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

Abstract

The invention provides a temperature self-adaptive adjustment strategy and device in a high-boiling-point solvent waste liquid recovery process, and the method comprises the steps: executing a first temperature control strategy for a single tower based on a vacuum module, a steam valve and a cold water valve when it is detected that the absolute value of the difference value between the temperature in the single gas-liquid separation tower and a first preset temperature is smaller than a preset difference value; when it is detected that the temperature in the single gas-liquid separation tower reaches a second preset temperature, a second temperature control strategy is executed for the single tower based on the vacuum module, the steam valve and the cold water valve; and according to the first temperature control strategy or the second temperature control strategy, a cooperative temperature control strategy is executed on the rest of the gas-liquid separation towers, so that linkage control over the temperatures in the gas-liquid separation towers in the recovery process of the high-boiling-point solvent waste liquid is achieved. The recovery safety and the recovery efficiency of the high-boiling-point solvent waste liquid are improved.

Description

Technical Field

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

[0002] In the field of high-boiling solvent waste liquid recovery, the distillation process is the core technical path to realize solvent recycling. The waste liquid recovery of high-boiling solvents relies on multi-stage distillation to separate impurities. However, there is a strong coupling relationship between the pressure and temperature in the gas-liquid separation tower - reducing the pressure can significantly reduce the boiling point of high-boiling solvents, thereby reducing the risk of thermal decomposition at high temperatures. However, in actual operation, temperature fluctuations in the tower are inevitable. When the temperature rises abnormally, high-boiling solvents such as DMF (N,N-dimethylformamide) will rapidly decompose thermally to produce a large amount of dimethylamine. If the concentration of dimethylamine reaches the explosion threshold in the gas phase space, it may trigger a deflagration accident, seriously threatening equipment safety and production continuity.

[0003] Traditional high-boiling solvent waste liquid recovery systems generally adopt a fixed pressure-temperature control mode, that is, parameters such as the vacuum degree and heating amount 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 is likely to cause the spread of faults. Summary of the Invention

[0004] This application provides a temperature adaptive regulation strategy and device in a high-boiling solvent waste liquid recovery process. For a tower with abnormal temperature, different control strategies are executed based on the specific temperature value. At the same time, for the remaining multiple towers, a coordinated control strategy is executed. When the upstream tower reduces pressure, the downstream tower adjusts the pressure proportionally; when the downstream tower is abnormal, the upstream tower reduces the load input to achieve the linkage control of multiple towers under abnormal temperature.

[0005] In the first aspect, this application provides a temperature adaptive regulation strategy in a high-boiling solvent waste liquid recovery process, which is applied to a high-boiling solvent waste liquid recovery system. The system includes a vacuum module, a distillation module, and a control module. The distillation module includes a plurality of gas-liquid separation towers connected in sequence. The bottom of a single 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 the steam to heat the waste liquid at the tower bottom, and the waste liquid contains the high-boiling solvent. The cold water valve is used to control the cold water to condense the gas phase at the tower top. The vacuum module is respectively connected to the plurality of gas-liquid separation towers, and the control module is respectively connected to the vacuum module, a plurality of steam valves, and a plurality of cold water valves; wherein, The vacuum module is used to regulate the vacuum degree in the plurality of gas-liquid separation towers to inhibit the thermal decomposition rate by reducing the boiling point of the waste liquid in the tower; The rectification module is used to perform multi-stage rectification treatment on the waste liquid in the tower through the multiple gas-liquid separation towers to obtain high-purity solvent; The control module is used to, when the absolute value of the difference between the temperature in the single gas-liquid separation tower and the first preset temperature is less than the preset difference, execute a first temperature control strategy 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; and, when the temperature in the single gas-liquid separation tower reaches the second preset temperature, execute a second temperature control strategy 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, where the first preset temperature is lower than the second preset temperature; Execute a cooperative 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 temperatures in the multiple gas-liquid separation towers during the recovery process of the high-boiling-point solvent waste liquid.

[0006] In a second aspect, an embodiment of the present application provides a temperature adaptive adjustment device in a high-boiling-point solvent waste liquid recovery process, which is applied to a high-boiling-point solvent waste liquid recovery system. The system includes a vacuum module, a rectification module and a control module. The rectification module includes a plurality of gas-liquid separation towers connected in sequence. The bottom of a single gas-liquid separation tower is connected to a steam valve, and the top of the tower is connected to a cold water valve. The steam valve is used to control the 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 the cold water to condense the gas phase at the top of the tower. The vacuum module is respectively connected to the plurality of gas-liquid separation towers. The control module is respectively connected to the vacuum module, a plurality of steam valves and a plurality of cold water valves; the device includes: The first processing unit is used to, when the absolute value of the difference between the temperature in the single gas-liquid separation tower and the first preset temperature is less than the preset difference, execute a first temperature control strategy 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; and, when the temperature in the single gas-liquid separation tower reaches the second preset temperature, execute a second temperature control strategy 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, where the first preset temperature is lower than the second preset temperature; The second processing unit is used to execute a cooperative 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 temperatures in the multiple gas-liquid separation towers during the recovery process of the high-boiling-point solvent waste liquid.

