Tower top temperature control method, system and equipment for fluoride rectifying tower and medium

Abstract

The invention relates to the technical field of rectification tower control, provides a tower top temperature control method, system and equipment for a fluoride rectification tower and a storage medium, and aims to solve the problem of low temperature control stability in the rectification production process in the prior art. The actual condensation temperature is collected through the tower top temperature monitoring device in the branch pipe, and the deviation type and size between the actual condensation temperature and the target condensation temperature are judged; when the deviation is too high and exceeds a first preset deviation threshold value, a to-be-adjusted branch is determined, the model is called, a temperature track is predicted based on the fluoride load value and the temperature change trend, refrigerant adjusting parameters are calculated, and regulation and control are conducted through a condenser refrigerating system; when the deviation in adjustment is medium or the temperature is low, the opening degree of the condenser auxiliary heating system and the to-be-adjusted branch is adjusted through global optimization decision in combination with the fluoride load value and the deviation, the temperature can be accurately controlled, lag is reduced, the operation flexibility and automation degree of a rectifying tower are improved, and the purification quality requirement of fluoride products is met.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of rectifying column control, and in particular to a column top temperature control method, system, device and storage medium for a fluorine compound rectifying column. BACKGROUND

[0002] Chlorine trifluoride, chlorine pentafluoride and other fluorine compound gases are highly toxic and corrosive gases, and their rectification and purification need to remove light components such as fluorine gas and nitrogen gas, and heavy component impurities such as hydrogen fluoride and metal ions. In industry, a combination process of rectifying column and cryogenic heat exchanger is often used, and the column top output needs to be processed through pipeline, condenser, reflux pump and other equipment. The control precision of high-purity fluorine compound on the column top condensation temperature and reflux temperature is extremely high, and accurate column top temperature control is the core requirement to ensure product quality and reduce production risk.

[0003] At present, the column top temperature control method of the existing fluorine compound rectifying column mainly relies on the conventional combination architecture of the rectifying column and the cryogenic heat exchanger. The temperature data of the column top are collected by a column top temperature monitoring device, the control logic focuses on the basic adjustment of the condensation temperature and the reflux temperature, and the temperature stability is mainly maintained by adjusting the parameters of the condenser refrigeration system. The column top is processed through pipeline, condenser and reflux pump according to the established process.

[0004] However, the existing technology lacks specific process optimization for the column top fraction of the fluorine compound rectifying column. On the one hand, the deep cooling control mode has a significant temperature response lag phenomenon, and the cooling effect is difficult to accurately match the demand. On the other hand, the individual differences of the parallel branch pipes in the column top condenser are not considered, and it is difficult to achieve differentiated and accurate control, which cannot meet the strict temperature control requirements of high-purity fluorine compound. At the same time, the series connection of many devices also increases the leakage risk, which restricts the stability of rectification production and the product qualification rate. SUMMARY

[0005] The present application aims to provide a column top temperature control method, system, device and storage medium for a fluorine compound rectifying column to solve the problem of low temperature control stability in the existing rectification production process.

[0006] To solve the above technical problems, in a first aspect, the present application provides a column top temperature control method for a fluorine compound rectifying column, comprising:

[0007] In the rectification process, the actual condensation temperature of the column top in each branch pipe connected in parallel in the column top condenser is collected by a column top temperature monitoring device, and the column top temperature monitoring device is arranged in each branch pipe.

[0008] determining a deviation type to which a deviation between the actual condensation temperature and a target condensation temperature required by the fluorides belongs, the deviation type including a temperature deviation high type for indicating that the actual condensation temperature is higher than the target condensation temperature, and a temperature deviation low type for indicating that the actual condensation temperature is lower than the target condensation temperature;

[0009] in a case where the deviation type is the temperature deviation high type and the deviation is greater than a first preset deviation threshold, determining that a corresponding branch is a to-be-adjusted branch, and calling a pre-established branch dynamic thermodynamic model to predict a temperature variation trajectory of the to-be-adjusted branch within a future control period based on a fluorine load value and a temperature variation trend in the to-be-adjusted branch;

[0010] based on the temperature variation trajectory, the fluorine load value and the deviation, dynamically calculating a temperature adjustment parameter for temperature adjustment, the temperature adjustment parameter including an adjustment mode and a final adjustment duration, wherein the adjustment mode includes at least one of the following: adjusting a refrigerant temperature in a condensation pipeline of an external device of the to-be-adjusted branch and adjusting a refrigerant flow rate;

[0011] in a process of performing corresponding adjustment according to the adjustment mode and the final adjustment duration, when it is determined that the deviation is less than the first preset deviation threshold and greater than a second preset deviation threshold, or the deviation type is the temperature deviation low type, adjusting an opening degree between a condenser auxiliary heating system and the to-be-adjusted branch based on the fluorine load value and the deviation in the branch.

[0012] Optionally, the calling of the pre-established branch dynamic thermodynamic model to predict the temperature variation trajectory of the to-be-adjusted branch within the future control period based on the fluorine load value and the temperature variation trend in the to-be-adjusted branch includes:

[0013] integrating the actual condensation temperature and condensation temperature data at a plurality of historical time points of the same to-be-adjusted branch in chronological order to obtain an ordered temperature sequence;

[0014] based on the ordered temperature sequence, analyzing fluctuation variation rules of condensation temperature data at different time points to obtain a dynamic feature vector for reflecting a temperature variation trend;

[0015] quantitatively converting fluorine flow data of the to-be-adjusted branch at a current time point to obtain a fluorine load value, inputting the dynamic feature vector and the fluorine load value into the pre-established branch dynamic thermodynamic model, combining phase change characteristics of fluorine in a rectifying condensation process, and performing data fitting processing through the branch dynamic thermodynamic model to obtain a thermal dynamic response factor for characterizing a thermal inertia capability of the branch and a phase change latent heat influence factor for characterizing an influence of phase change latent heat on temperature variation;

[0016] The trajectory deduction operation is performed according to the correlation between the thermal dynamic response factor and the latent heat of phase change influencing factor, so as to obtain a temperature change trajectory of the to-be-adjusted branch in a future control period.

[0017] Optionally, the dynamic feature vector and the fluoride load value are jointly input into a pre-established branch dynamic thermodynamic model, and data fitting processing is performed on the branch dynamic thermodynamic model to obtain a thermal dynamic response factor for characterizing the thermal inertia capability of the branch and a latent heat of phase change influencing factor for characterizing the influence of the latent heat of phase change on temperature change, including:

[0018] Based on the temperature change rate information in the dynamic feature vector, the rate fluctuation law of the temperature change of the branch is analyzed to obtain an acceleration feature, and the acceleration feature and the fluoride load value are associated to obtain a thermal inertia weight reflecting the thermal response delay degree of the system;

[0019] The thermal inertia weight and the dynamic feature vector are cooperatively processed through a temperature trend processing rule in the branch dynamic thermodynamic model to obtain a thermal dynamic response factor;

[0020] Based on the similarity between the actual condensation temperature and the preset phase change temperature point of the fluoride, the urgency of phase change is quantitatively processed to obtain a phase change proximity coefficient, and the phase change proximity coefficient and the fluoride load value are associated to obtain a latent heat of phase change influencing factor.

[0021] Optionally, based on the fluoride load value and the deviation in the branch pipe, a global optimization decision is used to adjust the opening degree between the condenser auxiliary heating system and the to-be-adjusted branch.

[0022] Based on a preset compensation demand intensity determination rule in the auxiliary heating coordination mode, the deviation and the fluoride load value in the branch pipe in the adjustment process are associated to obtain a heat compensation demand intensity;

[0023] Based on a cooperative heating rule in the auxiliary heating coordination mode, the heat compensation demand intensity is rule-matching processed according to the phase change thermal characteristics of the fluoride in the rectification and condensation process to obtain a reference heating power of the condenser auxiliary heating system.

[0024] A heat transfer correlation rule between the to-be-adjusted branch and the condenser auxiliary heating system is established, and based on the heat transfer correlation rule and the actual condensation temperature of each to-be-adjusted branch, a global optimization decision is used to divide different heating urgency degrees to obtain a target branch heating priority sequence.

[0025] dynamically allocate the base heating power based on the target branch heating priority sequence and a power distribution rule in the auxiliary heating coordination mode to obtain an initial heating opening degree corresponding to each to-be-adjusted branch;

[0026] optimize the initial heating opening degree based on a thermal saturation state of the metal ball filler in the to-be-adjusted branch to obtain a final heating opening degree value, so as to complete coordination control of the opening degree between the condenser auxiliary heating system and the to-be-adjusted branch.

[0027] In a second aspect, the present application provides a tower top temperature control system for a fluorine rectification tower, comprising:

[0028] The acquisition module is configured to acquire actual condensation temperatures of the tower top in each branch pipe connected in parallel in the tower top condenser during the rectification process by a tower top temperature monitoring device arranged in each branch pipe one by one.

[0029] The determination module is configured to determine a deviation type to which a deviation between the actual condensation temperature and a target condensation temperature required by the fluorine belongs, the deviation type including a temperature deviation high type indicating that the actual condensation temperature is higher than the target condensation temperature, and a temperature deviation low type indicating that the actual condensation temperature is lower than the target condensation temperature.

[0030] The prediction module is configured to, in a case where the deviation type is the temperature deviation high type and the deviation is greater than a first preset deviation threshold, determine that a corresponding branch is a to-be-adjusted branch, and call a pre-established branch dynamic thermodynamic model to predict a temperature variation trajectory of the to-be-adjusted branch in a future control period based on a fluorine load value and a temperature variation trend in the to-be-adjusted branch.

