Temperature adaptive regulation strategy and device in high-boiling-point solvent waste liquid recovery process

Abstract

This application provides a temperature adaptive regulation strategy and apparatus for a high-boiling-point solvent waste recovery process, comprising: when the absolute value of the temperature difference between a single gas-liquid separation tower and a first preset temperature is less than a preset difference, executing a first temperature control strategy for the single tower based on a vacuum module, a steam valve, and a cold water valve; when the temperature in a single gas-liquid separation tower reaches a second preset temperature, executing a second temperature control strategy for the single tower based on a vacuum module, a steam valve, and a cold water valve; and executing a coordinated temperature control strategy for the remaining multiple gas-liquid separation towers according to the first or second temperature control strategy, thereby achieving coordinated temperature control of multiple gas-liquid separation towers during the high-boiling-point solvent waste recovery process. This application is beneficial for improving the safety and recovery efficiency of high-boiling-point solvent waste recovery.

Description

Technical Field

[0001] This application relates to the field of high-boiling-point solvent waste liquid recovery technology, and in particular to a temperature adaptive regulation strategy and device in the high-boiling-point solvent waste liquid recovery process. Background Technology

[0002] In the field of high-boiling-point solvent waste recovery, distillation is the core technology for achieving solvent recycling. The recovery of high-boiling-point solvent waste relies on multi-stage distillation to separate impurities. However, pressure and temperature are strongly coupled within the gas-liquid separation tower—reducing pressure can significantly lower the boiling point of high-boiling-point solvents, thereby reducing the risk of thermal decomposition at high temperatures. But in actual operation, temperature fluctuations within the tower are unavoidable. When the temperature rises abnormally, high-boiling-point solvents such as DMF (N,N-dimethylformamide) will rapidly thermally decompose to produce large amounts of dimethylamine. If the dimethylamine concentration in the gas phase reaches the explosion threshold, it may cause a deflagration accident, seriously threatening equipment safety and production continuity.

[0003] Traditional high-boiling-point solvent waste recovery systems generally adopt a fixed pressure-temperature control mode, that is, the vacuum degree, heating amount and other parameters of each tower are preset according to the initial process conditions, lacking a dynamic adjustment mechanism. Moreover, when the temperature of a certain tower is abnormal, there is no linkage adjustment mechanism for pressure and flow, which can easily lead to the spread of faults. Summary of the Invention

[0004] This application provides a temperature adaptive regulation strategy and device for a high-boiling-point solvent waste liquid recovery process. For a single tower with abnormal temperature, different control strategies are executed based on the specific temperature value. At the same time, a coordinated control strategy is executed for the other multiple towers. When the pressure of the upstream tower is reduced, the pressure of the downstream tower is adjusted proportionally. When the downstream tower is abnormal, the load input of the upstream tower is reduced, so as to realize the linkage control of multiple towers under abnormal temperature conditions.

[0005] In a first aspect, this application provides a temperature adaptive adjustment strategy for a high-boiling-point solvent waste liquid recovery process, applied to a high-boiling-point solvent waste liquid recovery system. The system includes a vacuum module, a distillation module, and a control module. The distillation module includes multiple gas-liquid separation towers connected in sequence. The bottom of each gas-liquid separation tower is connected to a steam valve, and the top is connected to a cold water valve. The steam valve controls the heating of the waste liquid at the bottom of the tower with steam. The waste liquid contains the high-boiling-point solvent. The cold water valve controls the condensation of the gas phase at the top of the tower with cold water. The vacuum module is connected to each of the multiple gas-liquid separation towers. The control module is connected to the vacuum module, the multiple steam valves, and the multiple cold water valves.

[0006] The vacuum module is used to regulate the vacuum level in the multiple gas-liquid separation towers in order to suppress the thermal decomposition rate by lowering the boiling point of the waste liquid in the towers.

[0007] The distillation module is used to perform multi-stage distillation treatment on the waste liquid in the multiple gas-liquid separation towers to obtain high-purity solvent.

[0008] The control module is configured to, when the absolute value of the temperature difference between the individual gas-liquid separator and the first preset temperature is detected to be less than a preset difference, execute a first temperature control strategy for the individual gas-liquid separator based on the vacuum module, the steam valve corresponding to the individual gas-liquid separator, and the cold water valve; and...

[0009] When the temperature inside the single gas-liquid separator is detected to reach the second preset temperature, a second temperature control strategy is executed for the single gas-liquid separator based on the vacuum module, the steam valve and the cold water valve corresponding to the single gas-liquid separator, and the first preset temperature is lower than the second preset temperature.

[0010] A coordinated temperature control strategy is implemented for the remaining multiple gas-liquid separation towers according to the first temperature control strategy or the second temperature control strategy, so as to achieve linkage control of the temperature inside the multiple gas-liquid separation towers during the high-boiling-point solvent waste liquid recovery process.

[0011] Secondly, embodiments of this application provide a temperature adaptive regulation device for a high-boiling-point solvent waste liquid recovery process, applied to a high-boiling-point solvent waste liquid recovery system. The system includes a vacuum module, a distillation module, and a control module. The distillation module includes multiple gas-liquid separation towers connected in sequence. The bottom of each gas-liquid separation tower is connected to a steam valve, and the top is connected to a cold water valve. The steam valve is used to control steam to heat the waste liquid at the bottom of the tower. The waste liquid contains the high-boiling-point solvent. The cold water valve is used to control cold water to condense the gas phase at the top of the tower. The vacuum module is connected to the multiple gas-liquid separation towers respectively. The control module is connected to the vacuum module, the multiple steam valves, and the multiple cold water valves respectively. The device includes:

[0012] The first processing unit is configured to, when the absolute value of the difference between the temperature inside the single gas-liquid separation tower and the first preset temperature is detected to be less than a preset difference, execute a first temperature control strategy for the single gas-liquid separation tower based on the vacuum module, the steam valve corresponding to the single gas-liquid separation tower, and the cold water valve; and, when the temperature inside the single gas-liquid separation tower is detected to reach a second preset temperature, execute a second temperature control strategy for the single gas-liquid separation tower based on the vacuum module, the steam valve corresponding to the single gas-liquid separation tower, and the cold water valve, wherein the first preset temperature is lower than the second preset temperature;

[0013] The second processing unit is used to execute a coordinated temperature control strategy on the remaining multiple gas-liquid separation towers according to the first temperature control strategy or the second temperature control strategy, so as to realize the linkage control of the temperature inside the multiple gas-liquid separation towers during the high-boiling-point solvent waste liquid recovery process.

[0014] Thirdly, embodiments of this application provide an electronic device including a processor, a memory, and one or more programs, the one or more programs being stored in the memory and configured to be executed by the processor, the programs including instructions for performing the steps in the first aspect of embodiments of this application.

[0015] Fourthly, embodiments of this application provide a computer-readable storage medium having a computer program / instructions stored thereon, which is executed by a processor to implement the steps of the strategy described in the first aspect above.

[0016] As can be seen from the embodiments of this application, when the absolute value of the temperature difference between a single gas-liquid separation tower and a first preset temperature is detected to be less than a preset difference, a first temperature control strategy is executed for the single gas-liquid separation tower based on the vacuum module, the steam valve corresponding to the single gas-liquid separation tower, and the cold water valve; and when the temperature inside a single gas-liquid separation tower is detected to reach a second preset temperature, a second temperature control strategy is executed for the single gas-liquid separation tower based on the vacuum module, the steam valve corresponding to the single gas-liquid separation tower, and the cold water valve; a coordinated temperature control strategy is executed for the remaining multiple gas-liquid separation towers according to the first or second temperature control strategy, so as to achieve linkage control of the temperature inside multiple gas-liquid separation towers during the high-boiling-point solvent waste liquid recovery process. Thus, compared with the existing single-tower fixed pressure-temperature temperature control scheme, this application suppresses the risk of thermal decomposition of high-boiling-point solvents through single-tower temperature-pressure dual-stage linkage adjustment and multi-tower coordinated control, which is beneficial to improving the safety and efficiency of high-boiling-point solvent waste liquid recovery. Attached Figure Description

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

[0018] Figure 1 This is a schematic diagram of a high-boiling-point solvent waste liquid recovery system provided in an embodiment of this application;

[0019] Figure 2 This is a schematic diagram of the system architecture of a high-boiling-point solvent waste liquid recovery system provided in an embodiment of this application;

[0020] Figure 3 This is a schematic diagram of the structure of a control module provided in an embodiment of this application;

[0021] Figure 4 This is a schematic diagram of the structure of a distillation tower provided in an embodiment of this application;

[0022] Figure 5 This is a process flow diagram of high-boiling-point solvent waste liquid recovery provided in an embodiment of this application;

[0023] Figure 6 This is a schematic diagram of a temperature adaptive adjustment strategy in a high-boiling-point solvent waste liquid recovery process provided in an embodiment of this application;

[0024] Figure 7 This is a flowchart illustrating a collaborative temperature control strategy provided in an embodiment of this application;

[0025] Figure 8 This is a schematic diagram of the functional modules of a temperature adaptive regulation device in a high-boiling-point solvent waste liquid recovery process provided in this application embodiment;

[0026] Figure 9 This is a structural block diagram of an electronic device provided in an embodiment of this application. Detailed Implementation

[0027] To enable those skilled in the art to better understand the present application, the technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present application, and not all embodiments. Based on the embodiments in the present application, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the scope of protection of the present application.