[0007] In a third aspect, an embodiment of the present application provides an electronic device, including a processor, a memory, and one or more programs. The one or more programs are stored in the memory and configured to be executed by the processor. The programs include instructions for performing the steps in the first aspect of the embodiments of the present application.

[0008] In a fourth aspect, an embodiment of the present application provides a computer-readable storage medium, on which a computer program / instructions is stored. The computer program / instructions, when executed by a processor, implements the steps of the strategy described in the first aspect above.

[0009] It can be seen that in the embodiments of the present application, when the absolute value of the difference between the temperature in a single gas-liquid separation tower and the first preset temperature is 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 and the cold water valve corresponding to the single gas-liquid separation tower; and when the temperature in the single gas-liquid separation tower reaches 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; and a coordinated temperature control strategy is executed 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 the linkage control of the temperatures in multiple gas-liquid separation towers during the recovery process of high-boiling solvent waste liquid. In this way, compared with the existing temperature control scheme of a fixed pressure-temperature for a single tower, the present application suppresses the risk of thermal decomposition of high-boiling solvents through two-stage linkage adjustment of single-tower temperature-pressure and multi-tower coordinated control, which is beneficial to improving the safety and efficiency of the recovery of high-boiling solvent waste liquid. Description of the Drawings

[0010] In order to more clearly illustrate the technical solutions in the embodiments of the present application or the prior art, the following will briefly introduce the drawings required for use in the description of the embodiments or the prior art. Obviously, the drawings in the following description are only some embodiments of the present application. For those of ordinary skill in the art, other drawings can be obtained based on these drawings without creative efforts.

[0011] Figure 1 is a schematic structural diagram of a high-boiling solvent waste liquid recovery system provided by an embodiment of the present application; Figure 2 is a schematic system architecture diagram of a high-boiling solvent waste liquid recovery system provided by an embodiment of the present application; Figure 3 is a schematic structural diagram of a control module provided by an embodiment of the present application; Figure 4 is a schematic structural diagram of a stripping column provided by an embodiment of the present application; Figure 5 is a process flow diagram of high-boiling solvent waste liquid recovery provided by an embodiment of the present application; Figure 6 It is a schematic flow diagram of a temperature adaptive adjustment strategy in a high-boiling solvent waste liquid recovery process provided by an embodiment of the present application; Figure 7 It is a schematic flow diagram of a collaborative temperature control strategy provided by an embodiment of the present application; Figure 8 It is a schematic diagram of functional modules of a temperature adaptive adjustment device in a high-boiling solvent waste liquid recovery process provided by an embodiment of the present application; Figure 9 It is a structural block diagram of an electronic device provided by an embodiment of the present application. Detailed implementation manners

[0012] In order to enable those skilled in the art to better understand the solution of 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 in the embodiments of the present application. Obviously, the described embodiments are only a part of the embodiments of the present application, rather than all the embodiments. Based on the embodiments in the present application, all other embodiments obtained by those of ordinary skill in the art without creative efforts shall fall within the protection scope of the present application.

[0013] The terms "first", "second", etc. in the specification and claims of the present application and the above accompanying drawings are used to distinguish different objects, rather than to describe a specific order. In addition, the terms "include" and "have" and any variations thereof are intended to cover non-exclusive inclusion. For example, a process, method, system, product or device that includes a series of steps or units is not limited to the listed steps or units, but optionally further includes steps or units not listed, or optionally further includes other steps or units inherent to these processes, methods, products or devices.

[0014] Referring to "embodiment" in this text means that a specific feature, structure or characteristic described in connection with the embodiment can be included in at least one embodiment of the present application. The phrase appears in various places in the specification and does not necessarily refer to the same embodiment, nor is it an independent or alternative embodiment mutually exclusive with other embodiments. Those skilled in the art will explicitly and implicitly understand that the embodiments described herein can be combined with other embodiments.

[0015] The "and / or" in the embodiments of the present application describes the association relationship of 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.

[0016] In the embodiments of the present application, the symbol " / " may indicate that the associated objects before and after are in an "or" relationship. Additionally, the symbol " / " may also represent the division sign, that is, for performing division operations. For example, A / B may represent A divided by B.

[0017] The "at least one (item)" or its similar expressions in the embodiments of the present application refer to any combination of these items, including any combination of single item (s) or plural items (s), meaning one or more, and multiple means two or more. For example, at least one (item) of a, b, or c may represent the following seven cases: a, b, c, a and b, a and c, b and c, a, b, and c. Among them, each of a, b, and c can be an element or a set containing one or more elements.

[0018] "Equal to" in the embodiments of the present application can be used in combination with "greater than", applicable to the technical solutions adopted when it is greater than, and can also be used in combination with "less than", applicable to the technical solutions adopted when it is less than. When "equal to" is used in combination with "greater than", it is not used in combination with "less than"; when "equal to" is used in combination with "less than", it is not used in combination with "greater than".

[0019] Traditional high-boiling solvent waste liquid recovery systems generally adopt a fixed pressure-temperature control mode, that is, parameters such as the vacuum degree and heating amount of each tower are preset according to the initial process conditions, lacking a dynamic adjustment mechanism, and when the temperature of a certain tower is abnormal, lacking a linkage adjustment mechanism for pressure and flow, which is likely to lead to the spread of faults.