[0031] The calculation module is configured to dynamically calculate a temperature adjustment parameter for temperature adjustment based on the temperature variation trajectory, the fluorine load value and the deviation, the temperature adjustment parameter including an adjustment mode and a final adjustment duration, and the adjustment mode including at least one of the following: adjusting a refrigerant temperature in a condensation pipeline of an external device of the to-be-adjusted branch and adjusting a refrigerant flow rate.

[0032] The adjustment module is configured to, in a process of corresponding adjustment according to the adjustment mode and the final adjustment duration, when it is determined that the deviation is less than the first preset deviation threshold and greater than a second preset deviation threshold, or the deviation type is the temperature deviation low type, adjust an opening degree between the condenser auxiliary heating system and the to-be-adjusted branch based on the fluorine load value and the deviation in the branch pipe by using a global optimization decision.

[0033] In a third aspect, the present application provides an electronic device, comprising:

[0034] a memory configured to store a computer program;

[0035] The processor is configured to execute the computer program to implement the steps of the column top temperature control method for a fluorine compound rectifying column according to the first aspect.

[0036] In a fourth aspect, the present application provides a computer readable storage medium, wherein a computer program is stored in the computer readable storage medium, and the computer program is configured to implement the steps of the column top temperature control method for a fluorine compound rectifying column according to the first aspect when executed by a processor.

[0037] The column top temperature control method for a fluorine compound rectifying column provided by the present application comprises the following steps: collecting actual condensation temperatures of the column top in each branch pipe of a parallel connection in a column top condenser in a rectifying process by a column top temperature monitoring device, wherein the column top temperature monitoring device is arranged in each branch pipe one by one; determining a deviation type to which a deviation between the actual condensation temperature and a target condensation temperature required by the fluorine compound belongs, wherein the deviation type comprises a temperature deviation high type for indicating that the actual condensation temperature is higher than the target condensation temperature, and a temperature deviation low type for indicating that the actual condensation temperature is lower than the target condensation temperature; in a case where the deviation type is the temperature deviation high type and the deviation is greater than a first preset deviation threshold, determining that a corresponding branch is an adjustment branch, and calling a pre-established branch dynamic thermodynamic model to predict a temperature variation trajectory of the adjustment branch in a future control period based on a fluorine compound load value and a temperature variation trend in the adjustment branch; dynamically calculating a temperature adjustment parameter for temperature adjustment based on the temperature variation trajectory, the fluorine compound load value and the deviation, wherein the temperature adjustment parameter comprises an adjustment mode and a final adjustment duration, and the adjustment mode comprises at least one of the following: adjusting a refrigerant temperature in a condensation pipeline arranged outside the adjustment branch and adjusting a refrigerant flow rate; in a process of performing corresponding adjustment according to the adjustment mode and the final adjustment duration, when it is determined that the deviation is less than the first preset deviation threshold and greater than a second preset deviation threshold, or the deviation type is the temperature deviation low type, adjusting an opening degree between a condenser auxiliary heating system and the adjustment branch based on the fluorine compound load value and the deviation in the branch.

[0038] The technical scheme of the present application has the following beneficial effects:

[0039] The present application can accurately obtain the real temperature condition of a single branch by collecting the actual condensation temperature in each branch, avoiding the deviation caused by overall monitoring; can determine the type and size of the deviation, and clearly determine the direction and degree of temperature deviation from the target value, providing a clear basis for subsequent adjustment; can accurately position the branch that needs to be adjusted by locking the branch to be adjusted and predicting the temperature trajectory, and can predict the temperature change trend in advance to reduce the adjustment lag; can form a targeted refrigeration adjustment scheme by calculating the refrigerant adjustment parameters, making the refrigeration operation more accurate; and can adapt to the medium deviation and low temperature deviation by adjusting the opening degree of the condenser auxiliary heating system and the branch, realizing the coordinated temperature control of refrigeration and heating, and maintaining the temperature stability.

[0040] Further, the present application integrates the actual condensation temperature of the same branch to be adjusted and the condensation temperature data at multiple historical time points into an ordered temperature sequence in time sequence, analyzes the fluctuation change rule of the temperature in the sequence to obtain a dynamic feature vector reflecting the temperature change trend, quantitatively converts the fluorine flow data at the current time into a fluorine load value, and inputs the dynamic feature vector and the fluorine load value into a pre-established branch dynamic thermodynamic model. Combined with the phase change characteristics of fluorine rectification condensation, the model data is adapted and processed to obtain a thermal dynamic response factor representing the thermal inertia ability of the branch and a phase change latent heat influence factor representing the influence of the phase change latent heat on the temperature change. Then, the trajectory is deduced in combination with the correlation between the two types of factors to obtain the temperature change trajectory of the branch to be adjusted in a future control period.

[0041] The present application extracts the temperature change trend characteristics by integrating historical and real-time temperature data, quantifies the fluorine load, and combines the fluorine phase change characteristics to process the model to obtain key factors affecting temperature change, and then accurately deduces the future temperature change trajectory of the branch, providing reliable data support for subsequent development of accurate temperature adjustment scheme. BRIEF DESCRIPTION OF DRAWINGS

[0042] In order to more clearly illustrate the technical solutions of the embodiments of the present application or the prior art, the following will briefly introduce the drawings needed to be used in the embodiment or prior art description. Obviously, the drawings in the following description are only some embodiments of the present application, and those skilled in the art can also obtain other drawings according to these drawings without creative labor.

[0043] Figure 1 A flowchart of a tower top temperature control method for a fluorine rectification tower provided by an embodiment of the present application;

[0044] Figure 2 A specific implementation diagram of a tower top temperature control method for a fluorine rectification tower provided by an embodiment of the present application;

[0045] Figure 3A structural schematic diagram of a tower top temperature control system for a fluorine rectification tower provided by an embodiment of the present application is provided.

[0046] Figure 4 A structural schematic diagram of an electronic device provided by an embodiment of the present application is provided. DETAILED DESCRIPTION

[0047] The control precision of fluorine rectification purification on the tower top temperature is extremely high, but the existing technology mostly adopts the overall temperature monitoring mode, it is difficult to accurately obtain the real temperature condition of each parallel branch pipe in the tower top condenser, and the deep cooling control mode has obvious response lag problem, and lacks differentiated adjustment scheme for each branch pipe. At the same time, the tower top production needs to pass through multiple equipment in series, which not only further aggravates the complexity of temperature control, but also increases the leakage risk, and cannot meet the production demand of high-purity fluorine.

[0048] To solve the above problems, the present application provides a tower top temperature control method for a fluorine rectification tower, by one-to-one corresponding setting of tower top temperature monitoring devices in each branch pipe to obtain accurate temperature data, and classified adjustment according to the deviation direction and size of temperature and target value: when the temperature is high and the deviation is large, the temperature change trajectory is predicted in advance and the refrigerant parameters are adjusted accordingly; when the temperature deviation is moderate or low, the opening of the condenser auxiliary heating system and the branch is optimized. The scheme realizes accurate temperature measurement and differentiated regulation of each branch pipe, effectively reduces the temperature control lag, at the same time simplifies the temperature control logic through targeted adjustment, reduces the leakage risk caused by equipment in series, and meets the rectification production requirements of high-purity fluorine.

[0049] In order for those skilled in the art to better understand the present application, the present application will be further described in detail below in combination with the drawings and specific embodiments. Obviously, the described embodiments are only part of the embodiments of the present application, not all. Based on the embodiments in the present application, all other embodiments obtained by those skilled in the art without creative labor are within the scope of protection of the present application.

[0050] The core of the present application is to provide a tower top temperature control method for a fluorine rectification tower, and a flowchart of one specific embodiment thereof is shown in Figure 1 The method comprises:

[0051] S101, in the rectification process, the actual condensation temperature of the tower top in each branch pipe connected in parallel in the tower top condenser is collected by a tower top temperature monitoring device, and the tower top temperature monitoring device is one-to-one corresponding to each branch pipe.

[0052] In the above scheme, the overhead temperature monitoring device refers to a device for real-time detection of the condensation temperature in the branch pipe of the overhead condenser, which has precise temperature measurement function and is configured one-to-one with each branch pipe to ensure independent collection of temperature data of a single branch pipe.

[0053] In the examples of the present application, before the fluoride distillation operation is formally carried out, a plurality of overhead temperature monitoring devices are installed in each parallel branch pipe of the overhead condenser according to the configuration principle that one branch pipe corresponds to one overhead temperature monitoring device. During installation, it is ensured that each device can directly contact the condensing medium in the branch pipe to avoid interference of the external environment on the temperature measurement results. In the present application, the condensing medium is also called condensing agent, refrigerant, coolant, etc. When the distillation process is started, all overhead temperature monitoring devices start the temperature measurement function at the same time, continuously capturing the condensation temperature data of the overhead position in the corresponding branch pipe. These real-time collected temperature data are directly transmitted to the temperature control unit to form independent temperature records of each branch pipe, providing raw data support for subsequent temperature analysis and adjustment operation.

[0054] In actual application, the overhead condenser of a certain fluoride distillation system has 8 parallel branch pipes, and the same type of overhead temperature monitoring device is configured for each branch pipe. The temperature measurement range of the device is -50℃ to 50℃, the temperature measurement accuracy is ±0.1℃, and the temperature of the condensing medium in the branch pipe can be captured in real time and the data can be transmitted synchronously. During the distillation and purification of chlorine trifluoride, the 8 overhead temperature monitoring devices start the collection work at the same time, and after 10 minutes, the stable actual condensation temperature data of each branch pipe are obtained, which are: 12.3℃ for branch pipe 1, 12.5℃ for branch pipe 2, 11.9℃ for branch pipe 3, 12.4℃ for branch pipe 4, 12.1℃ for branch pipe 5, 14.6℃ for branch pipe 6, 12.0℃ for branch pipe 7, and 12.2℃ for branch pipe 8. In this distillation production, according to the requirements of the fluoride purification process, the target condensation temperature is set to 12.3℃.