[0028] The terms "first," "second," etc., in the specification, claims, and accompanying drawings of this application are used to distinguish different objects, not to describe a specific order. Furthermore, the terms "comprising" and "having," and any variations thereof, are intended to cover non-exclusive inclusion. For example, a process, method, system, product, or apparatus that includes a series of steps or units is not limited to the listed steps or units, but may optionally include steps or units not listed, or may optionally include other steps or units inherent to these processes, methods, products, or apparatuses.

[0029] In this document, the term "embodiment" means that a particular feature, structure, or characteristic described in connection with an embodiment may be included in at least one embodiment of this application. The appearance of this phrase in various places throughout the specification does not necessarily refer to the same embodiment, nor is it a separate or alternative embodiment mutually exclusive with other embodiments. It will be explicitly and implicitly understood by those skilled in the art that the embodiments described herein can be combined with other embodiments.

[0030] In the embodiments of this application, "and / or" describes the relationship between associated objects, indicating that three relationships can exist. For example, A and / or B can represent the following three situations: A exists alone; A and B exist simultaneously; B exists alone. Among them, A and B can be singular or plural.

[0031] In this embodiment, the symbol " / " can indicate that the preceding and following objects are in an "or" relationship. Alternatively, the symbol " / " can also represent a division sign, i.e., performing a division operation. For example, A / B can mean A divided by B.

[0032] In the embodiments of this application, "at least one item" or its similar expression refers to any combination of these items, including any combination of a single item or a plurality of items. "One or more" means one or more, while "multiple" means two or more. For example, "at least one item" of a, b, or c can represent the following seven cases: a, b, c; a and b; a and c; b and c; a, b, and c. Each of a, b, and c can be an element or a set containing one or more elements.

[0033] In the embodiments of this application, "equal to" can be used with "greater than" and is applicable to technical solutions used when "greater than" is used; it can also be used with "less than" and is applicable to technical solutions used when "less than" is used. When "equal to" is used with "greater than", it is not used with "less than"; when "equal to" is used with "less than", it is not used with "greater than".

[0034] Traditional high-boiling-point solvent waste recovery systems generally adopt a fixed pressure-temperature control mode, that is, the vacuum degree, heating amount and other parameters of each tower are preset according to the initial process conditions, lacking a dynamic adjustment mechanism. Moreover, when the temperature of a certain tower is abnormal, there is no linkage adjustment mechanism for pressure and flow, which can easily lead to the spread of faults.

[0035] To address the aforementioned issues, this application provides a temperature adaptive adjustment strategy and apparatus for a high-boiling-point solvent waste liquid recovery process. The embodiments of this application will be described in detail below with reference to the accompanying drawings.

[0036] Please see Figure 1 Figure 1 is a schematic diagram of a high-boiling-point solvent waste liquid recovery system provided in an embodiment of this application. As shown in Figure 1, Figure 1 The medium-to-high boiling point solvent waste liquid recovery system includes a vacuum module 110, a distillation module 120, and a control module 130. The distillation module 120 includes multiple gas-liquid separation towers connected in sequence. The bottom of each gas-liquid separation tower is connected to a steam valve, and the top is connected to a cold water valve. The steam valve controls the heating of the waste liquid at the bottom of the tower with steam, and the cold water valve controls the condensation of the gas phase at the top of the tower with cold water. The vacuum module 110 is connected to the multiple gas-liquid separation towers, and the control module 130 is connected to the vacuum module 110, the multiple steam valves, and the multiple cold water valves.

[0037] The vacuum module 110 is used to regulate the vacuum level in multiple gas-liquid separation towers to suppress the thermal decomposition rate by lowering the boiling point of the waste liquid in the towers; the distillation module 120 is used to perform multi-stage distillation on the waste liquid in the towers through multiple gas-liquid separation towers to obtain high-purity solvent; the control module 130 is used to execute a first temperature control strategy for a single gas-liquid separation tower based on the vacuum module, the steam valve and the cold water valve corresponding to the single gas-liquid separation tower when the absolute value of the temperature difference between the single gas-liquid separation tower and the first preset temperature is less than the preset difference; and to execute a second temperature control strategy for a single gas-liquid separation tower based on the vacuum module, the steam valve and the cold water valve corresponding to the single gas-liquid separation tower when the temperature in the single gas-liquid separation tower reaches the second preset temperature, wherein the first preset temperature is lower than the second preset temperature; and to execute a coordinated temperature control strategy for the remaining multiple gas-liquid separation towers according to the first temperature control strategy or the second temperature control strategy to achieve linkage control of the temperature in multiple gas-liquid separation towers during the high-boiling-point solvent waste liquid recovery process.

[0038] Specifically, please refer to Figure 2 , Figure 2 This is a schematic diagram of the system architecture of a high-boiling-point solvent waste liquid recovery system provided in an embodiment of this application, as shown below. Figure 2 As shown, the high-boiling-point solvent waste liquid recovery system includes a concentration module 210, an evaporation module 220, a vacuum module 110, a distillation module 120, and a control module 130. The distillation module 120 includes a stripping column, a rectification column, and a purification column. Each column works collaboratively through reboilers (first reboiler / second reboiler / third reboiler), condensers (first condenser / second condenser / third condenser), steam valves, cold water valves, and reflux valves.

[0039] The concentration module 210 is used to concentrate the original waste liquid to obtain a first waste liquid with a concentration greater than a first preset concentration, and to transfer the first waste liquid to the evaporation module 220; the evaporation module 220 is used to receive the first waste liquid, heat and evaporate the first waste liquid to obtain a second waste liquid with a concentration greater than a second preset concentration; and to transfer the second waste liquid to the bottom of the distillation column for multi-stage distillation.

[0040] Specifically, the multi-stage distillation process includes: performing a first-stage distillation on the waste liquid in the bottom of the stripping column through a first reboiler and a first condenser corresponding to the stripping column to obtain a first target liquid phase, and transferring the first target liquid phase to the bottom of the distillation column; performing a second-stage distillation on the first target liquid phase in the bottom of the distillation column through a second reboiler and a second condenser corresponding to the distillation column to obtain a second target liquid phase, and transferring the second target liquid phase to the bottom of the purification column; and performing a third-stage distillation on the second target liquid phase in the bottom of the purification column through a third reboiler and a third condenser corresponding to the purification column to obtain a high-purity solvent.

[0041] For further details on the specific functions of the control module 130, please refer to [link / reference needed]. Figure 3 , Figure 3 This is a schematic diagram of the structure of a control module provided in an embodiment of this application, such as... Figure 3 As shown, the control module 130 includes a detection unit 310 and a processing unit 320.

[0042] The detection unit 310 is responsible for collecting various key data in the high-boiling-point solvent waste recovery system in real time, mainly including temperature and pressure information in each gas-liquid separation tower, as well as parameters such as heating steam flow rate in the reboiler and cooling water flow rate in the condenser. Through sensors (such as temperature sensors, pressure sensors, and flow sensors) distributed at various key locations in the system, these physical quantities are converted into electrical or digital signals, providing a data foundation for subsequent analysis and decision-making.