[0020] To address the above problems, the embodiments of the present application provide a temperature adaptive adjustment strategy and device in a high-boiling solvent waste liquid recovery process. The embodiments of the present application will be introduced in detail below with reference to the accompanying drawings.

[0021] Please refer to Figure 1 , FIG. 1 is a schematic structural diagram of a high-boiling solvent waste liquid recovery system provided by the embodiments of the present application. As shown in FIG. 1, Figure 1 the high-boiling solvent waste liquid recovery system includes a vacuum module 110, a rectification module 120, and a control module 130. Among them, the rectification module 120 includes a plurality of gas-liquid separation towers connected in sequence. The bottom of a single 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 the steam to heat the waste liquid at the bottom of the tower, and the cold water valve is used to control the cold water to condense the gas phase at the top of the tower. The vacuum module 110 is respectively connected to the plurality of gas-liquid separation towers, and the control module 130 is respectively connected to the vacuum module 110, the plurality of steam valves, and the plurality of cold water valves.

[0022] Among them, the vacuum module 110 is used to regulate the vacuum degree in multiple gas-liquid separation towers, so as to inhibit the thermal decomposition rate by reducing the boiling point of the waste liquid in the towers; the rectification module 120 is used to perform multi-stage rectification treatment on the waste liquid in the towers through multiple gas-liquid separation towers to obtain high-purity solvents; the control module 130 is used to, when the absolute value of the difference between the temperature in a single gas-liquid separation tower and the first preset temperature is less than the preset difference, execute the first temperature control strategy 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; and, when the temperature in a single gas-liquid separation tower reaches the second preset temperature, execute the second temperature control strategy 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 first preset temperature is lower than the second preset temperature; execute the cooperative temperature control strategy for 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 temperatures in multiple gas-liquid separation towers during the recovery process of high-boiling-point solvent waste liquid.

[0023] Specifically, please refer to Figure 2 , Figure 2 which is a schematic diagram of the system architecture of a high-boiling-point solvent waste liquid recovery system provided by an embodiment of the present application. As Figure 2 shown, the high-boiling-point solvent waste liquid recovery system includes a concentration module 210, an evaporation module 220, a vacuum module 110, a rectification module 120 and a control module 130. Among them, the rectification module 120 includes a stripping column, a rectification column and a purification column. Each column works together through a reboiler (first reboiler / second reboiler / third reboiler), a condenser (first condenser / second condenser / third condenser), a steam valve, a cold water valve, a reflux valve, etc.

[0024] Among them, the concentration module 210 is used to concentrate the original waste liquid to obtain a first waste liquid with a concentration greater than the first preset concentration, and transmit 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 the second preset concentration; and, transmit the second waste liquid to the bottom of the stripping column for multi-stage rectification treatment.

[0025] Specifically, the multi-stage rectification treatment includes performing the first-stage rectification on the waste liquid in the bottom of the stripping column through the first reboiler and the first condenser corresponding to the stripping column to obtain a first target liquid phase, and transmitting the first target liquid phase to the bottom of the rectification column; and, performing the second-stage rectification on the first target liquid phase in the bottom of the rectification column through the second reboiler and the second condenser corresponding to the rectification column to obtain a second target liquid phase, and transmitting the second target liquid phase to the bottom of the purification column; and, performing the third-stage rectification on the second target liquid phase in the bottom of the purification column through the third reboiler and the third condenser corresponding to the purification column to obtain high-purity solvents.

[0026] Further, for the specific functions of the control module 130, please refer to Figure 3 , Figure 3 which is a schematic structural diagram of a control module provided by an embodiment of the present application. As Figure 3 shown, the control module 130 includes a detection unit 310 and a processing unit 320.

[0027] Among them, the detection unit 310 is responsible for collecting various key data in the high-boiling solvent waste liquid recovery system in real time, mainly including the temperature and pressure information in each gas-liquid separation tower, as well as parameters such as the heating steam flow rate of the reboiler and the cooling water flow rate of the condenser. Through sensors (such as temperature sensors, pressure sensors, flow sensors, etc.) distributed at key positions in the system, these physical quantities are converted into electrical signals or digital signals, providing a data basis for subsequent analysis and decision-making.

[0028] Among them, the processing unit 320 is used to receive the data transmitted by the detection unit 310 and analyze, process, and judge the data using preset algorithms and logical rules. On the one hand, it will compare the collected data with the preset standard parameters to determine whether the system is in a normal operating state; on the other hand, when abnormal data is detected, the processing unit 320 will quickly generate corresponding control instructions according to the established control strategy. For example, when it is detected that the temperature of a certain rectification tower reaches the first preset temperature, the processing unit will calculate the parameter values that need to be adjusted (such as the vacuum degree that the vacuum module should increase, the opening degree that the steam valve should decrease, the flow rate that the cold water valve should increase, etc.), and send these instructions to the relevant execution components in the vacuum module and the rectification module.

[0029] It can be seen that in this embodiment, in the high-boiling solvent waste liquid recovery system, the vacuum module controls the pressure, the rectification module realizes separation, and the control module conducts scheduling. Through the cooperation between modules, precise regulation of parameters such as temperature and pressure during the recovery process of high-boiling solvent waste liquid is achieved, the risk of thermal decomposition is reduced, and the recovery safety and efficiency are improved.