[0055] Through the above S101, independent and accurate collection of the temperature of each branch pipe can be realized, and the temperature deviation of a single branch pipe caused by overall monitoring is avoided, providing real and reliable basic data for subsequent targeted adjustment.

[0056] S102, determining the deviation type of the deviation between the actual condensation temperature and the target condensation temperature required by the fluoride, the deviation type including a temperature deviation type for indicating that the actual condensation temperature is higher than the target condensation temperature, and a temperature deviation type for indicating that the actual condensation temperature is lower than the target condensation temperature.

[0057] In the above scheme, the deviation type refers to a classification identifier distinguishing the deviation direction of the actual condensation temperature relative to the target condensation temperature, including a temperature deviation high type and a temperature deviation low type, the former corresponding to a case that the actual condensation temperature is higher than the target condensation temperature, and the latter corresponding to a case that the actual condensation temperature is lower than the target condensation temperature, for clearly defining the specific direction of temperature adjustment.

[0058] In the examples of the present application, the actual condensation temperature data of each branch pipe collected in the S101 step is first acquired, and then the target condensation temperature data preset for the fluorine compound rectification process is retrieved. The temperature deviation of each branch pipe is calculated through a set temperature deviation calculation formula, as follows: , wherein, is the temperature deviation of the branch pipe, is the actual condensation temperature collected in the branch pipe, is the target condensation temperature required for the fluorine compound rectification. After the calculation, the deviation type is determined according to the positive and negative of the deviation result. When the deviation result is positive, it means that the actual condensation temperature is higher than the target condensation temperature, corresponding to the determination of the temperature deviation high type. When the deviation result is negative, it means that the actual condensation temperature is lower than the target condensation temperature, corresponding to the determination of the temperature deviation low type. Finally, the determination of the deviation type of all branch pipes is completed.

[0059] In actual application, the fluorine compound rectification system of the S101 example is taken. The actual condensation temperatures of the 8 branch pipes are 12.3℃, 12.5℃, 11.9℃, 12.4℃, 12.1℃, 14.6℃, 12.0℃ and 12.2℃ respectively. The target condensation temperature set for this rectification process is 12.3℃. The deviation of each branch pipe is calculated through the temperature deviation calculation formula: the deviation of branch pipe 1 is 0℃, the deviation of branch pipe 2 is 0.2℃, the deviation of branch pipe 3 is -0.4℃, the deviation of branch pipe 4 is 0.1℃, the deviation of branch pipe 5 is -0.2℃, the deviation of branch pipe 6 is 2.3℃, the deviation of branch pipe 7 is -0.3℃, and the deviation of branch pipe 8 is -0.1℃. According to the deviation result, branch pipes 2, 4 and 6 are determined as the temperature deviation high type, and branch pipes 3, 5, 7 and 8 are determined as the temperature deviation low type. These deviation data and deviation types will be directly used in the subsequent S103 step to determine whether each branch pipe is a to-be-adjusted branch and to select the corresponding adjustment logic.

[0060] The above S102 can clearly define the direction of the temperature deviation of each branch pipe, provide a clear basis for subsequent targeted selection of refrigeration or heating adjustment mode, and avoid deviation in the adjustment direction. At the same time, combined with the deviation data, it lays a foundation for subsequent accurate matching of adjustment strength and adjustment strategy, guarantees the rationality and effectiveness of temperature adjustment, and helps to improve the smoothness of the overall temperature control process.

[0061] S103. When the deviation type is high temperature and the deviation is greater than the first preset deviation threshold, the corresponding branch is determined as the branch to be adjusted, and the pre-established dynamic thermodynamic model of the branch is called. Based on the fluoride load value and temperature change trend in the branch to be adjusted, the temperature change trajectory in the branch to be adjusted in the next control cycle is predicted.

[0062] As a specific implementation method, step S103 involves calling a pre-established dynamic thermodynamic model of the branch to be adjusted, and predicting the temperature change trajectory of the branch to be adjusted within a future control cycle based on the fluoride load value and temperature change trend within the branch to be adjusted, including:

[0063] Step 1031: Integrate the actual condensation temperature and the condensation temperature data of multiple historical moments of the same branch to be adjusted in chronological order to obtain an ordered temperature sequence.

[0064] Step 1032: Based on the ordered temperature sequence, analyze the fluctuation pattern of the condensation temperature data at different times to obtain a dynamic feature vector that reflects the temperature change trend.

[0065] Step 1033: Quantize and convert the fluoride flow data of the branch to be adjusted at the current time to obtain the fluoride load value. Input the dynamic feature vector and the fluoride load value into the pre-established branch dynamic thermodynamic model. Combine the phase change characteristics of fluoride in the distillation and condensation process, perform data adaptation processing through the branch dynamic thermodynamic model to obtain the thermal dynamic response factor for characterizing the thermal inertia of the branch and the phase change latent heat influence factor for characterizing the effect of phase change latent heat on temperature change.

[0066] Step 1033 may specifically include the following steps: based on the temperature change rate information in the dynamic feature vector, analyze the fluctuation law of the branch temperature change rate to obtain acceleration features; correlate the acceleration features with the fluoride load value to obtain a thermal inertia weight reflecting the degree of system thermal response hysteresis; through the temperature trend processing rules in the branch dynamic thermodynamic model, perform collaborative processing on the thermal inertia weight and the dynamic feature vector to obtain a thermal dynamic response factor; based on the similarity between the actual condensation temperature and the preset fluoride phase change temperature point, quantify the urgency of phase change to obtain a phase change proximity coefficient; correlate and fuse the phase change proximity coefficient with the fluoride load value to obtain a phase change latent heat influence factor.

[0067] Step 1034: Combining the correlation between the thermal dynamic response factor and the latent heat of phase change influence factor, perform trajectory extrapolation to obtain the temperature change trajectory of the branch to be adjusted within a future control cycle.

[0068] In the above scheme, the first preset deviation threshold refers to a temperature deviation critical value for judging whether targeted adjustment needs to be started, and is used to screen branches with high temperature and excessive deviation. For example, the first preset deviation threshold can be 2°C, and the value of the threshold is not limited in the embodiments of the present application. The branch to be adjusted refers to a branch that needs to be adjusted for refrigeration because the deviation type is high temperature and the deviation is greater than the first preset deviation threshold.

[0069] The branch dynamic thermodynamic model refers to a preset model for analyzing the temperature change rule of the branch and predicting the temperature trajectory, which combines the phase change characteristics of fluorides and the heat transfer rule of the branch. The ordered temperature sequence refers to a set of condensation temperature data of the same branch to be adjusted at current and multiple historical time points arranged in chronological order. The dynamic feature vector refers to a data carrier obtained based on the analysis of the ordered temperature sequence and used to quantitatively reflect the temperature fluctuation trend.

[0070] The fluorine load value refers to a parameter obtained by quantitatively converting the fluorine flow data at the current time point and representing the amount of fluorine material in the branch. The thermal dynamic response factor refers to a quantitative index representing the thermal inertia capability of the branch and reflecting the lag degree of temperature change. The phase change latent heat influence factor refers to a quantitative index representing the influence degree of the phase change latent heat of fluorides on temperature change. The acceleration feature refers to a parameter obtained based on the analysis of the temperature change rate information and reflecting the fluctuation speed of the temperature change rate. The thermal inertia weight refers to a weight value obtained by correlating the acceleration feature and the fluorine load value and reflecting the lag degree of the system thermal response. The phase change proximity coefficient refers to a parameter obtained by quantitatively reflecting the similarity between the actual condensation temperature and the phase change temperature point of fluorides and reflecting the urgency of phase change.

[0071] The temperature trend processing rule refers to a quantitative rule combining the thermal inertia weight and the dynamic feature vector, specifically, the temperature change trend is quantified by weighted summation, and the weight distribution is that the thermal inertia weight accounts for 0.4 and the trend quantization value corresponding to the dynamic feature vector accounts for 0.6, that is, the thermal dynamic response factor is calculated by the rule. The temperature change trajectory refers to the temperature change path of the branch to be adjusted in a future control period, which is deduced based on the correlation between the thermal dynamic response factor and the phase change latent heat influence factor.

[0072] In the embodiments of the present application, in step 1032, the temperature data in the ordered temperature sequence is analyzed, the temperature change rate of adjacent time points is calculated, the duration and amplitude features of temperature rise or fall are extracted, and the dynamic feature vector is formed after quantization to reflect the temperature change trend.

[0073] Then, step 1033 is performed, the fluorine flow data of the branch to be adjusted at the current time point is obtained, the fluorine load value is calculated by a quantization conversion formula, and the formula is: In the formula, Q is the fluoride load value, in kg / h; F is the fluoride flow rate at the current moment, in kg / h. ; The density of the fluoride under current operating conditions is given in units of... 60 is a unit conversion factor used to convert seconds to minutes. Then, based on the temperature change rate information in the dynamic feature vector, the difference in temperature change rates between two adjacent moments is calculated to obtain the acceleration feature, as shown in the formula. In the formula, a represents the acceleration characteristic; The rate of temperature change at time n is expressed in °C / min. The rate of temperature change at time n-1 is expressed in °C / min. The time interval between two adjacent moments is expressed in minutes. The thermal inertia weight is obtained by multiplying the acceleration characteristic value by the fluoride load value, using the following formula: In the formula, W represents the thermal inertia weight; a represents the acceleration characteristic; and Q represents the fluoride load value. Subsequently, the thermal dynamic response factor is calculated according to the temperature trend processing rule. This rule specifically involves a weighted summation quantification of the continuous temperature change trend, with the weight allocation as follows: thermal inertia weight accounts for 0.4, and the trend quantification value corresponding to the dynamic characteristic vector accounts for 0.6. The formula is: In the formula, R is the thermal dynamic response factor; W is the thermal inertia weight; and V is the trend quantization value corresponding to the dynamic feature vector, which is a quantization value between 0 and 1. The more obvious the heating trend, the more similar the value is (1); the more obvious the cooling trend, the more similar the value is (0). Then, the preset fluoride phase transition temperature point is retrieved, and the phase transition proximity coefficient is calculated using the formula: In the formula, K is the phase transition proximity coefficient; This is the actual condensation temperature; The preset fluoride phase transition temperature is used. The latent heat of phase transition influence factor is obtained by weighting and summing the phase transition proximity coefficient and the fluoride load value, as shown in the formula: In the formula, L is the latent heat of phase change influence factor; K is the phase change proximity coefficient; and Q is the fluoride load value.