[0043] The processing unit 320 receives data from the detection unit 310 and analyzes, processes, and judges the data using preset algorithms and logical rules. On one hand, it compares the collected data with preset standard parameters to determine whether the system is operating normally. On the other hand, when abnormal data is detected, the processing unit 320 quickly generates corresponding control commands based on a predetermined control strategy. For example, when the temperature of a distillation column reaches a first preset temperature, the processing unit calculates the parameter values ​​that need to be adjusted (such as the vacuum level to be increased in the vacuum module, the opening degree of the steam valve to be reduced, and the flow rate of the cold water valve to be increased), and sends these commands to the relevant actuators in the vacuum module and distillation module.

[0044] As can be seen, in this embodiment, the vacuum module controls the pressure, the distillation module achieves separation, and the control module schedules the high-boiling-point solvent waste liquid recovery system. Through the collaboration between the modules, the temperature, pressure and other parameters during the high-boiling-point solvent waste liquid recovery process can be precisely controlled, reducing the risk of thermal decomposition and improving the safety and efficiency of the recovery.

[0045] The following is combined with Figure 4 The structure of a distillation tower provided in the embodiments of this application will be described. Figure 4 This is a schematic diagram of a distillation column provided in an embodiment of this application. The distillation column 410 is the core equipment for rectification. Waste liquid is fed from the middle of the column; the bottom of the column is used to store the liquid at the bottom of the column, which is the source of the circulating liquid in the first reboiler 420. Part of the liquid in the bottom of the column is heated and vaporized in the first reboiler 420 and returned to the column, while the other part can be discharged as heavy components.

[0046] The first reboiler 420 is used to receive waste liquid from the bottom of the column through a liquid phase pipeline; and the first reboiler 420 is connected to a steam pipeline through a first steam valve 421 to receive hot steam, and the waste liquid in the first reboiler 420 is heated by the hot steam to obtain a gas phase; and the first reboiler 420 is used to transfer the gas phase back to the stripping column 410 through a gas phase pipeline.

[0047] The first condenser 430 is used to receive the gas phase located at the top of the tower; and the first condenser 430 is connected to the cold water pipeline through the first cold water valve 431 to access cold water, and the gas phase is condensed into the target liquid phase by the cold water; and the first condenser 430 is used to transfer the target liquid phase to the first reflux tank 440.

[0048] The first reflux tank 440 is used to receive the target liquid phase from the first condenser 430; and the first reflux tank 440 is connected to the reflux pipeline through the first reflux valve 441 to control the reflux flow rate of the target liquid phase back into the gas-liquid separator; and the first reflux tank 440 is used to transfer the target liquid phase that does not participate in the reflux to the next gas-liquid separator through the pipeline.

[0049] The operating principle of a single gas-liquid separation tower is as follows: high-boiling-point solvent waste liquid is fed into the middle of the tower and enters the bottom. The liquid in the bottom is heated and vaporized in a reboiler, generating a gas phase that rises to the top of the tower. The liquid phase remains in the bottom or is discharged. The vapor phase at the top is condensed in a condenser, generating a liquid phase which is then transferred to a reflux tank. The liquid phase is partially refluxed and partially discharged through the reflux tank, thus achieving gas-liquid separation and purification of the high-boiling-point solvent waste liquid. This structure ensures the efficient and stable operation of the gas-liquid separation tower, meeting the requirements for the recovery and distillation of high-boiling-point solvent waste liquid.

[0050] Furthermore, based on the structural analysis of a single gas-liquid separation tower, the process flow of the entire high-boiling-point solvent waste recovery system is described in the following reference: Figure 5 , Figure 5 This is a process flow diagram of high-boiling-point solvent waste liquid recovery provided in an embodiment of this application, as shown below. Figure 5 As shown, the specific structure and operating principle of the stripping column 410 are described in the above embodiment. The high-boiling-point solvent waste liquid recovery system also includes a distillation column 510 and a purification column 550, the structures of which are similar to those of the stripping column 410.

[0051] As can be seen, the process flow for high-boiling-point solvent waste liquid recovery is as follows: Waste liquid containing high-boiling-point solvents is fed into the middle of the stripping column 410. The liquid in the column bottom is transferred to the first reboiler 420 through a liquid phase pipeline. The first reboiler 420 is heated by hot steam under the control of the first steam valve 421. The resulting vapor phase returns to the stripping column 410 and rises to the top of the column. The vapor phase at the top of the column enters the first condenser 430, and after being condensed by cold water through the first cold water valve 431, it enters the first reflux tank 440. Part of the liquid phase in the first reflux tank 440 is refluxed back to the stripping column 410 through the first reflux valve 441, and the other part is discharged into the rectification column 510; and…

[0052] The liquid in the bottom of distillation column 510 is transferred to the second reboiler 520 via a liquid phase pipeline. The second reboiler 520 receives hot steam through a second steam valve 521 to heat the internal liquid phase, generating a vapor phase. This vapor phase returns to the distillation column 510 and rises to the top. The vapor phase at the top passes through the second condenser 530, where cold water is introduced through a second cold water valve 531 for condensation, and then enters the second reflux tank 540. A portion of the liquid phase in the second reflux tank 540 is returned to the distillation column 510 through the second reflux valve 541, while the remaining portion is discharged into the purification column 550.

[0053] The liquid in the bottom of the refining column 550 is transferred to the third reboiler 560 through the liquid phase pipeline. The third reboiler 560 is connected to hot steam through the third steam valve 561 to heat the internal liquid phase and generate a gas phase. The gas phase returns to the refining column 550 and rises to the top of the column. The gas phase at the top of the column passes through the third condenser 570 and is condensed by cold water through the third cold water valve 571 before entering the third reflux tank 580. Part of the liquid phase in the third reflux tank 580 is refluxed through the third reflux valve 581, and the other part is used as the final discharge to obtain a high-purity solvent after the high-boiling-point solvent in the waste liquid is purified by distillation.

[0054] The following is combined with Figure 6 This application describes a temperature adaptive adjustment strategy in a high-boiling-point solvent waste liquid recovery process. Figure 6 This is a schematic flowchart illustrating a temperature adaptive adjustment strategy in a high-boiling-point solvent waste liquid recovery process provided in this application embodiment, specifically including the following steps:

[0055] Step S610: A temperature rise was detected inside a single gas-liquid separation tower.

[0056] The temperature inside the tower is collected in real time by temperature sensors installed inside the gas-liquid separation tower (such as stripping tower, rectification tower, and refining tower). Once the sensor detects that the temperature value has increased compared to the normal operating range, it triggers the subsequent control logic, providing a basis for the system to respond to temperature anomalies in a timely manner.

[0057] Understandably, temperature is a critical parameter in the distillation process for recovering high-boiling-point solvent waste. Excessively high temperatures can cause thermal decomposition of high-boiling-point solvents, leading to safety risks and product quality issues. Timely detection of temperature rise signals allows the system to react in the early stages of anomalies, preventing further temperature runaway and ensuring the safety and stability of the distillation process.

[0058] Step S620: When the absolute value of the temperature difference between a single gas-liquid separation tower and a first preset temperature is less than a preset difference, the first temperature control strategy is executed for the single gas-liquid separation tower based on the vacuum module, the steam valve and the cold water valve corresponding to the single gas-liquid separation tower.

[0059] Understandably, when the actual temperature approaches the first preset temperature, and the absolute value of the difference is less than the preset difference, it indicates that the temperature inside the tower has begun to deviate from the normal range and enters a warning state, but has not yet reached an emergency level. For example, if the first preset temperature is 80℃ and the preset difference is 5℃, the trigger condition is met when the temperature inside the tower is between 75 and 80℃.

[0060] In one possible embodiment, the first temperature control strategy is to increase the vacuum level in the individual gas-liquid separation tower by using the vacuum module to reduce the gas pressure inside the tower; and simultaneously reduce the opening of the steam valve corresponding to the individual gas-liquid separation tower, so that the amount of hot steam delivered decreases by a first preset value, thereby reducing the heating load in the reboiler; and simultaneously increase the opening of the cold water valve corresponding to the individual gas-liquid separation tower, so that the amount of cold water flow increases by a second preset value, thereby accelerating the condensation of the gas phase at the top of the tower.