[0030] Next, in combination with Figure 4 the structure of a stripping tower provided by an embodiment of the present application will be described. Figure 4 which is a schematic structural diagram of a stripping tower provided by an embodiment of the present application. Among them, the stripping tower 410 is the core equipment for rectification. The waste liquid material is fed into the tower from the middle; the tower bottom is used to store the bottom liquid and is the source of the circulating liquid in the first reboiler 420. A part of the liquid in the tower bottom is heated and vaporized by the first reboiler 420 and returned to the tower, and the other part can be used as the heavy component for discharging.

[0031] Among them, the first reboiler 420 is used to receive the 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 access 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 transmit the gas phase back into the stripping column 410 through a gas-phase pipeline.

[0032] Among them, the first condenser 430 is used to receive the gas phase located at the top of the column; and, the first condenser 430 is connected to a cold water pipeline through a first cold water valve 431 to access cold water, and the gas phase is condensed into a target liquid phase by the cold water; and, the first condenser 430 is used to transmit the target liquid phase into the first reflux drum 440.

[0033] Among them, the first reflux drum 440 is used to receive the target liquid phase from the first condenser 430; and, the first reflux drum 440 is connected to a reflux pipeline through a first reflux valve 441 to control the reflux amount of the target liquid phase back into the gas-liquid separation column; and, the first reflux drum 440 is used to transmit the target liquid phase that does not participate in the reflux to the next gas-liquid separation column through a pipeline.

[0034] It can be understood that the operating principle of a single gas-liquid separation column is as follows: The high-boiling solvent waste liquid is fed into the middle of the column and enters the bottom of the column. The liquid in the bottom of the column is heated and vaporized by the reboiler, generating a gas phase that rises to the top of the column. The liquid phase part remains in the bottom of the column or is discharged. The gas phase at the top of the column is condensed by the condenser, generating a liquid phase and transmitted to the reflux drum. The liquid phase is partially refluxed through the reflux drum and partially discharged, realizing the gas-liquid separation and purification of the high-boiling solvent waste liquid. This structure ensures the efficient and stable operation of the gas-liquid separation column and meets the requirements of the recovery and rectification of the high-boiling solvent waste liquid.

[0035] Further, based on the structure of a single gas-liquid separation column, analyze the process flow of the entire high-boiling solvent waste liquid recovery system. Please refer to Figure 5 , Figure 5 which is a process flow chart of the recovery of high-boiling solvent waste liquid provided by an embodiment of the present application. As Figure 5 shown, for the specific structure and operating principle of the stripping column 410, refer to the above embodiment. The high-boiling solvent waste liquid recovery system further includes a rectification column 510 and a purification column 550. The structures of the rectification column 510 and the purification column 550 are similar to the structure of the stripping column 410.

[0036] It can be seen that the process flow for the recovery of high-boiling solvent waste liquid is as follows: The waste liquid material containing the high-boiling solvent is fed into the middle of the stripping column 410. The liquid in the column bottom is transmitted through a liquid-phase pipeline to the first reboiler 420. The first reboiler 420 is heated by introducing hot steam under the control of the first steam valve 421. The generated gas phase returns to the stripping column 410 and rises to the top of the column. The gas phase at the top of the column enters the first condenser 430, and after being condensed by introducing cold water through the first cold water valve 431, it enters the first reflux drum 440. A part of the liquid phase in the first reflux drum 440 returns to the stripping column 410 through the first reflux valve 441, and the other part is discharged as a feed into the rectification column 510; and, The liquid in the column bottom of the rectification column 510 is transmitted through a liquid-phase pipeline to the second reboiler 520. The second reboiler 520 is connected to hot steam through the second steam valve 521 to heat the internal liquid phase to generate a gas phase. The gas phase returns to the rectification column 510 and rises to the top of the column. The gas phase at the top of the column passes through the second condenser 530, and after being condensed by introducing cold water through the second cold water valve 531, it enters the second reflux drum 540. A part of the liquid phase in the second reflux drum 540 returns to the rectification column 510 through the second reflux valve 541, and the other part is discharged as a feed into the purification column 550; and, The liquid in the column bottom of the purification column 550 is transmitted through a liquid-phase pipeline to the third reboiler 560. The third reboiler 560 is connected to hot steam through the third steam valve 561 to heat the internal liquid phase to generate a gas phase. The gas phase returns to the purification 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 after being condensed by introducing cold water through the third cold water valve 571, it enters the third reflux drum 580. A part of the liquid phase in the third reflux drum 580 returns through the third reflux valve 581, and the other part is used as the final discharge to obtain a high-purity solvent after rectifying and purifying the high-boiling solvent in the waste liquid.

[0037] Next, in conjunction with Figure 6 a temperature adaptive adjustment strategy in a high-boiling solvent waste liquid recovery process provided by an embodiment of the present application will be described. Figure 6 It is a schematic flow diagram of a temperature adaptive adjustment strategy in a high-boiling solvent waste liquid recovery process provided by an embodiment of the present application, and specifically includes the following steps: Step S610, it is detected that the temperature inside a single gas-liquid separation tower rises.