[0074] Finally, step 1034 is executed to perform correlation analysis between the thermal dynamic response factor and the latent heat of phase change influence factor. The temperature change path of the branch to be adjusted within a future control cycle is deduced by linear fitting, and the temperature change trajectory is obtained.

[0075] In practical applications, the fluoride rectification system example is continued, the first preset deviation threshold is set to 2, the deviations of the 8 branches are 0℃, 0.2℃, -0.4℃, 0.1℃, -0.2℃, 2.3℃, -0.3℃, -0.1℃, among which branches 2, 4 and 6 are temperature high type, and only the deviation of branch 6 is 2.3℃ which is greater than the first preset deviation threshold 2, so branch 6 is determined as the to-be-adjusted branch. First, collect the condensation temperature data of branch 6 in the past 5 time points and the current time, which are 10.2℃, 11.0℃, 11.8℃, 12.5℃, 13.3℃ and 14.6℃, and integrate them into an ordered temperature sequence in chronological order.

[0076] Then, the temperature change rates of adjacent time points are calculated as 0.8℃ / min, 0.8℃ / min, 0.7℃ / min, 0.8℃ / min and 1.3℃ / min, the features of temperature rise lasting for 5 time points and the average amplitude of 0.88℃ / min are extracted, and the trend quantization value corresponding to the dynamic feature vector is quantized to 0.92.

[0077] Subsequently, since the fluoride flow rate of branch 6 at the current time is , the fluoride density at the current working condition is , the fluoride load value is calculated by the quantization conversion formula: , wherein Q is the fluoride load value, with the unit of kg / h; F is the fluoride flow rate at the current time, with the unit of ; is the density of fluoride at the current working condition, with the unit of kg / m³; 60 is the unit conversion coefficient for converting seconds to minutes, and the data is substituted to get . The acceleration feature is calculated based on the temperature change rate, the rates of the last two time points are 0.8℃ / min and 0.8℃ / min, the time interval is 1 min, and the formula is: , wherein a is the acceleration feature; is the temperature change rate at the nth time point, with the unit of ℃ / min; is the temperature change rate at the (n-1)th time point, with the unit of ℃ / min; is the time interval of adjacent two time points, with the unit of min. The data is substituted to get . The thermal inertia weight is calculated by the formula: , wherein W is the thermal inertia weight; a is the acceleration feature; Q is the fluoride load value. The data is substituted to get .

[0078] The thermal dynamic response factor is calculated according to the temperature trend processing rule, and the formula is: , wherein R is a thermal dynamic response factor; W is a thermal inertia weight; V is a trend quantization value corresponding to a dynamic characteristic vector, the value being a quantization value between 0 and 1, the more obvious the temperature rising trend, the more similar the value to 1, and the more obvious the temperature falling trend, the more similar the value to 0. Substituting the data into the formula obtains . The preset fluoride phase transition temperature point is 15.0℃, and the phase transition proximity coefficient is calculated by the formula: , wherein K is the phase transition proximity coefficient; is an actual condensing temperature; is a preset fluoride phase transition temperature point, and substituting the data into the formula obtains . The phase change latent heat influence factor is calculated by the formula: , wherein L is the phase change latent heat influence factor; K is the phase transition proximity coefficient; Q is the fluoride load value, and substituting the data into the formula obtains .

[0079] Finally, the temperature change trajectory of the branch pipe 6 in a future control period is obtained by linear fitting and deducing the thermal dynamic response factor 0.552 and the phase change latent heat influence factor 0.662, that is, the temperature rises to 15.0℃ at an average rate of 0.6℃ / min and then remains stable, and the trajectory is directly used in the subsequent step S104 to calculate the refrigerant adjustment mode and the final adjustment time.

[0080] Through the above S103, the branch to be adjusted that needs to be adjusted can be accurately screened out, the historical and real-time data are integrated, the fluoride phase change characteristics and the clear temperature trend processing rule are combined, the temperature change trajectory is predicted in advance, a reliable basis is provided for subsequent accurate refrigeration adjustment scheme, and adjustment lag and blindness are reduced.

[0081] S104, based on the temperature change trajectory, the fluoride load value and the deviation, dynamically calculating a temperature adjustment parameter for temperature adjustment, the temperature adjustment parameter including an adjustment mode and a final adjustment time, wherein the adjustment mode includes at least one of the following: adjusting the refrigerant temperature in the condensing pipeline of the external device of the branch to be adjusted and adjusting the refrigerant flow.

[0082] As a specific implementation, step S104, based on the temperature change trajectory, the fluoride load value and the deviation, dynamically calculating a temperature adjustment parameter for temperature adjustment, the temperature adjustment parameter including an adjustment mode and a final adjustment time, includes:

[0083] Step 1041, using a trajectory analysis method to perform feature recognition on the temperature change trajectory to obtain a temperature peak deviation, and performing weighted fusion processing on the temperature peak deviation and the deviation to obtain a comprehensive adjustment strength. The trajectory analysis method can be a method capable of positioning the highest temperature point. It needs to be noted that the specific type of the trajectory analysis method is not limited in the present application.

[0084] Step 1042, based on the comprehensive adjustment intensity and the fluoride load value, querying the corresponding adjustment mode and the basic adjustment duration from a pre-established fluoride adjustment strategy mapping table.

[0085] Step 1043, combining the thermal buffering characteristics of the metal ball filler inside the branch to be adjusted, adaptively correcting the basic adjustment duration to lengthen the adjustment duration when the thermal buffering effect is significant, and shorten the adjustment duration when the thermal buffering effect is weak, to obtain the final adjustment duration.

[0086] Step 1044, combining the adjustment mode and the final adjustment duration according to a preset parameter integration rule to form a temperature adjustment parameter.

[0087] In the above scheme, the temperature adjustment parameter refers to a core parameter set for guiding the temperature adjustment operation, including the adjustment mode and the final adjustment duration, for clearly indicating "how to adjust" and "how long to adjust"; the temperature peak deviation refers to the difference between the highest temperature in the temperature change trajectory and the target condensation temperature, for quantifying the maximum deviation that the future temperature can reach; the comprehensive adjustment intensity refers to a quantitative index obtained by fusing the temperature peak deviation and the current deviation, for reflecting the urgency and required intensity of temperature adjustment;

[0088] The fluoride adjustment strategy mapping table refers to a pre-set associated data table that records the adjustment mode and the basic adjustment duration corresponding to different comprehensive adjustment intensities and fluoride load values; the basic adjustment duration refers to the initial adjustment time directly queried from the mapping table, without considering the specific thermal characteristics of the branch; the metal ball filler thermal buffering characteristics refer to the ability of the metal ball filler to absorb and release heat, and the thermal buffering effect is significant, that is, the filler can absorb more heat to slow down temperature change, and the effect is weak, that is, the ability to absorb heat is poor; the final adjustment duration refers to the actual adjustment time of the basic adjustment duration after the thermal buffering characteristics correction, which is more suitable for the real working condition of the branch; the parameter integration rule refers to a unified rule for combining the adjustment mode and the final adjustment duration into a standard temperature adjustment parameter.

[0089] In the examples of the present application, first, step 1041 is performed, a trajectory analysis method is used to identify the characteristics of the temperature change trajectory, locate the highest temperature point in the trajectory, calculate the difference between the highest temperature and the target condensation temperature to obtain the temperature peak deviation, and then calculate the comprehensive adjustment intensity by a weighted fusion formula, the formula is: , wherein S is the comprehensive adjustment intensity, P is the temperature peak deviation, D is the deviation at the current time, and 0.6 and 0.4 are the weight coefficients of the temperature peak deviation and the deviation, respectively, for highlighting the influence of future temperature risk on adjustment decision.

[0090] Then, step 1042 is performed, and the calculated comprehensive adjustment intensity and the fluoride load value determined in S103 are taken as joint query conditions to match in a pre-established fluoride adjustment strategy mapping table. The mapping table has preset adjustment modes corresponding to different comprehensive adjustment intensity and fluoride load combinations according to a large amount of experimental data, including reducing the refrigerant temperature, increasing the refrigerant flow, or a combination of the two, while associating the corresponding basic adjustment duration. After matching, the corresponding adjustment mode and basic adjustment duration are directly obtained.

[0091] Then, step 1043 is performed, and the real-time temperature data of the metal ball packing at different depths in the branch to be adjusted is collected by the distributed temperature sensing network arranged in the packing, and the average temperature is calculated. The strength of the heat buffering effect is judged in combination with the preset heat absorption upper limit of the packing. If the average temperature of the packing is similar to the heat absorption upper limit, it indicates that the heat buffering effect is significant, and the adjustment duration needs to be extended to offset the influence of the subsequent release of heat by the packing; if the average temperature of the packing is much lower than the heat absorption upper limit, it indicates that the heat buffering effect is weak, and the adjustment duration can be shortened to avoid over-adjustment. The basic adjustment duration is adaptively corrected according to the strength of the effect to obtain the final adjustment duration.