[0061] This process involves increasing the vacuum level within a single gas-liquid separation tower using a vacuum module, thereby reducing the gas pressure inside the tower. Based on the relationship between boiling point and pressure, the boiling point of high-boiling-point solvents decreases as pressure decreases. For example, DMF has a boiling point of approximately 153°C at atmospheric pressure; as the vacuum level increases and the pressure decreases, its boiling point can drop significantly. Furthermore, by lowering the boiling point of DMF, it becomes less prone to thermal decomposition at the same temperature, reducing the generation of decomposition products such as dimethylamine, lowering safety risks such as explosions, and also facilitating the gas-liquid separation process.

[0062] Specifically, by reducing the opening of the steam valve, the amount of hot steam entering the reboiler is reduced by a first preset value (e.g., 10%). The reduced amount of hot steam lowers the heating power of the reboiler on the waste liquid in the column, preventing further temperature increases within the column.

[0063] Specifically, by increasing the opening of the cold water valve, the flow rate of cold water entering the condenser is increased by a second preset value (e.g., 20%). This results in more cold water flowing through the condenser, enhancing the cooling effect on the gas phase at the top of the column, helping to maintain the gas-liquid balance within the column, and further stabilizing the distillation process.

[0064] As can be seen, in this embodiment, when the absolute value of the difference between the temperature inside the tower and the first preset temperature is less than the preset difference, the tower is in an early warning state. Temperature control strategies are implemented from three aspects: reducing the boiling point, reducing the heat source, and enhancing cooling. This effectively controls the temperature inside the gas-liquid separation tower and ensures the safe and stable operation of the high-boiling-point solvent waste liquid recovery process.

[0065] Step S630: When the temperature inside a single gas-liquid separation tower is detected to reach the second preset temperature, a second temperature control strategy is executed for the single gas-liquid separation tower based on the vacuum module, the steam valve and the cold water valve corresponding to the single gas-liquid separation tower.

[0066] The first preset temperature is lower than the second preset temperature.

[0067] Understandably, when the temperature inside a single gas-liquid separation tower reaches the second preset temperature, the second temperature control strategy is triggered. This indicates that the temperature inside the tower has reached a dangerous level, significantly increasing the risk of thermal decomposition of the high-boiling-point solvent waste liquid, which may produce large amounts of flammable and explosive gases such as dimethylamine, seriously threatening equipment and production safety.

[0068] In one possible embodiment, the second temperature control strategy is to increase the vacuum level inside the single gas-liquid separation tower by using the vacuum module to reduce the gas pressure inside the tower to a preset safe range within a preset time; and simultaneously close the opening of the steam valve corresponding to the single gas-liquid separation tower to cut off the heat source; and simultaneously fully open the cold water valve corresponding to the single gas-liquid separation tower so that the cold water flow reaches its maximum value.

[0069] Specifically, the vacuum module reduces the pressure inside the tower to a preset safe range within a pre-defined time (e.g., 30 seconds). By rapidly reducing the pressure, the boiling point of the high-boiling-point solvent is significantly lowered, ensuring its relative stability even at the current high temperature and inhibiting further thermal decomposition reactions. Furthermore, a manual emergency control button can be installed. In the event of a system malfunction, operators can manually activate the vacuum module from the control room to control emergency pressure reduction as a final safety measure.

[0070] Specifically, by closing the steam valve, the hot steam supply to the reboiler is completely cut off, stopping the heating of the waste liquid in the column. By eliminating the source of heat input, further temperature increases are prevented, thus inhibiting the intensification of the thermal decomposition reaction.

[0071] By fully opening the cold water valve, the cold water flow rate is maximized. This greatly enhances the cooling capacity of the condenser, rapidly cooling the vapor phase at the top of the tower, causing it to condense quickly, carrying away a large amount of heat, reducing the overall temperature inside the tower, and restoring the system to a safe state as soon as possible.

[0072] As can be seen, in this embodiment, the second temperature control strategy is a key means to ensure the safety of the high-boiling-point solvent waste liquid recovery system under extreme conditions. By rapidly reducing pressure, cutting off heat, and strong cooling, it can quickly curb the risk of thermal decomposition caused by dangerous temperatures and avoid accidents.

[0073] Step S640: Implement a coordinated temperature control strategy for the remaining multiple gas-liquid separation towers according to the first temperature control strategy or the second temperature control strategy.

[0074] Understandably, in the recovery of high-boiling-point solvent waste, multiple gas-liquid separation towers (stripping towers, rectification towers, refining towers, etc.) are interconnected and work collaboratively. If one tower experiences a temperature anomaly, changes in its gas-liquid balance, pressure, and material composition will affect the operation of other towers through inter-tower connecting pipes and material transfer. For example, a temperature anomaly in the stripping tower leading to changes in the gas phase composition alters the composition of the material entering the rectification tower, potentially causing temperature fluctuations in the rectification tower. Therefore, when implementing temperature control strategies for an abnormal tower, it is necessary to simultaneously implement coordinated temperature control strategies for the remaining towers to maintain the stability of the entire system.

[0075] Please see Figure 7 , Figure 7 This is a flowchart illustrating a collaborative temperature control strategy provided in an embodiment of this application. In implementing the collaborative temperature control strategy for the remaining multiple gas-liquid separation towers according to a first temperature control strategy or a second temperature control strategy, the method may further include the following steps:

[0076] Step S710: Identify the individual gas-liquid separation tower with increased temperature.

[0077] Step S720: Is a single gas-liquid separation tower a stripping tower?

[0078] Specifically, if yes, then proceed to step S730; otherwise, proceed to step S740.

[0079] Step S730: Whether to implement the second temperature control strategy for the stripping column.

[0080] Specifically, if so, then proceed to step S731.

[0081] Step S731: Execute a first distillation-coordinated temperature control strategy for the distillation column and a first purification-coordinated temperature control strategy for the purification column.

[0082] Among them, the stripping column is the upstream column of the rectification column, and the rectification column is the upstream column of the refining column.

[0083] In one possible embodiment, the first distillation-coordinated temperature control strategy is to synchronously control the vacuum module to increase the vacuum level in the distillation column according to the rate of decrease of the gas pressure in the distillation column, so that the gas pressure in the distillation column decreases at the same rate of decrease until the pressure decrease amplitude reaches a fifth preset amplitude; and to increase the opening of the reflux valve corresponding to the distillation column, so that the reflux ratio of the second target liquid phase increases by an amplitude of a sixth preset amplitude, so as to reduce the temperature fluctuation at the top of the column.

[0084] In this process, simultaneous depressurization of the distillation column can maintain a stable pressure gradient between the two columns, preventing obstruction or backflow of gas phase transport due to sudden changes in pressure difference, and ensuring the continuity of material transport. By reducing the pressure to lower the boiling point of high-boiling-point solvents, the thermal load on the distillation column can be reduced.

[0085] The reflux liquid, as the cooling medium at the top of the column, can absorb heat from the gas phase and suppress temperature fluctuations at the top of the column caused by pressure reduction. Furthermore, if the pressure reduction in the stripping column increases the gas flow rate into the rectification column, increasing the reflux ratio can stabilize the gas-liquid balance by increasing the liquid phase load, thus avoiding a decrease in separation efficiency due to gas phase overrush.

[0086] In one possible embodiment, the first refining-coordinated temperature control strategy is to stop transferring the second target liquid phase from the distillation column to the refining column; and to increase the opening of the cold water valve corresponding to the refining column, thereby increasing the cold water flow rate to avoid water vaporization leading to a decrease in the purity of the generated high-purity solvent.

[0087] The current-stage distillation column experiences fluctuations in its product composition (such as a temporary increase in moisture content) due to the implementation of coordinated temperature control strategies (e.g., pressure reduction and reflux ratio adjustment). If this product continues to be fed into the purification column, it may affect the purity of the final product. By suspending material transfer and isolating upstream disturbances, the temporary anomalies in the distillation column are prevented from being transmitted to the purification column, ensuring that the purification column operates under stable conditions. Furthermore, by enhancing cooling to suppress moisture vaporization pathways, the separation efficiency of the purification column is maintained, ensuring that the purity of the final high-purity solvent is not affected by upstream operations.