[0038] Among them, the temperature inside the tower is obtained by a temperature sensor installed inside the gas-liquid separation tower (such as a stripping column, a rectification column, a purification column) to collect the temperature data inside the tower in real time. Once the sensor detects that the temperature value has risen compared with the normal operating range, the subsequent control logic is triggered, providing a basis for the system to respond to temperature anomalies in a timely manner.

[0039] It is understandable that temperature is a key parameter in the recovery rectification process of high-boiling solvent waste liquid. Excessive temperature will cause thermal decomposition of the high-boiling solvent, leading to safety risks and product quality problems. Timely capturing the signal of temperature increase can enable the system to react at the initial stage of abnormality, avoid further temperature out-of-control, and ensure the safety and stability of the rectification process.

[0040] Step S620, when the absolute value of the difference between the temperature in a single gas-liquid separation tower and the first preset temperature is less than the preset difference, execute the first temperature control strategy 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.

[0041] It is understandable that when the actual temperature approaches the first preset temperature and reaches the condition that the absolute value of the difference is less than the preset difference, it indicates that the temperature in the tower begins to deviate from the normal range and enters the warning state, but has not reached the emergency level. For example, if the first preset temperature is 80 °C and the preset difference is 5 °C, when the temperature in the tower is between 75–80 °C, this trigger condition is met.

[0042] In a possible embodiment, the first temperature control strategy is to increase the vacuum degree in the single gas-liquid separation tower through the vacuum module to reduce the tower pressure; and at the same time, reduce the opening degree of the steam valve corresponding to the single gas-liquid separation tower, so that the decrease amplitude of the conveying amount of the hot steam is the first preset amplitude, to reduce the heating load in the reboiler; and at the same time, increase the opening degree of the cold water valve corresponding to the single gas-liquid separation tower, so that the increase amplitude of the cold water flow is the second preset amplitude, to accelerate the condensation of the gas phase at the top of the tower.

[0043] Among them, increasing the vacuum degree in a single gas-liquid separation tower through the vacuum module reduces the tower pressure. According to the relationship between boiling point and pressure, the boiling point of the high-boiling solvent will decrease with the decrease of pressure. Taking DMF as an example, at normal pressure, the boiling point of DMF is about 153 °C. When the vacuum degree is increased and the pressure is reduced, its boiling point can drop significantly. Furthermore, after reducing the boiling point of DMF, at the same temperature, DMF is less likely to undergo thermal decomposition, reducing the generation of decomposition products such as dimethylamine, and reducing safety risks such as explosion. At the same time, it is also beneficial to the gas-liquid separation process.

[0044] Among them, by reducing the opening degree of the steam valve, the conveying amount of the hot steam entering the reboiler is decreased, and the decrease amplitude is the first preset amplitude (such as 10%). The reduction of the hot steam amount reduces the heating power of the reboiler for the waste liquid in the tower bottom, avoiding further increase of the temperature in the tower.

[0045] Among them, by increasing the opening degree of the cold water valve, the cold water flow entering the condenser is increased, and the increase amplitude is the second preset amplitude (such as 20%). Furthermore, more cold water flows through the condenser, enhancing the cooling effect on the gas phase at the top of the tower, contributing to maintaining the gas-liquid balance in the tower and further stabilizing the rectification process.

[0046] It can be seen that in this embodiment, when the absolute value of the difference between the temperature in the tower and the first preset temperature is less than the preset difference, it is in a warning state, and the temperature control strategy is implemented from three aspects: reducing the boiling point, reducing the heat source, and enhancing the cooling, effectively controlling the temperature in the gas-liquid separation tower, and ensuring the safe and stable operation of the high-boiling solvent waste liquid recovery process.

[0047] Step S630, when the temperature in a single gas-liquid separation tower is detected to reach the second preset temperature, execute the second temperature control strategy 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.

[0048] Among them, the first preset temperature is less than the second preset temperature.

[0049] It can be understood that when the temperature in a single gas-liquid separation tower reaches the second preset temperature, the second temperature control strategy is triggered. This indicates that the temperature in the tower has reached a dangerous level, the risk of thermal decomposition of the high-boiling solvent waste liquid has increased sharply, and a large amount of flammable and explosive gases such as dimethylamine may be generated, seriously threatening the safety of equipment and production.

[0050] In a possible embodiment, the second temperature control strategy is to increase the vacuum degree in the single gas-liquid separation tower through the vacuum module to reduce the tower pressure to a preset safe range within a preset time; and, at the same time, close the opening degree of the steam valve corresponding to the single gas-liquid separation tower to cut off the heat source; and, at the same time, fully open the cold water valve corresponding to the single gas-liquid separation tower so that the cold water flow reaches the maximum value.

[0051] Among them, the tower pressure is reduced to the preset safe range through the control of the vacuum module within a preset time (such as 30 seconds). By rapidly reducing the pressure, the boiling point of the high-boiling solvent is greatly reduced, and even at the current relatively high temperature, it can be in a relatively stable state, inhibiting the continuation of the thermal decomposition reaction. Further, a manual emergency control button can also be set. When the system fails, the operator can directly manually start the vacuum module in the control room to control the emergency pressure reduction as the last safety guarantee measure.