[0092] Finally, step 1044 is performed, and the obtained adjustment mode and the obtained final adjustment duration are combined according to the preset parameter integration rule to form complete temperature adjustment parameters containing explicit operation instructions and time parameters, which are used to directly control the action of related adjustment equipment.

[0093] In actual application, the fluoride rectification system of S103 is taken as an example, the branch to be adjusted is branch 6, the temperature change trajectory peak value is 15.0℃, the target condensing temperature is 12.3℃, the current deviation is 2.3℃, and the fluoride load value is 0.384kg / h. In step 1041, the temperature peak deviation is calculated first . Then, the comprehensive adjustment intensity is calculated by the comprehensive adjustment intensity formula .

[0094] Then, the comprehensive adjustment intensity 2.54 and the fluoride load value 0.384kg / h are taken as conditions to query the pre-established fluoride adjustment strategy mapping table. For example, the matched adjustment mode is to increase the refrigerant flow, and the basic adjustment duration is 5 minutes.

[0095] Then, the real-time temperature data of the metal ball packing in branch 6 is collected by the distributed temperature sensing network, and the average temperature is calculated to be 14.8℃. The preset heat absorption upper limit of the packing corresponds to a temperature of 15.2℃, and it is judged that the heat buffering effect is significant. The basic adjustment duration is extended by 20%, and the final adjustment duration is calculated by the formula: , wherein is the final adjustment duration, To adjust the length of time, k is the adjustment time correction factor, the data into the formula, the final adjustment time minutes.

[0096] Finally, according to the parameter integration rule combination, the temperature adjustment parameter is obtained as adjusting the refrigerant flow and adjusting the length of time 6 minutes. The parameter will be directly used to control the refrigerant flow adjustment valve of the condenser pipeline outside the branch 6, and provide clear operation basis for real-time monitoring of the deviation in the subsequent adjustment process and whether to switch the adjustment mode.

[0097] Through the above S104, the adjustment parameters are calculated by combining the future temperature change trend and the actual heat characteristics of the branch, so that the adjustment mode and the length of time are accurately adapted to the working conditions of the branch to be adjusted, which avoids both the insufficient adjustment that causes the temperature to deviate continuously and the excessive adjustment that causes resource waste, and provides reliable operation basis for subsequent precise temperature control.

[0098] S105, in the process of corresponding adjustment according to the adjustment mode and the final adjustment time, when it is determined that the deviation is less than the first preset deviation threshold and greater than the second preset deviation threshold, or the deviation type is the temperature low type, the opening between the condenser auxiliary heating system and the branch to be adjusted is adjusted based on the fluorine load value and the deviation in the branch. For example, the second preset deviation threshold is 0.3℃, and the numerical value of the threshold is not specifically limited in this embodiment.

[0099] As a specific implementation, step S105, based on the fluorine load value and the deviation in the branch, the opening between the condenser auxiliary heating system and the branch to be adjusted is adjusted by global optimization decision, comprising:

[0100] Step 1051, based on the compensation demand intensity determination rule in the preset auxiliary heating coordination mode, the deviation in the adjustment process and the fluorine load value in the branch are associated and processed to obtain the heat compensation demand intensity.

[0101] Step 1052, based on the cooperative heating rule in the auxiliary heating coordination mode, the heat compensation demand intensity is matched and processed according to the phase change heat characteristics of fluorine in the rectification and condensation process, to obtain the reference heating power of the condenser auxiliary heating system.

[0102] Step 1053, the heat transfer association rule between the branch to be adjusted and the condenser auxiliary heating system is established, based on the heat transfer association rule and the actual condensation temperature of each branch to be adjusted, the global optimization decision is adopted to divide different heating urgency, and the target branch heating priority sequence is obtained.

[0103] The step 1053 can specifically include the following steps: using a preset coupling analysis method of space and heat characteristics, comprehensively analyzing the spatial distribution position, heat transfer characteristics and heat transfer path differences of each to-be-adjusted branch, obtaining the corresponding relationship between the spatial position, heat transfer efficiency and heat distribution proportion, performing rule extraction processing on the corresponding relationship, and obtaining the heat transfer correlation rule between the to-be-adjusted branch and the condenser auxiliary heating system; calculating the difference between the actual condensing temperature and the target condensing temperature of each to-be-adjusted branch in the adjustment process to obtain the temperature deviation degree, and analyzing the change trend of the actual condensing temperature to obtain the emergency degree corresponding to the temperature change trend; combining the rectification characteristics of fluorides and the heat transfer correlation rule, using global optimization decision to perform weighted integration processing on the temperature deviation degree and the emergency degree, and obtaining the heating urgency evaluation value of each to-be-adjusted branch; performing numerical sorting processing on all the heating urgency evaluation values to obtain a preliminary branch heating priority sequence; combining the heat capacity saturation and thermal response characteristics of the metal ball filler inside each to-be-adjusted branch, performing dynamic fine-tuning processing on the preliminary branch heating priority sequence to obtain a target branch heating priority sequence.

[0104] Step 1054, based on the target branch heating priority sequence and the power distribution rule in the auxiliary heating coordination mode, performing dynamic distribution processing on the reference heating power to obtain the initial heating opening degree corresponding to each to-be-adjusted branch.

[0105] Step 1055, combining the heat saturation state of the metal ball filler inside the to-be-adjusted branch, performing optimization adjustment on the initial heating opening degree to obtain a final heating opening degree value, so as to complete the coordination control of the opening degree between the condenser auxiliary heating system and the to-be-adjusted branch.

[0106] The step 1055 can specifically include the following steps: using a distributed temperature sensing network arranged in the metal ball filler in the branch to be adjusted, collecting temperature data at different depths of the filler in real time, based on the temperature data, combining the heat absorption upper limit of the metal ball filler and the difference in the packing density of the filler, performing graphing processing on the temperature distribution law at different depths to obtain a heat saturation distribution graph of the metal ball filler; based on the heat saturation distribution graph, analyzing the attenuation degree of the overall heat buffering capacity of the metal ball; combining the deviation data and the deviation change rate of the branch to be adjusted, quantitatively converting the attenuation degree to obtain a heat buffering capacity coefficient; combining the fluorine load value in the branch and the dynamic response characteristics of the condenser auxiliary heating system, performing dynamic adaptation processing on the heat buffering capacity coefficient and the initial heating opening to obtain a heating opening dynamic adjustment factor; based on the heating opening dynamic adjustment factor, combining the phase change characteristics of fluorine in the rectification condensation process, performing real-time correction processing on the initial heating opening to obtain an intermediate heating opening value; combining the real-time heat supply margin of the condenser auxiliary heating system, performing range constraint processing on the intermediate heating opening value to obtain a final heating opening value.

[0107] In the above scheme, the auxiliary heating coordination mode refers to a comprehensive regulation framework integrating compensation demand determination, heating power matching, priority division and power allocation, including compensation demand intensity determination rules, collaborative heating rules and power allocation rules; the compensation demand intensity determination rules refer to the quantitative rules for calculating the heat compensation demand associated with the deviation and the fluorine load; the heat compensation demand intensity refers to a quantitative index representing how much heat needs to be supplemented by the branch;

[0108] The collaborative heating rules refer to the rules for matching the heat compensation demand with the reference heating power in combination with the phase change heat characteristics of fluorine, specifically, the heat compensation demand intensity 0-1 corresponds to the reference heating power 10%-50% of the rated power, which is matched according to a linear mapping relationship, i.e., reference heating power = rated heating power x (0.1+0.4x heat compensation demand intensity); the reference heating power refers to the initial heating power of the condenser auxiliary heating system matched based on the heat compensation demand intensity;

[0109] The heat transfer correlation rules refer to the rules for defining the heat distribution relationship between the branch to be adjusted and the condenser auxiliary heating system, specifically, when the spatial position distance of the branch to the heating source is ≤0.5m, the heat distribution proportion is 0.3, when the spatial position distance is in the range of 0.5-1.0m, the heat distribution proportion is 0.25, and when the spatial position distance is >1.0m, the heat distribution proportion is 0.2, the actual distribution weight is calculated by combining the heat transfer efficiency coefficient 0.8-1.0, i.e., actual distribution weight = distance distribution proportion x heat transfer efficiency coefficient;

[0110] The global optimization decision refers to a decision-making mode for determining the heating priority by comprehensively considering multiple factors; the heating urgency refers to an evaluation value reflecting the emergency degree of the branch needing heating; the target branch heating priority sequence refers to the sequence of branches obtained by sorting the heating urgency; the coupling analysis mode of space and thermal characteristics refers to an analysis method that comprehensively considers the spatial position, heat transfer characteristics and path difference of the branch; the heat capacity saturation degree refers to the proportion of the heat absorbed by the metal ball filler to the upper limit of heat absorption; the power distribution rule refers to a rule for distributing the reference heating power according to the heating priority, specifically, 40% for priority 1, 30% for priority 2, 20% for priority 3, 10% for priority 4 and below, and the total proportion being 100%;

[0111] The initial heating opening degree refers to the initial opening degree of the branch heating obtained according to the power distribution rule; the heat saturation state refers to the saturation degree of the metal ball filler after absorbing heat; the final heating opening degree value refers to the actual heating opening degree after optimization and adjustment of the heat saturation state; the heat saturation distribution map refers to a map reflecting the heat saturation state of the metal ball filler at different depths; the attenuation degree of the heat buffering capacity refers to the weakening degree of the heat buffering capacity of the metal ball filler with the change of heat absorption; the heat buffering capacity coefficient refers to an index quantifying the attenuation degree of the heat buffering capacity; the heating opening degree dynamic adjustment factor refers to an opening degree adjustment coefficient adapted based on the heat buffering capacity coefficient; the intermediate heating opening degree value refers to the heating opening degree after correction of the heat buffering characteristics; the heat supply margin refers to the additional heat supply available in real time for the condenser auxiliary heating system.