[0088] It should be clarified that the embodiments of this application provide a specific example of implementing a coordinated temperature control strategy for other columns when the stripping column implements the second temperature control strategy. However, this application does not limit the specific scheme of whether and how the coordinated temperature control strategy is implemented for other columns when the stripping column implements the first temperature control strategy.

[0089] Step S740: Is a single gas-liquid separation tower a distillation tower?

[0090] Specifically, if yes, then proceed to step S750; otherwise, proceed to step S760.

[0091] Step S750: Whether the first temperature control strategy is implemented for the distillation column.

[0092] Specifically, if yes, then proceed to step S751; otherwise, proceed to step S752.

[0093] Step S751: Execute the first stripping synergistic temperature control strategy for the stripping column.

[0094] In one possible embodiment, the first distillation-coordinated temperature control strategy is to synchronously control the vacuum module to increase the vacuum level in the distillation column according to the rate of decrease of the gas pressure in the distillation column, so that the gas pressure in the distillation column decreases at the same rate of decrease.

[0095] Understandably, when the pressure in the distillation column is reduced (e.g., by implementing the first temperature control strategy), the decrease in internal gas pressure will disrupt the pressure balance between the upstream and downstream. If the pressure in the stripping column does not decrease synchronously, a pressure difference may form between the stripping and distillation columns, causing liquid in the stripping column bottom to flow into the distillation column due to the pressure difference. Furthermore, by synchronizing the depressurization rate, the pressure difference between the stripping and distillation columns can be maintained stable (or close to the original difference) to prevent backflow caused by pressure imbalance.

[0096] Step S752: Determine whether to implement the second temperature control strategy for the distillation column.

[0097] Specifically, if so, proceed to step S753.

[0098] Step S753: Execute a second stripping synergistic temperature control strategy for the stripping column and a second refining synergistic temperature control strategy for the refining column.

[0099] Understandably, when the distillation column implements the second temperature control strategy (such as rapid pressure reduction and closing of steam valves), its operating status will change drastically. It is necessary to adjust the parameters of the upstream stripping column and the downstream refining column simultaneously to prevent the stripping column from experiencing gas-liquid transmission imbalance due to the rapid pressure drop in the distillation column, and to avoid material accumulation or purity fluctuations in the refining column due to feed interruption or heat imbalance.

[0100] In one possible embodiment, the second distillation-coordinated temperature control strategy involves synchronously controlling the vacuum module to increase the vacuum level in the distillation column according to the rate of decrease in the gas pressure inside the distillation column, so that the gas pressure inside the distillation column decreases at the same rate of decrease; and reducing the opening of the steam valve corresponding to the distillation column, so that the amount of hot steam delivered decreases by a third preset value, in order to prevent the reboiler from generating excessive gas phase.

[0101] In this method, the vacuum level of the stripping column is increased simultaneously according to the rate of pressure drop in the distillation column, so that the pressure drop rates of the two columns are the same, which helps to maintain a stable pressure gradient between the stripping and distillation columns.

[0102] When the distillation column implements the second temperature control strategy (such as closing the steam valve), its processing capacity decreases. If the stripping column continues to produce a large amount of gas, it will cause the distillation column to be overloaded in the gas phase (even if the vacuum is reduced, excessive gas volume may still cause flooding or temperature runaway). Therefore, reducing the steam input can prevent the distillation column from being unable to process due to excessive gas intake.

[0103] In one possible embodiment, the second refining synergistic temperature control strategy is to stop transferring the second target liquid phase from the distillation column to the refining column; and to fully open the reflux valve corresponding to the refining column, so that the high-purity solvent generated by the refining column can be continuously transferred back into the refining column to maintain the material balance in the refining column; and to increase the opening of the cold water valve corresponding to the refining column, so that the cold water flow rate increases by a seventh preset value to reduce pressure fluctuations in the column.

[0104] When the distillation column implements an emergency strategy, the purity of its product may fluctuate (e.g., insufficient separation due to rapid depressurization). Continuing to feed at this time will contaminate the high-purity material in the purification column.

[0105] Maximizing the reflux ratio can enhance the mass transfer efficiency within the tower. Even if there is no feed for a while, the concentration distribution within the tower can be kept stable through internal circulation, preventing moisture vaporization (moisture accumulation may evaporate due to heat imbalance, reducing product purity).

[0106] After the refining tower stops feeding, the heat inside the tower mainly comes from the reboiler (if it is not shut down) or residual heat of vaporization. Increasing cooling can quickly remove the heat and suppress the pressure rise caused by temperature fluctuations (such as the additional gas phase generated by water vaporization).

[0107] Step S760: Determine whether to implement the first temperature control strategy or the second temperature control strategy for the refining tower.

[0108] Specifically, if so, proceed to step S761.

[0109] Step S761: Execute the third stripping synergistic temperature control strategy for the stripping column.

[0110] In one possible embodiment, the third distillation-coordinated temperature control strategy is to synchronously control the vacuum module to increase the vacuum level in the distillation column according to the rate of decrease of the gas pressure in the refining column, so that the gas pressure in the distillation column decreases at the same rate of decrease; and to reduce the opening of the steam valve corresponding to the distillation column, so that the amount of hot steam delivered decreases by a fourth preset value, in order to prevent the reboiler from generating excessive gas phase.

[0111] It is understandable that when the temperature inside the refining column rises abnormally, the third stripping synergistic temperature control strategy is only implemented for the stripping column because the stripping column is the upstream column of the refining column. Regulating the stripping column can indirectly control the material / heat entering the refining column and alleviate the pressure on the refining column.

[0112] Among these measures, simultaneously reducing the gas pressure can maintain a stable pressure gradient between the two, thus preventing material backflow or transport obstruction caused by pressure differences. Furthermore, by reducing the amount of hot steam transported, the distillation products in the stripping tower can be reduced at the source, thereby indirectly reducing the material entering the refining tower. By directly reducing the temperature drive of the upstream tower, the temperature rise pressure in the refining tower is fundamentally alleviated.

[0113] As can be seen, in this embodiment, the collaborative temperature control strategy monitors the temperature and pressure changes of each gas-liquid separation tower and controls equipment such as vacuum modules, steam valves, and chilled water valves in a coordinated manner to achieve coordinated adjustment of parameters among multiple towers. When the temperature of a certain tower is abnormal, not only is a targeted temperature control strategy executed, but the vacuum degree, heat input, and cooling intensity of the upstream and downstream towers are also adjusted simultaneously to avoid system chain reactions caused by local anomalies. This effectively prevents problems such as material backflow and gas phase overload, maintains a stable system pressure gradient, material balance, and heat balance, ensures the safe and stable operation of the high-boiling-point solvent waste liquid recovery process, and improves product purity and system operating efficiency.

[0114] The above primarily describes the solutions of the embodiments of this application from the perspective of the method execution process. It is understood that, in order to achieve the above functions, mobile electronic devices include corresponding hardware structures and / or software modules for executing each function. Those skilled in the art should readily recognize that, in conjunction with the units and algorithm steps of the various examples described in the embodiments provided herein, this application can be implemented in hardware or a combination of hardware and computer software. Whether a function is executed by hardware or by computer software driving hardware depends on the specific application and design constraints of the technical solution. Those skilled in the art can use different methods to implement the described functions for each specific application, but such implementation should not be considered beyond the scope of this application.

[0115] This application embodiment can divide the electronic device into functional units according to the above method example. For example, each function can be divided into a separate functional unit, or two or more functions can be integrated into one processing unit. The integrated unit can be implemented in hardware or as a software functional unit. It should be noted that the unit division in this application embodiment is illustrative and only represents one logical functional division. In actual implementation, there may be other division methods.

[0116] Please see Figure 8 , Figure 8This is a functional module diagram of a temperature adaptive regulation device in a high-boiling-point solvent waste liquid recovery process provided in an embodiment of this application, as shown below. Figure 8 As shown, the device includes the following units:

[0117] The first processing unit 810 is configured to, when the absolute value of the difference between the temperature inside the single gas-liquid separation tower and the first preset temperature is detected to be less than a preset difference, execute a first temperature control strategy for the single gas-liquid separation tower based on the vacuum module, the steam valve corresponding to the single gas-liquid separation tower, and the cold water valve; and, when the temperature inside the single gas-liquid separation tower is detected to reach a second preset temperature, execute a second temperature control strategy for the single gas-liquid separation tower based on the vacuum module, the steam valve corresponding to the single gas-liquid separation tower, and the cold water valve, wherein the first preset temperature is lower than the second preset temperature;

[0118] The second processing unit 820 is used to execute a coordinated temperature control strategy on the remaining multiple gas-liquid separation towers according to the first temperature control strategy or the second temperature control strategy, so as to realize the linkage control of the temperature inside the multiple gas-liquid separation towers during the high-boiling-point solvent waste liquid recovery process.

