted plastic co-pyrolysis state evaluation parameters, perform combination and normalization to obtain a plastic co-pyrolysis multi-dimensional feature vector; Step two, input the plastic co-pyrolysis multi-dimensional feature vector into the pre-trained classification model; Step three, send a control prompt to the co-pyrolysis reactor temperature control center, and based on the co-pyrolysis reaction stage probability distribution and the corresponding mixed plastic co-pyrolysis reaction stage confidence, determine the current mixed plastic co-pyrolysis reaction stage; The specific process of determining the current mixed plastic co-pyrolysis reaction stage is as follows: Obtain the reaction stage confidence corresponding to the highest probability value in the co-pyrolysis reaction stage probability distribution, if the reaction stage confidence is greater than the preset confidence threshold, the mixed plastic co-pyrolysis reaction stage corresponding to the current highest probability value is determined as the current dominant mixed plastic co-pyrolysis reaction stage; If the current dominant mixed plastic co-pyrolysis reaction stage is determined as a low-temperature dechlorination dominant period, start the dechlorination priority constant temperature control; If the current dominant mixed plastic co-pyrolysis reaction stage is determined as a warming-up transition period, start the co-pyrolysis warming-up and heat compensation control; If the current dominant mixed plastic co-pyrolysis reaction stage is determined as a high-temperature cracking dominant period, start the high-temperature steady-state control.

3. The method of claim 1, wherein the temperature of the co-pyrolysis reactor is precisely controlled by adjusting the temperature of the heating element. The mixed plastic co-pyrolysis multi-dimensional state analysis further comprises: Mark the preset classification model as the main classification model, and mark other preset classification models that do not contain the main classification model as the calibration classification model; Input the plastic co-pyrolysis multi-dimensional feature vector into the calibration classification model to output the co-pyrolysis reaction stage calibration probability distribution corresponding to the current mixed plastic co-pyrolysis reaction stage; Based on the output co-pyrolysis reaction stage probability distribution and the co-pyrolysis reaction stage calibration probability distribution, perform reaction stage process calibration, the specific process is as follows: If the mixed plastic co-pyrolysis reaction stages corresponding to the highest probability values determined by the main classification model and the calibration classification model are consistent, the current reaction stage is determined as the mixed plastic co-pyrolysis reaction stage; If the mixed plastic co-pyrolysis reaction stage determined by the main classification model and the calibration classification model is inconsistent, whether the confidence of the reaction stage corresponding to the highest probability value of the main classification model and the highest probability value of the calibration classification model is greater than the preset confidence threshold is determined; If yes, the reaction stage confidence based on the classification model is determined, and if no, a model inconsistency prompt is sent; The reaction stage confidence based on the classification model means determining whether the confidence of the reaction stage corresponding to the highest probability value of the main classification model is greater than the confidence of the reaction stage corresponding to the highest probability value of the calibration classification model, and if yes, the reaction stage corresponding to the highest probability value of the main classification model is determined as the mixed plastic co-pyrolysis reaction stage, and if not, the reaction stage corresponding to the highest probability value of the calibration classification model is determined as the mixed plastic co-pyrolysis reaction stage.

4. The method of claim 2, wherein the temperature of the co-pyrolysis reactor is precisely controlled by adjusting the temperature of the heating element. The specific process of the constant temperature regulation with dechlorination priority is as follows: Firstly, the target temperature of the co-pyrolysis reactor is set to a preset low-temperature dechlorination constant value, which serves as the basis for constant temperature control; Secondly, high-precision constant temperature control is started. The specific process of the high-precision constant temperature control is as follows: the co-pyrolysis heating temperature deviation value is obtained. The output power of the heater of the co-pyrolysis reactor is dynamically adjusted based on the incremental proportional-integral control algorithm, and the specific adjustment method is as follows: The co-pyrolysis heating temperature deviation value is input into the incremental proportional-integral control algorithm, the heating power adjustment amount is output, and the heating power adjustment amount is sent to the power adjustment unit of the heater. In the process of high-precision constant temperature control, hydrogen chloride concentration discrimination for real-time monitoring of the safety and dechlorination efficiency of plastic waste co-pyrolysis reaction is simultaneously performed.