[0052] Among them, by closing the opening degree of the steam valve, the heat steam supply of the reboiler is completely cut off, and the heating of the waste liquid in the tower kettle is stopped. By eliminating the source of heat input, the temperature is prevented from rising further, and the intensification of the thermal decomposition reaction is blocked.

[0053] Among them, by fully opening the cold water valve, the cold water flow reaches the maximum value. The cooling capacity of the condenser is greatly enhanced, the gas phase at the top of the tower is quickly cooled, the gas phase at the top of the tower is quickly condensed, a large amount of heat is taken away, the overall temperature in the tower is reduced, and the system is restored to a safe state as soon as possible.

[0054] It can be seen that in this embodiment, the second temperature control strategy is the key means to ensure the safety of the high-boiling solvent waste liquid recovery system in extreme cases. By quickly reducing pressure, cutting off heat, and strongly cooling, the thermal decomposition risk brought by the dangerous temperature can be rapidly contained, and accidents can be avoided.

[0055] Step S640: 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.

[0056] It can be understood that during the recovery process of high-boiling solvent waste liquid, multiple gas-liquid separation towers (stripping towers, rectifying towers, refining towers, etc.) are interrelated and work in coordination. If the temperature of one tower is abnormal, changes in its gas-liquid equilibrium, pressure, material composition, and other states will affect the operation of other towers through the inter-tower connection pipelines and material transfer. For example, if the temperature of the stripping tower is abnormal, resulting in a change in the gas phase composition and a change in the material composition entering the rectifying tower, it may cause temperature fluctuations in the rectifying tower. Therefore, when implementing the temperature control strategy for the abnormal tower, it is necessary to synchronously implement the coordinated temperature control strategy for the remaining towers to maintain the stability of the entire system.

[0057] Please refer to Figure 7 , Figure 7 FIG. is a schematic flowchart of a coordinated temperature control strategy provided by an embodiment of the present application. Among them, in terms of implementing the 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, the above method may further include the following steps: Step S710: Determine a single gas-liquid separation tower with a rising temperature.

[0058] Step S720: Whether the single gas-liquid separation tower is a stripping tower.

[0059] Specifically, if so, execute step S730; if not, execute step S740.

[0060] Step S730: Whether to execute the second temperature control strategy for the stripping tower.

[0061] Specifically, if so, execute step S731.

[0062] Step S731: Execute the first rectifying coordinated temperature control strategy for the rectifying tower and the first refining coordinated temperature control strategy for the refining tower.

[0063] Among them, the stripping tower is the upstream tower of the rectifying tower, and the rectifying tower is the upstream tower of the refining tower.

[0064] In a possible embodiment, the first rectification collaborative temperature control strategy is to synchronously control the vacuum module to increase the vacuum degree in the rectification column according to the decreasing rate of the air pressure in the stripping column, so that the air pressure in the rectification column decreases at the same decreasing rate until the amplitude of the air pressure drop reaches the fifth preset amplitude; and, increase the opening degree of the reflux valve corresponding to the rectification column, so that the increasing amplitude of the reflux ratio of the second target liquid phase is the sixth preset amplitude, in order to reduce the fluctuation of the top temperature of the column.

[0065] Among them, the synchronous pressure reduction of the rectification column can maintain the stability of the pressure gradient between the two columns, avoid the blockage or backflow of gas phase transmission caused by the sudden change of the pressure difference, and ensure the continuity of material transmission. By reducing the pressure, the boiling point of the high-boiling solvent can be reduced, which can reduce the heat load of the rectification column.

[0066] Among them, the reflux liquid, as the cooling medium at the top of the column, can absorb the heat in the gas phase and suppress the fluctuation of the top temperature caused by the pressure reduction. Furthermore, if the pressure reduction of the stripping column increases the gas phase flow rate entering the rectification column, increasing the reflux ratio can stabilize the gas-liquid equilibrium by increasing the liquid phase load, and avoid the decrease of the separation efficiency caused by the overshoot of the gas phase.

[0067] In a possible embodiment, the first refining collaborative temperature control strategy is to stop transferring the second target liquid phase from the rectification column to the refining column; and, increase the opening degree of the cold water valve corresponding to the refining column, so that the cold water flow rate increases, in order to avoid the reduction of the purity of the generated high-purity solvent caused by the gasification of water.

[0068] Among them, due to the implementation of the collaborative temperature control strategy (such as pressure reduction and reflux ratio adjustment) in the current rectification column, the composition of its product fluctuates (such as the temporary increase of the water content). If it continues to be input into the refining column, it may affect the purity of the final product. By pausing the material transfer and isolating the disturbance of the previous stage, the temporary abnormality of the rectification column is avoided from being transmitted to the refining column, ensuring the operation of the refining column under stable working conditions; and, by strengthening the cooling to inhibit the gasification path of water, the separation efficiency of the refining column is maintained, ensuring that the purity of the finally produced high-purity solvent is not interfered by the previous stage operation.

[0069] It should be clear that the embodiments of the present application give specific examples of the collaborative temperature control strategy for other columns when the second temperature control strategy is executed in the stripping column, but the present application does not limit the specific scheme of whether and how to execute the collaborative temperature control strategy for other columns when the first temperature control strategy is executed in the stripping column.