[0119] As can be seen, in this embodiment, different control strategies are implemented for a single tower with abnormal temperature based on the specific temperature value. At the same time, a coordinated control strategy is implemented for the other multiple towers. When the pressure of the upstream tower is reduced, the pressure of the downstream tower is adjusted proportionally. When the downstream tower is abnormal, the load input of the upstream tower is reduced. This achieves linkage control of multiple towers under abnormal temperature conditions, which is beneficial to improving the safety and efficiency of high-boiling-point solvent waste liquid recovery.

[0120] In one embodiment, before the absolute value of the difference between the temperature inside the single gas-liquid separator and the first preset temperature is detected to be less than the preset difference, the first processing unit 810 is further configured to: detect an increase in temperature inside the single gas-liquid separator.

[0121] In one embodiment, regarding the implementation of a first temperature control strategy for the single gas-liquid separation tower based on the vacuum module, the steam valve corresponding to the single gas-liquid separation tower, and the cold water valve, the first processing unit 810 is specifically configured to: increase the vacuum level within the single gas-liquid separation tower through the vacuum module to reduce the gas pressure within the tower; and simultaneously reduce the opening of the steam valve corresponding to the single gas-liquid separation tower, such that the flow rate of the hot steam decreases by a first preset value, thereby reducing the heating load within the reboiler; and simultaneously increase the opening of the cold water valve corresponding to the single gas-liquid separation tower, such that the flow rate of the cold water increases by a second preset value, thereby accelerating the condensation of the gas phase at the top of the tower.

[0122] In one embodiment, regarding the implementation of the second temperature control strategy for the single gas-liquid separation tower based on the vacuum module, the steam valve corresponding to the single gas-liquid separation tower, and the cold water valve, the first processing unit 810 is specifically configured to: increase the vacuum level inside the single gas-liquid separation tower through the vacuum module to reduce the gas pressure inside the tower to a preset safe range within a preset time; and simultaneously close the opening of the steam valve corresponding to the single gas-liquid separation tower to cut off the heat source; and simultaneously fully open the cold water valve corresponding to the single gas-liquid separation tower to maximize the cold water flow rate.

[0123] In one embodiment, regarding the aspect of implementing a coordinated temperature control strategy for the remaining plurality of gas-liquid separation towers according to the first temperature control strategy or the second temperature control strategy, the second processing unit 820 is specifically configured to: if the second temperature control strategy is implemented for the stripping tower, then simultaneously implement a first rectification coordinated temperature control strategy for the distillation tower and a first purification coordinated temperature control strategy for the purification tower; if the first temperature control strategy is implemented for the distillation tower, then simultaneously implement a first stripping coordinated temperature control strategy for the stripping tower; and if the second temperature control strategy is implemented for the distillation tower, then simultaneously implement a second stripping coordinated temperature control strategy for the stripping tower and a second purification coordinated temperature control strategy for the purification tower; if the first temperature control strategy or the second temperature control strategy is implemented for the purification tower, then simultaneously implement a third stripping coordinated temperature control strategy for the stripping tower.

[0124] In one embodiment, regarding the implementation of the first stripping synergistic temperature control strategy for the stripping column, the second processing unit 820 is specifically configured to: synchronously control the vacuum module to increase the vacuum level in the stripping column according to the rate of decrease of the gas pressure in the stripping column, so that the gas pressure in the stripping column decreases at the same rate of decrease.

[0125] In one embodiment, regarding the implementation of the second distillation-coordinated temperature control strategy for the distillation column, the second processing unit 820 is specifically configured to: synchronously control the vacuum module to increase the vacuum level in the distillation column according to the rate of decrease of the gas pressure in the distillation column, so that the gas pressure in the distillation column decreases at the same rate of decrease; and reduce the opening of the steam valve corresponding to the distillation column, so that the amount of hot steam delivered decreases by a third preset value, in order to prevent the reboiler from generating excessive gas phase during heating.

[0126] In one embodiment, regarding the implementation of the third distillation synergistic temperature control strategy for the distillation column, the second processing unit 820 is specifically configured to: synchronously control the vacuum module to increase the vacuum level in the distillation column according to the rate of decrease of the gas pressure in the refining column, so that the gas pressure in the distillation column decreases at the same rate of decrease; and reduce the opening of the steam valve corresponding to the distillation column, so that the amount of hot steam delivered decreases by a fourth preset value, in order to prevent the reboiler from generating excessive gas phase during heating.

[0127] In one embodiment, regarding the implementation of the first distillation-coordinated temperature control strategy for the distillation column, the second processing unit 820 is specifically configured to: synchronously control the vacuum module to increase the vacuum level in the distillation column according to the rate of decrease of the gas pressure in the distillation column, so that the gas pressure in the distillation column decreases at the same rate of decrease until the pressure decrease amplitude reaches a fifth preset amplitude; and increase the opening of the reflux valve corresponding to the distillation column, so that the reflux ratio of the second target liquid phase increases by an amplitude of a sixth preset amplitude, thereby reducing the temperature fluctuation at the top of the column.

[0128] In one embodiment, regarding the implementation of the first refining synergistic temperature control strategy for the refining column, the second processing unit 820 is specifically configured to: stop the transfer of the second target liquid phase from the distillation column to the refining column; and increase the opening of the cold water valve corresponding to the refining column, thereby increasing the cold water flow rate to prevent water vaporization from causing a decrease in the purity of the generated high-purity solvent.

[0129] In one embodiment, regarding the implementation of the second refining synergistic temperature control strategy for the refining column, the second processing unit 820 is specifically configured to: stop the transfer of the second target liquid phase from the distillation column to the refining column; and fully open the reflux valve corresponding to the refining column, so that the high-purity solvent generated by the refining column can be continuously transferred back into the refining column to maintain the material balance within the refining column; and increase the opening of the cold water valve corresponding to the refining column, so that the cold water flow rate increases by a seventh preset value to reduce pressure fluctuations within the column.

[0130] Figure 9 This is a structural block diagram of an electronic device provided in this application. For example... Figure 9 As shown, the electronic device 900 may include one or more of the following components: a processor 901 and a memory 902 coupled to the processor 901, wherein the memory 902 may store one or more computer programs, which may be configured to implement the methods described in the examples above when executed by one or more processors 901. The electronic device 900 may be a terminal device in the aforementioned high-boiling-point solvent waste recovery system.

[0131] Processor 901 may include one or more processing cores. Processor 901 connects to various parts within the electronic device 900 using various interfaces and lines, and performs various functions and processes data of the electronic device 900 by running or executing instructions, programs, code sets, or instruction sets stored in memory 902, and by calling data stored in memory 902. Optionally, processor 901 may be implemented using at least one hardware form of Digital Signal Processing (DSP), Field-Programmable Gate Array (FPGA), or Programmable Logic Array (PLA). Processor 901 may integrate one or a combination of several of the following: Central Processing Unit (CPU), Graphics Processing Unit (GPU), and modem. It is understood that the aforementioned modem may also not be integrated into processor 901, but may be implemented separately through a communication chip.

[0132] The memory 902 may include random access memory (RAM) or read-only memory (ROM). The memory 902 can be used to store instructions, programs, code, code sets, or instruction sets. The memory 902 may include a program storage area and a data storage area. The program storage area may store instructions for implementing an operating system, instructions for implementing at least one function (such as touch functionality, sound playback functionality, image playback functionality, etc.), and instructions for implementing the above-described method examples. The data storage area may also store data created during the use of the electronic device 900.

[0133] It is understood that the electronic device 900 may include more or fewer structural elements than those shown in the above block diagram, such as a power module, physical buttons, WiFi (Wireless Fidelity) module, speaker, Bluetooth module, sensor, etc., without limitation.