[0112] In the examples of the present application, first, step 1051 is performed to obtain the real-time deviation and fluorine load value of the branch pipe, and the heat compensation demand intensity is calculated according to the compensation demand intensity determination rule by the formula: , wherein C is the heat compensation demand intensity, the value range is 0-1, E is the real-time deviation, Q is the fluorine load value, and 0.7 and 0.3 are the weight coefficients of the deviation and the fluorine load value, is the preset maximum allowed deviation, which is used to normalize the calculation result to the range of 0-1.

[0113] Then, step 1052 is performed to call the collaborative heating rule in the auxiliary heating coordination mode, and the calculated heat compensation demand intensity is substituted into the linear mapping formula of the collaborative heating rule to calculate the reference heating power of the condenser auxiliary heating system, according to the phase change heat characteristics of fluorine in the rectification and condensation process, the formula is: , wherein is the reference heating power, is the rated heating power of the condenser auxiliary heating system, C is the heat compensation demand intensity, and 0.1 and 0.4 are the rule preset coefficients for establishing the correlation between the heat compensation demand and the heating power.

[0114] Then, step 1053 is performed, first, the preset space and thermal characteristic coupling analysis mode is used to collect the space distribution position, heat transfer characteristic and heat transfer path difference data of each to-be-adjusted branch, the actual distribution weight of each branch is calculated in combination with the heat transfer correlation rule; the difference between the actual deviation of each branch and the target condensing temperature is calculated to obtain the temperature deviation degree, and the change trend of the actual condensing temperature is analyzed, the emergency degree corresponding to the temperature rising trend is 0.3-0.5, and the emergency degree corresponding to the temperature stable trend or temperature falling trend is 0.1-0.3;

[0115] Then, the temperature deviation degree and the emergency degree are weighted and integrated by a formula to obtain the heating urgency evaluation value of each to-be-adjusted branch, in combination with the distillation characteristics of fluorides and the heat transfer correlation rule and by using global optimization decision-making, the formula is: In the formula, U is the heating urgency evaluation value, D is the normalized value of the temperature deviation degree, the value range is 0-1, J is the emergency degree, W is the actual distribution weight, and 0.5, 0.3 and 0.2 are the weight coefficients corresponding to each factor; the heating urgency evaluation values of all to-be-adjusted branches are sorted in descending order to obtain a preliminary branch heating priority sequence;

[0116] Finally, the heat capacity saturation and thermal response characteristics of the metal ball packing in each to-be-adjusted branch are collected, and the preliminary branch heating priority sequence is dynamically fine-tuned, the priority of the branch with high heat capacity saturation is appropriately reduced, and the priority of the branch with good thermal response characteristics is appropriately increased to obtain a target branch heating priority sequence.

[0117] Then, step 1054 is performed, the reference heating power is dynamically distributed according to the target branch heating priority sequence according to the power distribution rule in the auxiliary heating coordination mode, the higher the priority of the branch, the greater the power proportion allocated to the branch, and the initial heating opening degree corresponding to each to-be-adjusted branch is determined according to the power proportion allocated, and the power proportion and the initial heating opening degree are in a positive correlation relationship.

[0118] Finally, step 1055 is performed, the temperature data at different depths of the metal ball packing in the to-be-adjusted branch are collected in real time through the distributed temperature sensing network arranged in the metal ball packing, based on the temperature data, in combination with the heat absorption upper limit of the metal ball packing and the packing density difference, the temperature distribution law at different depths is graphically processed to generate a heat saturation distribution map of the metal ball packing; based on the heat saturation distribution map, the attenuation degree of the overall heat buffering capacity of the metal ball packing is analyzed, and the attenuation degree is quantitatively converted into a heat buffering capacity coefficient in combination with the real-time deviation data and the deviation change rate of the to-be-adjusted branch;

[0119] The heat buffering capacity coefficient and the initial heating opening degree are dynamically adapted by a formula based on the fluoride load value in the branch pipe and the dynamic response characteristics of the condenser auxiliary heating system, to obtain a heating opening degree dynamic adjustment factor, and the formula is: , wherein F is the heating opening degree dynamic adjustment factor, is the heat buffering capacity coefficient, 0.9 and 0.2 are the adaptation coefficients; based on the heating opening degree dynamic adjustment factor, the initial heating opening degree is multiplied by the adjustment factor to obtain an intermediate heating opening degree value, in combination with the phase change characteristics of the fluoride in the rectification condensing process; the real-time heating capacity margin of the condenser auxiliary heating system is called, if the heating power corresponding to the intermediate heating opening degree value exceeds the heating capacity margin range, the intermediate heating opening degree value is constrained to the upper limit or the lower limit corresponding to the heating capacity margin to obtain the final heating opening degree value, and the coordination control of the opening degree between the condenser auxiliary heating system and the branch to be adjusted is completed.

[0120] In actual application, the fluoride rectification system example is taken as an example, the first preset deviation threshold is 2°C, the second preset deviation threshold is 0.3°C, the rated heating power of the condenser auxiliary heating system is 10 kW, and the preset maximum allowed deviation is 5°C. In the process of adjusting the branch pipe 6 according to S104 parameters, it is found that the branch pipe 3 deviation is -0.4°C, which belongs to the low temperature type, the branch pipe 5 deviation is -0.2°C, which belongs to the low temperature type, the branch pipe 6 deviation is reduced to 1.8°C, which is less than 2°C and greater than 0.3°C, the branch pipe 7 deviation is -0.3°C, which is equal to the second preset deviation threshold and is included in the adjustment range, and the four branch pipes are all the branch pipes to be adjusted.

[0121] Firstly, the fluoride load value of the branch pipe 6 is 0.384 kg per hour, and the deviation is 1.8°C. The heat compensation demand intensity is calculated by the formula: , wherein C is the heat compensation demand intensity, E is the real-time deviation, Q is the fluoride load value, is the preset maximum allowed deviation, and the data is substituted to obtain . The deviation of the branch pipe 3 is 0.4°C, the load is 0.35 kg per hour, the calculated C is 0.077; the deviation of the branch pipe 5 is 0.2°C, the load is 0.36 kg per hour, the calculated C is 0.0496; the deviation of the branch pipe 7 is 0.3°C, the load is 0.37 kg per hour, and the calculated C is 0.0642.

[0122] Then, the C value of the branch pipe 6 is taken as the core to match the overall reference heating power, and the formula is: , wherein is the reference heating power, is the rated heating power, and C is the heat compensation demand intensity. The data is substituted to obtain kW.

[0123] Then, branch pipe 6, being 0.4 meters from the heating source, corresponds to an allocation ratio of 0.3, a heat transfer efficiency coefficient of 0.95, and an actual allocation weight of 0.3 multiplied by 0.95 equaling 0.285; the normalized value for temperature deviation is 1.8 divided by 5, equaling 0.36; a slow temperature increase corresponds to an urgency level of 0.4; the urgency evaluation value for heating is calculated using the formula: In the formula, U is the evaluation value of the urgency of heating, D is the normalized value of the temperature deviation, J is the degree of urgency, and W is the actual assigned weight. Substituting the data, we get... Similarly, the U-values ​​for branch pipe 3 are calculated to be 0.223, for branch pipe 5 to be 0.189, and for branch pipe 7 to be 0.208. The target branch heating priority sequence is obtained by sorting the U-values ​​from largest to smallest as follows: branch pipe 6 is priority 1, branch pipe 3 is priority 2, branch pipe 7 is priority 3, and branch pipe 5 is priority 4.

[0124] Then, according to the power allocation rules, the baseline heating power is allocated as follows: branch pipe 6 is allocated 40% multiplied by 2.10016 kW, which is approximately 0.84 kW, corresponding to an initial heating opening of 40%; branch pipe 3 is allocated 30%, which is approximately 0.63 kW, corresponding to an initial heating opening of 30%; branch pipe 7 is allocated 20%, which is approximately 0.42 kW, corresponding to an initial heating opening of 20%; and branch pipe 5 is allocated 10%, which is approximately 0.21 kW, corresponding to an initial heating opening of 10%.

[0125] Finally, the thermal buffer capacity coefficient was obtained from the thermal saturation distribution spectrum analysis of the packing in branch pipe 6. The dynamic adjustment factor for heating opening is 0.85, calculated using the formula: In the formula, F is the dynamic adjustment factor for heating opening. The thermal buffering capacity coefficient is obtained by substituting the data. The intermediate heating opening is 40% multiplied by 1.07, which equals 42.8%. The condenser auxiliary heating system has sufficient real-time heat supply margin and requires no constraints; therefore, the final heating opening value is 42.8%. Branches 3, 5, and 7 are calculated similarly to achieve final heating openings of 32%, 9.5%, and 21%, respectively. These final heating opening values ​​will be directly used to control the connection opening between the condenser auxiliary heating system and each branch, while also providing a clear basis for subsequent temperature closed-loop monitoring and parameter fine-tuning.

[0126] The aforementioned S105 coordinates the heating needs of multiple branches through global optimization decision-making, and accurately allocates heating resources by combining branch characteristics and system capabilities, thereby achieving coordinated control of heating and cooling, avoiding local temperature being too high or too low, ensuring the overall temperature stability of the tower top, and improving the comprehensiveness and adaptability of temperature control.