5. The method of claim 4, wherein the temperature of the co-pyrolysis reactor is precisely controlled by adjusting the temperature of the heating fluid to a temperature that is within a range of 10°C of the temperature of the co-pyrolysis reactor. The specific process of the hydrogen chloride concentration discrimination is as follows: The hydrogen chloride concentration value is obtained. When the hydrogen chloride concentration value is not greater than the preset HCl second concentration threshold, the constant temperature regulation with dechlorination priority is continued to be performed. Otherwise, strong exhaust dynamic regulation is started, and the specific process is as follows: When the hydrogen chloride concentration value is greater than the preset HCl first concentration threshold, the co-pyrolysis reactor temperature control center outputs a step increment command. When the hydrogen chloride concentration value is not greater than the preset HCl first concentration threshold and greater than the preset HCl second concentration threshold, hydrogen chloride exhaust dynamic adjustment is performed, and the specific adjustment process is as follows: The hydrogen chloride concentration adjustment deviation value is obtained as the proportional adjustment input quantity of the feedback control module in the strong exhaust dynamic regulation loop. The preset HCl second concentration threshold is less than the preset HCl first concentration threshold. The product of the hydrogen chloride concentration adjustment deviation value and the preset proportional coefficient is taken as the exhaust valve position adjustment amount. The amplitude corresponding to the exhaust valve position adjustment amount is taken as the adjustment step, the valve opening of the exhaust valve position actuator is adjusted step by step in the direction of decreasing the hydrogen chloride concentration adjustment deviation value, and the corresponding exhaust valve position control signal is continuously output. The hydrogen chloride concentration value is continuously monitored, and when the hydrogen chloride concentration value is not greater than the preset HCl second concentration threshold value, the exhaust amount is maintained at the valve position determined in the last adjustment period, and the steady state maintenance stage is entered, otherwise, the hydrogen chloride exhaust dynamic adjustment is continuously executed, and when the number of times of execution of the hydrogen chloride exhaust dynamic adjustment is greater than the preset maximum number of adjustments, a hydrogen chloride exhaust dynamic adjustment failure prompt is sent.

6. The method of claim 2, wherein the temperature of the co-pyrolysis reactor is precisely controlled by adjusting the temperature of the heating element. The dechlorination priority constant temperature regulation further comprises: When the hydrogen chloride concentration value is monitored to be not greater than the preset HCl first concentration threshold value and greater than the preset HCl second concentration threshold value, a strong exhaust prompt is sent to the co-pyrolysis reactor temperature regulation center.

7. The method of claim 2, wherein the temperature of the co-pyrolysis reactor is precisely controlled by adjusting the temperature of the heating fluid to a temperature that is within a range of 10°C of the temperature of the co-pyrolysis reactor. The specific process of the co-pyrolysis temperature rising and heat compensation regulation is as follows: The specific prediction process is as follows: The plastic co-pyrolysis multi-dimensional feature vector is input into a preset thermal dynamic model, and a co-pyrolysis target temperature rising curve is output; Based on the co-pyrolysis temperature rising curve, a co-pyrolysis reference power overcoming the thermal inertia of the co-pyrolysis reactor is calculated; The co-pyrolysis heating power is obtained; The co-pyrolysis heating power is sent to the co-pyrolysis reactor temperature regulation center to generate a co-pyrolysis heating power instruction, and the co-pyrolysis heating power instruction is sent to the main power controller of the co-pyrolysis reactor for global power distribution and output; The temperatures of each partition of the co-pyrolysis reactor are monitored in parallel, and co-pyrolysis partition directional compensation heating is started in the co-pyrolysis reactor temperature rising lag area.