[0134] This application also provides a computer storage medium storing a computer program / instructions thereon, which, when executed by a processor, implements some or all of the steps of any of the methods described in the above method embodiments.

[0135] This application also provides a computer program product, which includes a non-transitory computer-readable storage medium storing a computer program operable to cause a computer to perform some or all of the steps of any of the methods described in the above method embodiments.

[0136] It should be understood that in the various embodiments of this application, the order of the above-mentioned processes does not imply the order of execution. The execution order of each process should be determined by its function and internal logic, and should not constitute any limitation on the implementation process of the embodiments of this application.

[0137] In the several embodiments provided in this application, it should be understood that the disclosed methods, apparatuses, and systems can be implemented in other ways. For example, the apparatus embodiments described above are merely illustrative; for example, the division of units is merely a logical functional division, and there may be other division methods in actual implementation; for example, multiple units or components may be combined or integrated into another system, or some features may be ignored or not executed. Furthermore, the coupling or direct coupling or communication connection shown or discussed may be through some interfaces, and the indirect coupling or communication connection between devices or units may be electrical, mechanical, or other forms.

[0138] The units described as separate components may or may not be physically separate. The components shown as units may or may not be physical units; that is, they may be located in one place or distributed across multiple network units. Some or all of the units can be selected to achieve the purpose of this embodiment according to actual needs.

[0139] Furthermore, the functional units in the various embodiments of the present invention can be integrated into one processing unit, or each unit can be physically comprised separately, or two or more units can be integrated into one unit. The integrated unit described above can be implemented in hardware or in the form of hardware plus software functional units.

[0140] The integrated units implemented as software functional units described above can be stored in a computer-readable storage medium. These software functional units, stored in a storage medium, include several instructions to cause a computer device (which may be a personal computer, server, or network device, etc.) to execute partial steps of the methods of the various embodiments of the present invention. The aforementioned storage medium includes: a USB flash drive, a portable hard drive, a magnetic disk, an optical disk, volatile memory, or non-volatile memory. The non-volatile memory can be read-only memory (ROM), programmable read-only memory (PROM), erasable programmable read-only memory (EPROM), electrically erasable programmable read-only memory (EEPROM), or flash memory. The volatile memory can be random access memory (RAM), which is used as an external cache. By way of example, but not limitation, many forms of random access memory (RAM) are available, such as static random access memory (SRAM), dynamic random access memory (DRAM), synchronous dynamic random access memory (SDRAM), double data rate synchronous dynamic random access memory (DDRSDRAM), enhanced synchronous dynamic random access memory (ESDRAM), synchronous linked dynamic random access memory (SLDRAM), and direct rambus RAM (DRRAM), etc., which are various media that can store program code.

[0141] While the present invention has been disclosed above, it is not limited thereto. Any person skilled in the art can easily conceive of variations or substitutions without departing from the spirit and scope of the present invention, and various modifications and alterations can be made, including combinations of the different functions and implementation steps described above, as well as software and hardware implementation methods, all of which are within the protection scope of the present invention.

Claims

1. A temperature adaptive adjustment strategy in a high-boiling-point solvent waste liquid recovery process, characterized in that, This system is applied to the recovery of high-boiling-point solvent waste liquid. The system includes a vacuum module, a distillation module, and a control module. The distillation module comprises multiple gas-liquid separation towers connected in sequence. Each gas-liquid separation tower consists of a stripping tower, a rectification tower, and a refining tower connected in sequence. The bottom of each gas-liquid separation tower is connected to a steam valve, and the top is connected to a cold water valve. The steam valve controls the heating of the waste liquid at the bottom of the tower, which contains high-boiling-point solvents. The cold water valve controls the condensation of the vapor phase at the top of the tower. The vacuum module is connected to each of the multiple gas-liquid separation towers, and the control module is connected to the vacuum module, multiple steam valves, and multiple cold water valves. The vacuum module is used to regulate the vacuum level in multiple gas-liquid separation towers in order to suppress the thermal decomposition rate by lowering the boiling point of the waste liquid in the towers. The distillation module is used to perform multi-stage distillation treatment on the waste liquid in the tower through multiple gas-liquid separation towers to obtain high-purity solvents; The control module is configured to, when the absolute value of the temperature difference between a single gas-liquid separation tower and a first preset temperature is detected to be less than a preset difference, execute a first temperature control strategy for the single gas-liquid separation tower based on the vacuum module, the steam valve corresponding to the single gas-liquid separation tower, and the cold water valve. The first temperature control strategy involves increasing the vacuum level within the single gas-liquid separation tower via the vacuum module to reduce the gas pressure within the tower; simultaneously reducing the opening of the steam valve corresponding to the single gas-liquid separation tower, causing a decrease in the hot steam flow rate by a first preset magnitude to reduce the heating load in the reboiler; and simultaneously increasing the opening of the cold water valve corresponding to the single gas-liquid separation tower, causing an increase in the cold water flow rate by a second preset magnitude to accelerate the condensation of the gas phase at the top of the tower; and... When the temperature inside a single gas-liquid separator is detected to reach the second preset temperature, a second temperature control strategy is executed for the single gas-liquid separator based on the vacuum module, the steam valve and the cold water valve corresponding to the single gas-liquid separator. The second temperature control strategy is to increase the vacuum level inside the single gas-liquid separator by the vacuum module to reduce the gas pressure inside the separator to a preset safe range within a preset time; and simultaneously close the opening of the steam valve corresponding to the single gas-liquid separator to cut off the heat source; and simultaneously fully open the cold water valve corresponding to the single gas-liquid separator to make the cold water flow reach the maximum value, so that the first preset temperature is lower than the second preset temperature. If a second temperature control strategy is implemented for the stripping column, a first distillation-coordinated temperature control strategy is simultaneously implemented for the rectification column. The first distillation-coordinated temperature control strategy involves synchronously controlling the vacuum module to increase the vacuum level in the rectification column according to the rate of decrease in gas pressure within the stripping column, so that the gas pressure in the rectification column decreases at the same rate of decrease until the pressure decrease reaches a fifth preset value; and increasing the opening of the reflux valve corresponding to the rectification column, so that the reflux ratio of the second target liquid phase increases by a sixth preset value to reduce temperature fluctuations at the top of the column. A first purification-coordinated temperature control strategy is also implemented for the purification column, which involves stopping the transfer of the second target liquid phase from the rectification column to the purification column; and increasing the opening of the cold water valve corresponding to the purification column, so that the cold water flow rate increases to prevent water vaporization from reducing the purity of the generated high-purity solvent. If a first temperature control strategy is applied to the distillation column, a first stripping-coordinated temperature control strategy is simultaneously applied to the stripping column. This first stripping-coordinated temperature control strategy involves synchronously controlling the vacuum module to increase the vacuum level in the stripping column based on the rate of decrease in gas pressure within the distillation column, thereby reducing the gas pressure in the stripping column at the same rate of decrease. Furthermore, if a second temperature control strategy is applied to the distillation column, a second stripping-coordinated temperature control strategy is simultaneously applied to the stripping column. This second stripping-coordinated temperature control strategy involves synchronously controlling the vacuum module to increase the vacuum level in the stripping column based on the rate of decrease in gas pressure within the distillation column, thereby reducing the gas pressure in the stripping column at the same rate of decrease. And, reducing... The opening degree of the steam valve corresponding to the small distillation column is adjusted so that the hot steam delivery rate decreases by a third preset value to prevent excessive gas phase generation during reboiler heating. A second refining-coordinated temperature control strategy is implemented for the refining column, which involves stopping the transfer of the second target liquid phase from the distillation column to the refining column; fully opening the reflux valve corresponding to the refining column to continuously transfer the high-purity solvent generated in the refining column back into the column to maintain material balance; and increasing the opening degree of the cold water valve corresponding to the refining column to increase the cold water flow rate by a seventh preset value to reduce pressure fluctuations within the column. If the first or second temperature control strategy is implemented for the refining tower, a third stripping-coordinated temperature control strategy is simultaneously implemented for the stripping tower. The third stripping-coordinated temperature control strategy involves synchronously controlling the vacuum module to increase the vacuum level in the stripping tower according to the rate of decrease in gas pressure in the refining tower, so that the gas pressure in the stripping tower decreases at the same rate of decrease; and reducing the opening of the steam valve corresponding to the stripping tower, so that the amount of hot steam delivered decreases by a fourth preset value, in order to prevent excessive gas phase from being generated by reboiler heating, thereby achieving linkage control of the temperature in multiple gas-liquid separation towers during the high-boiling-point solvent waste recovery process.