[0070] Step S740, whether a single gas-liquid separation column is a rectification column.

[0071] Specifically, if so, execute step S750; if not, execute step S760.

[0072] Step S750, whether to execute the first temperature control strategy for the rectification column.

[0073] Specifically, if so, execute step S751; if not, execute step S752.

[0074] In step S751, execute the first stripping collaborative temperature control strategy for the stripping column.

[0075] In a possible embodiment, the first stripping collaborative temperature control strategy is to synchronously control the vacuum module to increase the vacuum degree in the stripping column according to the decreasing rate of the air pressure in the rectification column, so that the air pressure in the stripping column decreases at the same decreasing rate.

[0076] It can be understood that when the rectification column reduces pressure (such as executing the first temperature control strategy), the decrease of its internal air pressure will break the upstream and downstream pressure balance. If the air pressure of the stripping column does not decrease synchronously, a pressure difference from the stripping column to the rectification column may be formed, resulting in the liquid in the bottom of the stripping column flowing into the rectification column due to the pressure difference; and, by synchronizing the pressure reduction rate, the air pressure difference between the stripping column and the rectification column is maintained stable (or close to the original difference), avoiding backflow caused by pressure imbalance.

[0077] In step S752, determine whether to execute the second temperature control strategy for the rectification column.

[0078] Specifically, if so, execute step S753.

[0079] In step S753, execute the second stripping collaborative temperature control strategy for the stripping column and the second refining collaborative temperature control strategy for the refining column.

[0080] It can be understood that when the rectification column executes the second temperature control strategy (such as rapid pressure reduction, closing the steam valve), its operating state will change violently, and the parameters of the upstream stripping column and the downstream refining column need to be adjusted synchronously to prevent the stripping column from losing balance in gas-liquid transmission due to the sudden pressure drop of the rectification column, and to avoid material accumulation or purity fluctuation in the refining column caused by interrupted feeding or heat imbalance.

[0081] In a possible embodiment, the second stripping collaborative temperature control strategy is to synchronously control the vacuum module to increase the vacuum degree in the stripping column according to the decreasing rate of the air pressure in the rectification column, so that the air pressure in the stripping column decreases at the same decreasing rate; and, reduce the opening degree of the steam valve corresponding to the stripping column, so that the decrease amplitude of the hot steam delivery volume is the third preset amplitude, to prevent the reboiler from heating to generate excessive gas phase.

[0082] Among them, according to the decreasing rate of the rectification column air pressure, synchronously increasing the vacuum degree of the stripping column to make the air pressure decrease rates of the two the same is beneficial to maintaining the stability of the pressure gradient between the stripping column and the rectification column.

[0083] Among them, when the rectification column executes the second temperature control strategy (such as closing the steam valve), its processing capacity decreases. If the stripping column continues to generate a large amount of gas, it will cause the gas phase load of the rectification column to be overloaded (even if the vacuum degree decreases, excessive gas volume may still cause flooding or temperature runaway), and then reducing the steam input can avoid the rectification column from being unable to handle due to excessive intake air volume.

[0084] In a possible embodiment, the second refining collaborative temperature control strategy is to stop transferring the second target liquid phase from the rectification 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 in the refining column; and, increase the opening degree of the cold water valve corresponding to the refining column, so that the increased amplitude of the cold water flow rate is the seventh preset amplitude to reduce the pressure fluctuation in the column.

[0085] Among them, when the rectification column executes the emergency strategy, the purity of its product may fluctuate (such as insufficient separation due to rapid pressure reduction). At this time, continuing to feed will contaminate the high-purity material in the refining column.

[0086] Among them, maximizing the reflux ratio can enhance the mass transfer efficiency in the column. Even if there is no feed temporarily, the concentration distribution in the column can be kept stable through internal circulation, avoiding water vaporization (accumulation of water may evaporate due to heat imbalance, reducing the product purity).

[0087] Among them, after the refining column stops feeding, the heat in the column mainly comes from the reboiler (if not closed) or the residual heat of vaporization. Increasing the cooling can quickly remove the heat and inhibit the pressure rise caused by temperature fluctuation (such as additional gas phase generated by water vaporization).

[0088] Step S760, regarding whether the refining column executes the first temperature control strategy or the second temperature control strategy.

[0089] Specifically, if so, execute step S761.

[0090] Step S761, execute the third stripping collaborative temperature control strategy for the stripping column.

[0091] In a possible embodiment, the third stripping collaborative temperature control strategy is to synchronously control the vacuum module to increase the vacuum degree in the stripping column according to the decreasing rate of the air pressure in the refining column, so that the air pressure in the stripping column decreases at the same decreasing rate; and, reduce the opening degree of the steam valve corresponding to the stripping column, so that the delivery volume of the hot steam decreases by the fourth preset amplitude to prevent the reboiler from heating to generate excessive gas phase.

[0092] It is understandable that when the temperature in the refining tower rises abnormally, the third stripping coordinated temperature control strategy is only executed for the stripping tower. This is because the stripping tower is the upstream tower of the rectifying tower. Regulating the stripping tower can indirectly control the material / heat entering the refining tower and relieve the pressure of the refining tower.