[0127] In a practical application, the above-described method for controlling the top temperature of a fluoride distillation column can be applied to, for example... Figure 2In the distillation column overhead temperature control system shown, the method comprises a column overhead condenser 1, a column overhead temperature monitoring device 2, a condenser refrigeration system, a condenser auxiliary heating system 4 and a temperature control device 5, wherein the condenser refrigeration system comprises a condenser pipeline 3.

[0128] For example, the column overhead condenser 1 is installed at the top of the distillation column to meet the demand for large flow distillation and improve the condensation effect of distillation. Inside it, at least two vertical pipes are used to form a parallel branch structure. The distillation column overhead vapor is divided into each branch pipe for condensation and reflux. The material vapor can be divided to improve the condensation effect. The inlet and outlet of each branch pipe are equipped with on-off valves, which can flexibly open different numbers of branch pipes for condensation according to the flow demand of the condensed material. Further, the branch pipe is filled with different sizes of metal balls made of copper, iron, nickel and other materials to increase the heat transfer area and improve the uniformity of heat transfer and temperature control accuracy.

[0129] In another example, the column overhead condenser 1 is installed at the top of the distillation column to meet the demand for large flow distillation and improve the condensation effect of distillation. Inside it, at least two vertical pipes are used to form a parallel branch structure. The distillation column overhead vapor is divided into each branch pipe for condensation and reflux. The material vapor can be divided to improve the condensation effect. The inlet and outlet of each branch pipe are equipped with on-off valves, which can flexibly open different numbers of branch pipes for condensation according to the flow demand of the condensed material. Further, the branch pipe is filled with different sizes of metal balls made of copper, iron, nickel and other materials to increase the heat transfer area and improve the uniformity of heat transfer and temperature control accuracy.

[0130] The temperature control process of the system is as follows: first, the column overhead condenser 1 is pre-cooled to the set temperature by the condenser pipeline 3 in the condenser refrigeration system, then the real-time temperature monitoring is started by the column overhead temperature monitoring device 2, and then the distillation system is started. During the distillation process, the material vapor rises and enters each branch pipe of the column overhead condenser 1 for condensation and reflux. The change of the column overhead temperature is fed back to the temperature control device 5 in real time. The temperature control device 5 outputs adjustment instructions to the condenser refrigeration system according to the feedback signal to accurately adjust the temperature and circulation flow of the refrigerant, and controls the condenser auxiliary heating system 4 to compensate the heat in a targeted manner, so as to stabilize the column overhead temperature within the set range. It should be noted that during this process, the products analyzed as unqualified after condensation will be directed to the tail gas treatment link, and the material vapor that is not completely condensed but qualified will be further condensed through the gas phase outlet and finally collected in the product container.

[0131] Another example, the condenser refrigeration system consists of a condenser pipeline 3 and a cryogenic tank, the condenser pipeline 3 as the core heat exchange structure of the condenser refrigeration system, which adopts the form of winding coil, tightly wound outside each branch pipe of the overhead condenser, and its inside is cooled by the refrigerant provided by the cryogenic tank, the overhead condenser and the internal material vapor of each branch pipe are cooled, and the temperature control device 5 controls the output of the condenser refrigeration system to enter the condenser pipeline 3, and the temperature of the overhead condenser 1 and the internal material vapor of each branch pipe are cooled, and the control precision can reach ±2℃.

[0132] In some embodiments, the condenser auxiliary heating system 4 is an electric heating belt, which is wound outside the overhead condenser, and the heating power is adjusted by the temperature control device 5, which optimizes the temperature of the overhead condenser in time according to the temperature signal, reduces the temperature fluctuation, and further improves the temperature control precision of the overhead condenser 1 to ±0.3℃. The combination of the temperature control device 5 and the condenser auxiliary heating system 4 is the core key of the temperature precise control of this embodiment. The temperature control device 5 can receive the temperature signal transmitted by the overhead temperature monitoring device 2, and adjust the temperature of different branch pipes according to the temperature signal of each branch pipe, and output the control instruction to the condenser refrigeration system and the condenser auxiliary heating system 4, so as to ensure that the overhead temperature is stable in the set range.

[0133] Figure 3 A specific embodiment structure diagram of a tower top temperature control system for a fluorine rectifying tower provided by the present application is shown in Figure 3 The system can include:

[0134] The acquisition module 31 is used to acquire the actual condensation temperature of the overhead of each branch pipe in the overhead condenser in parallel during the rectification process by the overhead temperature monitoring device, and the overhead temperature monitoring device is set in each branch pipe.

[0135] The determination module 32 is used to determine the deviation type of the deviation between the actual condensation temperature and the target condensation temperature required by the fluorine, and the deviation type includes a temperature deviation type for indicating that the actual condensation temperature is higher than the target condensation temperature, and a temperature deviation type for indicating that the actual condensation temperature is lower than the target condensation temperature.

[0136] The prediction module 33 is used to determine that the corresponding branch is the to-be-adjusted branch when the deviation type is the temperature deviation type and the deviation is greater than the first preset deviation threshold, and call the pre-established branch dynamic thermodynamic model to predict the temperature variation trajectory of the to-be-adjusted branch in a future control period based on the fluorine load value and the temperature variation trend in the to-be-adjusted branch.

[0137] The computing module 34 is configured to dynamically calculate a temperature adjustment parameter for temperature adjustment based on the temperature change trajectory, the fluoride load value and the deviation, the temperature adjustment parameter including an adjustment mode and a final adjustment duration, wherein the adjustment mode includes at least one of the following: reducing the temperature of the refrigerant in the condenser pipeline of the external device of the branch to be adjusted and increasing the refrigerant flow.

[0138] The adjusting module 35 is configured to, during the corresponding adjustment according to the adjustment mode and the final adjustment duration, adjust the opening between the condenser auxiliary heating system and the branch to be adjusted based on the fluoride load value and the deviation in the branch when it is determined that the deviation is less than a first preset deviation threshold and greater than a second preset deviation threshold, or the deviation type is a temperature deviation low type.

[0139] The tower top temperature control system for the fluoride rectifying tower according to the embodiments of the present application is used to implement the foregoing tower top temperature control method for the fluoride rectifying tower, and therefore the specific embodiments in the tower top temperature control system for the fluoride rectifying tower can be seen from the foregoing embodiments of the tower top temperature control method for the fluoride rectifying tower, and the specific embodiments can be referred to the descriptions of the corresponding embodiments, which will not be described here again.

[0140] As shown in Figure 4 The present application further provides an electronic device, which comprises a memory 41 configured to store a computer program and a processor 42 configured to execute the computer program to implement the steps of any of the foregoing tower top temperature control methods for the fluoride rectifying tower.

[0141] The present application further provides a computer readable storage medium, which stores a computer program, and the computer program is executed by a processor to implement the steps of any of the foregoing tower top temperature control methods for the fluoride rectifying tower.

[0142] In an exemplary embodiment, the foregoing computer readable storage medium can include, but is not limited to, a U disk, a read-only memory, a random access memory, a mobile hard disk, a magnetic disk or an optical disk and various media that can store computer programs.

[0143] The embodiments of the present application further provide a computer program product, which comprises a computer program, and the computer program is executed by a processor to implement the steps in any of the foregoing tower top temperature control methods for the fluoride rectifying tower.

[0144] Those skilled in the art will further realize that the mere concepts, teachings, and embodiments described herein are merely meant to provide an enabling description of embodiments of the present application and are not intended to limit the scope of the present application. Accordingly, embodiments as described herein contemplate all modifications that come within the scope of the present application as recited by the claims set forth below and any equivalents thereto, with the scope of the present application being measured by the broadest interpretation of those claims set forth below.

[0145] The above provides a kind of for the tower top temperature control method, system, equipment and storage medium of fluoride rectifying column provided in the present application in detail.The principle and implementation mode of the present application are described in the specific examples in this paper, the above example is only used to help understanding the method of the present application and its core idea.It should be pointed out that, for the ordinary skilled in the art, without departing from the principle of the present application, the present application can be improved and modified, these improvements and modifications also fall within the scope of the present application.

Claims

1. A method for controlling the top temperature of a fluoride distillation column, characterized in that, include: During the distillation process, the actual condensation temperature at the top of the column is collected by the parallel branch pipes inside the top condenser of the column using a column top temperature monitoring device, which is installed one by one inside each branch pipe. Determine the type of deviation between the actual condensation temperature and the target condensation temperature required for the fluoride, including a temperature-to-high type indicating that the actual condensation temperature is higher than the target condensation temperature, and a temperature-to-low type indicating that the actual condensation temperature is lower than the target condensation temperature. When the deviation type is high temperature and the deviation is greater than the first preset deviation threshold, the corresponding branch is determined as the branch to be adjusted, and the pre-established dynamic thermodynamic model of the branch is called. Based on the fluoride load value and temperature change trend in the branch to be adjusted, the temperature change trajectory in the branch to be adjusted in the next control cycle is predicted. Based on the temperature change trajectory, the fluoride load value, and the deviation, the temperature regulation parameters for temperature regulation are dynamically calculated. The temperature regulation parameters include the regulation method and the final regulation duration. The regulation method includes at least one of the following: lowering the refrigerant temperature in the condenser pipe of the branch to be adjusted and increasing the refrigerant flow rate. During the adjustment process according to the adjustment method and the final adjustment duration, when the deviation is determined to be less than the first preset deviation threshold and greater than the second preset deviation threshold, or when the deviation type is low temperature, the opening between the condenser auxiliary heating system and the branch to be adjusted is adjusted using global optimization decision based on the fluoride load value and deviation in the branch.