2. The strategy according to claim 1, characterized in that, The plurality of gas-liquid separation towers are connected in sequence. The distillation module further includes a plurality of reboilers, a plurality of condensers, and a plurality of reflux tanks, each corresponding to one of the plurality of gas-liquid separation towers. The bottom of each gas-liquid separation tower is connected to the reboiler, the top of the tower is connected to the condenser, the condenser is connected to the reflux tank, and the reflux tank is connected to two adjacent gas-liquid separation towers simultaneously. The reboiler is used to receive waste liquid from the bottom of the column via a liquid phase pipeline; and the reboiler is connected to a steam pipeline via a steam valve to receive hot steam, and the waste liquid in the reboiler is heated by the hot steam to obtain a gas phase; and the reboiler is used to transfer the gas phase back to the gas-liquid separation column via a gas phase pipeline. The condenser is used to receive the gas phase located at the top of the tower; and the condenser is connected to a cold water pipeline through the cold water valve to access cold water, and the gas phase is condensed into a target liquid phase through the cold water; and the condenser is used to transfer the target liquid phase to the reflux tank. The reflux tank is used to receive the target liquid phase from the condenser; and the reflux tank is connected to the reflux pipeline via a reflux valve to control the reflux flow rate of the target liquid phase back into the gas-liquid separation tower; and the reflux tank is used to transfer the target liquid phase that does not participate in the reflux to the next gas-liquid separation tower via a pipeline, and the control module is connected to the reflux valve.

3. The strategy according to claim 2, characterized in that, The multi-stage distillation process includes performing a first-stage distillation on the waste liquid in the bottom of the distillation column through the first reboiler and the first condenser corresponding to the distillation column to obtain a first target liquid phase, and transferring the first target liquid phase to the bottom of the distillation column. as well as, The first target liquid phase in the bottom of the distillation column is subjected to a second-stage distillation through the second reboiler and the second condenser corresponding to the distillation column to obtain the second target liquid phase, and the second target liquid phase is transferred to the bottom of the purification column. as well as, The second target liquid phase in the bottom of the purification column is subjected to a third-stage distillation through the third reboiler and the third condenser corresponding to the purification column to obtain the high-purity solvent. The high-purity solvent is the product obtained by distillation and purification of the high-boiling-point solvent in the waste liquid.

4. The strategy according to any one of claims 1-3, characterized in that, The control module is also configured to detect a temperature rise in the single gas-liquid separation tower before detecting that the absolute value of the difference between the temperature inside the single gas-liquid separation tower and the first preset temperature is less than the preset difference.

5. A temperature adaptive regulation device for a high-boiling-point solvent waste liquid recovery process, characterized in that, This system is applied to the recovery of high-boiling-point solvent waste liquid. The system includes a vacuum module, a distillation module, and a control module. The distillation module includes multiple gas-liquid separation towers connected in sequence. Each gas-liquid separation tower has a stripping tower, a rectification tower, and a refining tower connected in sequence. The bottom of each gas-liquid separation tower is connected to a steam valve, and the top is connected to a cold water valve. The steam valve controls the heating of the waste liquid at the bottom of the tower, which contains high-boiling-point solvents. The cold water valve controls the condensation of the vapor phase at the top of the tower. The vacuum module is connected to each of the multiple gas-liquid separation towers, and the control module is connected to the vacuum module, multiple steam valves, and multiple cold water valves. The device includes: The first processing unit is configured to, when the absolute value of the temperature difference between a single gas-liquid separator and a first preset temperature is detected to be less than a preset difference, execute a first temperature control strategy for the single gas-liquid separator based on the vacuum module, the steam valve corresponding to the single gas-liquid separator, and the cold water valve. The first temperature control strategy involves increasing the vacuum level within the single gas-liquid separator through the vacuum module to reduce the gas pressure inside the separator; simultaneously reducing the opening of the steam valve corresponding to the single gas-liquid separator, causing the hot steam flow rate to decrease by a first preset value, thereby reducing the heating load in the reboiler; and simultaneously increasing the opening of the cold water valve corresponding to the single gas-liquid separator, causing the cold water flow rate to increase by a first preset value. Two preset amplitudes are used to accelerate the condensation of the gas phase at the top of the tower; and when the temperature inside a single gas-liquid separation tower is detected to reach the second preset temperature, a second temperature control strategy is executed for the single gas-liquid separation tower based on the vacuum module, the steam valve and the cold water valve corresponding to the single gas-liquid separation tower. The second temperature control strategy is to increase the vacuum degree inside the single gas-liquid separation tower through the vacuum module to reduce the gas pressure inside the tower to a preset safe range within a preset time; and simultaneously close the opening of the steam valve corresponding to the single gas-liquid separation tower to cut off the heat source; and simultaneously fully open the cold water valve corresponding to the single gas-liquid separation tower to make the cold water flow reach the maximum value, and the first preset temperature is lower than the second preset temperature. The second processing unit is configured to, if a second temperature control strategy is implemented for the stripping column, simultaneously implement a first distillation-coordinated temperature control strategy for the rectification column. The first distillation-coordinated temperature control strategy involves synchronously controlling the vacuum module to increase the vacuum level in the rectification column based on the rate of decrease in gas pressure within the stripping column, causing the gas pressure in the rectification column to decrease at the same rate of decrease until the pressure drop reaches a fifth preset value; and increasing the opening of the corresponding reflux valve in the rectification column, increasing the reflux ratio of the second target liquid phase by a sixth preset value to reduce temperature fluctuations at the top of the column; and implementing a first purification-coordinated temperature control strategy for the purification column, which involves stopping the dispensing of the second target liquid phase from the rectification column. The distillation column is transferred to the purification column; and the opening of the corresponding cold water valve in the purification column is increased to increase the cold water flow rate, so as to avoid the reduction of the purity of the generated high-purity solvent due to water vaporization; if the first temperature control strategy is implemented for the distillation column, a first stripping-coordinated temperature control strategy is simultaneously implemented for the stripping column. The first stripping-coordinated temperature control strategy is to synchronously control the vacuum module to increase the vacuum degree in the stripping column according to the rate of decrease of the gas pressure in the distillation column, so that the gas pressure in the stripping column decreases at the same rate of decrease; and if the second temperature control strategy is implemented for the distillation column, a second stripping-coordinated temperature control strategy is simultaneously implemented for the stripping column. The second stripping-coordinated temperature control strategy is to synchronously control the vacuum module to increase the vacuum degree in the stripping column according to the rate of decrease of the gas pressure in the distillation column. The synchronous control vacuum module increases the vacuum level in the stripping column, causing the gas pressure in the stripping column to decrease at the same rate; and reduces the opening of the steam valve corresponding to the stripping column, causing the hot steam delivery rate to decrease by a third preset value to prevent excessive gas phase generation during reboiler heating; implements a second refining-coordinated temperature control strategy for the refining column, which stops the transfer of the second target liquid phase from the stripping column to the refining column; fully opens the reflux valve corresponding to the refining column, allowing the high-purity solvent generated in the refining column to be continuously transferred back into the refining column to maintain material balance within the refining column; and increases the opening of the cold water valve corresponding to the refining column, so that... The cold water flow rate is increased by the seventh preset value to reduce pressure fluctuations within the tower. If the first or second temperature control strategy is implemented for the refining tower, the third stripping-coordinated temperature control strategy is simultaneously implemented for the stripping tower. The third stripping-coordinated temperature control strategy involves synchronously controlling the vacuum module to increase the vacuum level in the stripping tower according to the rate of decrease in gas pressure within the refining tower, so that the gas pressure in the stripping tower decreases at the same rate of decrease. Additionally, the opening of the steam valve corresponding to the stripping tower is reduced, so that the amount of hot steam delivered decreases by the fourth preset value to prevent excessive gas phase generation during reboiler heating. This achieves coordinated temperature control within multiple gas-liquid separation towers during the high-boiling-point solvent waste recovery process.

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