8. The method of claim 7, wherein the temperature of the co-pyrolysis reactor is precisely controlled by adjusting the temperature of the heating fluid to a temperature that is within a range of 10°C of the temperature of the co-pyrolysis reactor. The specific process of the parallel monitoring of the temperatures of each partition of the co-pyrolysis reactor and the starting of the co-pyrolysis partition directional compensation heating in the co-pyrolysis reactor temperature rising lag area is as follows: The co-pyrolysis reactor partition temperature rising rate is continuously monitored; When the co-pyrolysis reactor temperature rising lag duration is greater than the preset temperature rising lag time threshold value and the partition temperature rising rate deviation value is greater than the preset temperature rising lag temperature threshold value, the co-pyrolysis reactor partition is marked as a co-pyrolysis reactor temperature rising lag area; The specific process of the starting of the co-pyrolysis partition directional compensation heating based on the co-pyrolysis reactor temperature rising lag area is as follows: The lag compensation heating instruction is sent to the heater in the co-pyrolysis reactor temperature rising lag area; The co-pyrolysis temperature rising and heat compensation regulation is continuously performed.

9. The method of claim 2, wherein the temperature of the co-pyrolysis reactor is precisely controlled by adjusting the temperature of the heating element. The specific process of the high-temperature steady state regulation is as follows: The temperature regulation center switches and locks the high-temperature target temperature set point at the preset high-temperature target temperature; Based on the high-temperature target temperature, a multivariable decoupling steady state control is started, and the specific process is as follows: Based on the decoupling control algorithm, the power output of each partition heater of the co-pyrolysis reactor is adjusted; During the high-temperature steady state regulation, the co-pyrolysis gas discharge safety monitoring is simultaneously performed, and the specific process is as follows: The toxicity equivalent of dioxin substances is obtained; It is judged whether the toxicity equivalent of dioxin substances is greater than the preset dioxin risk threshold value, if yes, a toxic gas warning is issued, otherwise, the temperature regulation center generates a highest priority intervention instruction, forcibly switches and stabilizes the overall temperature set point of the co-pyrolysis reactor at the preset low risk set point, and continuously monitors the co-pyrolysis hazardous gas, and the specific process is as follows: If the toxicity equivalent of dioxin substances is not greater than the preset dioxin risk threshold value within the preset observation time, the high-temperature steady state regulation is continuously performed; If the toxicity equivalent of the dioxin-like substances is still greater than the preset dioxin risk threshold within the preset observation time, a toxic gas warning is issued.

10. A temperature precision control system of a co-pyrolysis reactor, applying a temperature precision control method of a co-pyrolysis reactor according to any one of claims 1-9, characterized in that, The method comprises the following steps: The mixed plastic co-pyrolysis multi-dimensional state monitoring module, the co-pyrolysis reactor temperature regulation module and the co-pyrolysis gas emission safety monitoring module are used for mixed plastic co-pyrolysis multi-dimensional state analysis, and plastic co-pyrolysis reaction progress identification is performed based on the collected mixed plastic co-pyrolysis multi-dimensional state analysis results to generate a plastic co-pyrolysis reaction progress identification result. The co-pyrolysis reactor temperature regulation module is used for executing a temperature regulation strategy corresponding to each mixed plastic co-pyrolysis reaction stage based on the result of the plastic co-pyrolysis reaction progress identification; The co-pyrolysis gas emission safety monitoring module is used for continuously monitoring the concentration of characteristic pollutants in the exhaust gas of the co-pyrolysis reactor during the execution of the temperature regulation strategy, and based on the obtained co-pyrolysis gas emission safety monitoring result, it is judged whether to generate the highest priority intervention instruction, if yes, the overall temperature set point of the co-pyrolysis reactor is forcibly switched and stabilized at the preset low-risk set point, and the co-pyrolysis hazardous gas continuous monitoring is performed, if not, a toxic gas warning is issued. ​

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