2. The method for controlling the top temperature of a fluoride distillation column according to claim 1, characterized in that, The process of calling a pre-established branch dynamic thermodynamic model, based on the fluoride load value and temperature change trend within the branch to be adjusted, predicts the temperature change trajectory within the branch to be adjusted over a future control cycle, including: The actual condensation temperature of the same branch to be adjusted and the condensation temperature data at multiple historical moments are integrated in chronological order to obtain an ordered temperature sequence. Based on the ordered temperature sequence, the fluctuation pattern of condensation temperature data at different times is analyzed to obtain a dynamic feature vector that reflects the temperature change trend. The fluoride flow rate data of the branch to be adjusted at the current time is quantified and converted to obtain the fluoride load value. The dynamic feature vector and the fluoride load value are input into the pre-established branch dynamic thermodynamic model. Combined with the phase change characteristics of fluoride in the distillation and condensation process, the data is adapted through the branch dynamic thermodynamic model to obtain the thermal dynamic response factor for characterizing the thermal inertia of the branch and the phase change latent heat influence factor for characterizing the effect of phase change latent heat on temperature change. By combining the correlation between the thermal dynamic response factor and the latent heat of phase change influence factor, trajectory extrapolation is performed to obtain the temperature change trajectory of the branch to be adjusted within a future control cycle.

3. The method for controlling the top temperature of a fluoride distillation column according to claim 2, characterized in that, The dynamic feature vector and the fluoride load value are input together into a pre-established branch dynamic thermodynamic model. Combining the phase change characteristics of fluoride during distillation and condensation, data adaptation processing is performed through the branch dynamic thermodynamic model to obtain a thermodynamic response factor characterizing the branch's thermal inertia and a phase change latent heat influence factor characterizing the effect of latent heat of phase change on temperature changes, including: Based on the temperature change rate information in the dynamic feature vector, the fluctuation law of the branch temperature change rate is analyzed to obtain the acceleration feature. The acceleration feature is correlated with the fluoride load value to obtain the thermal inertia weight that reflects the degree of thermal response hysteresis of the system. By using the temperature trend processing rules in the branch dynamic thermodynamic model, the thermal inertia weight and the dynamic feature vector are processed collaboratively to obtain the thermal dynamic response factor. Based on the similarity between the actual condensation temperature and the preset fluoride phase transition temperature, the urgency of the phase transition is quantified to obtain the phase transition proximity coefficient. The phase transition proximity coefficient is then correlated and fused with the fluoride load value to obtain the latent heat influence factor of the phase transition.

4. The method for controlling the top temperature of a fluoride distillation column according to claim 1, characterized in that, The method of adjusting the opening between the condenser auxiliary heating system and the branch to be adjusted based on the fluoride load value and deviation in the branch pipe, using global optimization decision-making, includes: Based on the preset rules for determining the intensity of compensation demand in the auxiliary heating coordination mode, the deviation during the adjustment process and the fluoride load value in the branch pipe are correlated to obtain the intensity of heat compensation demand. Based on the synergistic heating rules in the auxiliary heating coordination mode, and combined with the phase change heat characteristics of fluorides in the distillation and condensation process, the intensity of the heat compensation demand is matched according to rules to obtain the reference heating power of the condenser auxiliary heating system. Establish a heat transfer association rule between the branch to be adjusted and the condenser auxiliary heating system. Based on the heat transfer association rule and the actual condensing temperature of each branch to be adjusted, adopt a global optimization decision to divide different heating urgency levels and obtain the target branch heating priority sequence. Based on the target branch heating priority sequence and the power allocation rules in the auxiliary heating coordination mode, the reference heating power is dynamically allocated to obtain the initial heating opening degree corresponding to each branch to be adjusted. Based on the thermal saturation state of the metal ball packing inside the branch to be adjusted, the initial heating opening is optimized and adjusted to obtain the final heating opening value, so as to complete the coordinated control of the opening between the condenser auxiliary heating system and the branch to be adjusted.

5. The method for controlling the top temperature of a fluoride distillation column according to claim 4, characterized in that, The process involves establishing heat transfer correlation rules between the branch to be adjusted and the condenser auxiliary heating system. Based on these rules and the actual condensing temperature of each branch, a global optimization decision is adopted to classify different heating urgency levels, resulting in a target branch heating priority sequence, including: Using a pre-defined spatial and thermal characteristic coupling analysis method, the spatial distribution location, heat transfer characteristics, and heat transfer path differences of each branch to be adjusted are comprehensively analyzed to obtain the correspondence between spatial location, heat transfer efficiency, and heat distribution ratio. The correspondence is then processed into rules to obtain the heat transfer association rules between the branch to be adjusted and the condenser auxiliary heating system. Calculate the difference between the actual condensing temperature and the target condensing temperature of each branch to be adjusted during the adjustment process to obtain the degree of temperature deviation, and analyze the trend of the actual condensing temperature change to obtain the urgency corresponding to the temperature change trend. Combining the distillation characteristics of fluorides and the heat transfer correlation rules, a global optimization decision is used to weight and integrate the temperature deviation and the urgency to obtain the heating urgency evaluation value of each branch to be adjusted. All the heating urgency evaluation values ​​are numerically sorted to obtain a preliminary branch heating priority sequence. By combining the heat capacity saturation and thermal response characteristics of the metal ball packing inside each branch to be adjusted, the heating priority sequence of the preliminary branch is dynamically fine-tuned to obtain the heating priority sequence of the target branch.

6. The method for controlling the top temperature of a fluoride distillation column according to claim 4, characterized in that, The initial heating opening is optimized and adjusted based on the thermal saturation state of the metal ball packing inside the branch to be adjusted, to obtain the final heating opening value, including: A distributed temperature sensing network is installed in the metal ball packing inside the branch to be adjusted to collect temperature data at different depths of the packing in real time. Based on the temperature data, combined with the upper limit of heat absorption of the metal ball packing and the difference in packing density, the temperature distribution pattern at different depths is processed into a graph to obtain the heat saturation distribution graph of the metal ball packing. Based on the aforementioned thermal saturation distribution map, the degree of attenuation of the overall thermal buffering capacity of the metal sphere is analyzed; By combining the deviation data and the rate of change of the deviation of the branch to be adjusted, the attenuation degree is quantified and converted to obtain the thermal buffer capacity coefficient. By combining the fluoride load value in the branch pipe and the dynamic response characteristics of the condenser auxiliary heating system, the heat buffer capacity coefficient and the initial heating opening are dynamically adapted to obtain the heating opening dynamic adjustment factor. Based on the aforementioned dynamic adjustment factor for heating opening, and combined with the phase change characteristics of fluorides during distillation and condensation, the initial heating opening is corrected in real time to obtain an intermediate heating opening value. By combining the real-time heat supply margin of the condenser auxiliary heating system, the intermediate heating opening value is subjected to range constraint processing to obtain the final heating opening value.

7. The method for controlling the top temperature of a fluoride distillation column according to claim 1, characterized in that, Based on the temperature change trajectory, the fluoride load value, and the deviation, the temperature regulation parameters for temperature control are dynamically calculated. These parameters include the regulation method and the final regulation duration. The temperature change trajectory is characterized by trajectory analysis to obtain the temperature peak deviation. The temperature peak deviation and the deviation are then weighted and fused to obtain the comprehensive regulation intensity. Based on the comprehensive regulation intensity and the fluoride load value, the corresponding regulation method and basic regulation duration are queried from the pre-established fluoride regulation strategy mapping table; Based on the thermal buffering characteristics of the metal ball packing inside the branch to be adjusted, the basic adjustment time is adaptively modified to extend the adjustment time when the thermal buffering effect is significant and shorten the adjustment time when the thermal buffering effect is weak, so as to obtain the final adjustment time. The adjustment method and the final adjustment duration are combined according to a preset parameter integration rule to form temperature adjustment parameters.

8. A top temperature control system for a fluoride distillation column, characterized in that, include: The acquisition module is used to acquire the actual condensation temperature of the top of the column in each branch pipe connected in parallel inside the top condenser during the distillation process through the top temperature monitoring device. The top temperature monitoring device is installed in each branch pipe. The determination module is used to determine the type of deviation between the actual condensation temperature and the target condensation temperature required for the fluoride. The deviation types include a temperature-to-high type, which indicates that the actual condensation temperature is higher than the target condensation temperature, and a temperature-to-low type, which indicates that the actual condensation temperature is lower than the target condensation temperature. The prediction module is used to determine the corresponding branch as the branch to be adjusted when the deviation type is high temperature and the deviation is greater than a first preset deviation threshold, and to call the pre-established dynamic thermodynamic model of the branch to be adjusted to predict the temperature change trajectory of the branch to be adjusted in the next control cycle based on the fluoride load value and temperature change trend in the branch to be adjusted. The calculation module is used to dynamically calculate the temperature adjustment parameters for temperature regulation based on the temperature change trajectory, the fluoride load value and the deviation. The temperature adjustment parameters include the adjustment method and the final adjustment duration. The adjustment method includes at least one of the following: lowering the refrigerant temperature in the condenser pipe of the branch to be adjusted and increasing the refrigerant flow rate. The adjustment module is used to adjust the opening between the condenser auxiliary heating system and the branch to be adjusted based on the fluoride load value and deviation in the branch pipe when the deviation is determined to be less than the first preset deviation threshold and greater than the second preset deviation threshold, or when the deviation type is low temperature, during the corresponding adjustment process according to the adjustment method and the final adjustment duration.

9. An electronic device, characterized in that, include: Memory, used to store computer programs; A processor, configured to execute the computer program to implement the steps of the method for controlling the top temperature of a fluoride distillation column as described in any one of claims 1 to 7.

10. A computer-readable storage medium, characterized in that, The computer-readable storage medium stores a computer program that, when executed by a processor, enables the implementation of the method for controlling the top temperature of a fluoride distillation column as described in any one of claims 1 to 7.

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