[0093] Among them, synchronously reducing the gas pressure can maintain the stability of the pressure gradient between the two, which can avoid the backflow of materials or transportation obstruction caused by pressure difference. In addition, by reducing the hot steam delivery volume, the distillation products of the distillation tower can be reduced from the source, and then the materials entering the refining tower can be indirectly reduced. By directly reducing the temperature drive of the upstream tower, the temperature rise pressure of the refining tower can be fundamentally alleviated.

[0094] It can be seen that in this embodiment, the coordinated temperature control strategy realizes the coordinated adjustment of parameters among multiple towers by monitoring the temperature and pressure changes of each gas-liquid separation tower, and controlling the vacuum module, steam valve, cold water valve and other equipment in a linked manner. When the temperature of a tower is abnormal, not only the temperature control strategy is implemented in a targeted manner, but also the vacuum degree, heat input and cooling intensity of the upstream and downstream towers are adjusted synchronously to avoid system chain reactions caused by local abnormalities, effectively prevent problems such as material backflow and gas phase overload, maintain the stability of the system pressure gradient, material balance and heat balance, ensure the safe and stable operation of the high-boiling point solvent waste liquid recovery process, and improve product purity and system operation efficiency.

[0095] The above mainly introduces the scheme of the embodiment of the present application from the perspective of the execution process on the method side. It is understandable that in order to realize the above functions, the mobile electronic device includes a hardware structure and / or software module corresponding to the execution of each function. Those skilled in the art should easily realize that, in combination with the units and algorithm steps of each example described in the embodiment provided in this article, the present application can be implemented in the form of hardware or a combination of hardware and computer software. Whether a function is executed in the form of hardware or computer software driving hardware depends on the specific application and design constraints of the technical solution. Professional and technical personnel can use different methods to implement the described functions for each specific application, but such implementation should not be considered to be beyond the scope of this application.

[0096] The embodiment of the present application can divide the electronic device into functional units according to the above method example. For example, each functional unit can be divided according to each function, or two or more functions can be integrated into one processing unit. The above integrated unit can be implemented in the form of hardware or in the form of software functional units. It should be noted that the division of units in the embodiment of the present application is schematic and is only a logical function division. There may be other division methods in actual implementation.

[0097] See also Figure 8 , Figure 8Schematic diagram of the functional modules of a temperature adaptive regulation device in a high-boiling solvent waste liquid recovery process provided by an embodiment of the present application, as Figure 8 shown. The device includes the following units: The first processing unit 810 is configured to, when the absolute value of the difference between the temperature in the single gas-liquid separation tower and the first preset temperature is 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 and the cold water valve corresponding to the single gas-liquid separation tower; and, when the temperature in the single gas-liquid separation tower reaches the second preset temperature, execute a second temperature control strategy 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, where the first preset temperature is lower than the second preset temperature; The second processing unit 820 is configured 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, so as to achieve the linkage control of the temperatures in the multiple gas-liquid separation towers during the high-boiling solvent waste liquid recovery process.

[0098] It can be seen that in this embodiment, for a single tower with abnormal temperature, different control strategies are executed based on the specific temperature value. At the same time, for the remaining multiple towers, a coordinated control strategy is executed. When the upstream tower reduces pressure, the downstream tower adjusts the pressure proportionally; when the downstream tower is abnormal, the upstream tower reduces the load input, so as to achieve the linkage control of multiple towers under abnormal temperature, which is beneficial to improving the safety and efficiency of high-boiling solvent waste liquid recovery.

[0099] In one embodiment, before the absolute value of the difference between the temperature in the single gas-liquid separation tower and the first preset temperature is detected to be less than the preset difference, the first processing unit 810 is further configured to: detect that the temperature in the single gas-liquid separation tower rises.

[0100] In one embodiment, in terms of executing the first temperature control strategy 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 first processing unit 810 is specifically configured to: increase the vacuum degree in the single gas-liquid separation tower through the vacuum module to reduce the tower internal pressure; and, at the same time, reduce the opening degree of the steam valve corresponding to the single gas-liquid separation tower, so that the reduction amplitude of the hot steam delivery volume is a first preset amplitude, to reduce the heating load in the reboiler; and, at the same time, increase the opening degree of the cold water valve corresponding to the single gas-liquid separation tower, so that the increase amplitude of the cold water flow rate is a second preset amplitude, to accelerate the condensation of the gas phase at the tower top.

[0101] In one embodiment, in terms of the second temperature control strategy being executed for the single gas-liquid separation column based on the vacuum module, the steam valve and the cold water valve corresponding to the single gas-liquid separation column, the first processing unit 810 is specifically configured to: increase the vacuum degree in the single gas-liquid separation column through the vacuum module to reduce the tower internal pressure to a preset safe range within a preset time; and, simultaneously close the opening degree of the steam valve corresponding to the single gas-liquid separation column to cut off the heat source; and, simultaneously fully open the cold water valve corresponding to the single gas-liquid separation column so that the cold water flow rate reaches the maximum value.

[0102] In one embodiment, in terms of the coordinated temperature control strategy being executed for the remaining multiple gas-liquid separation columns 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 executed for the stripping column, then synchronously execute the first rectification coordinated temperature control strategy for the rectification column and the first purification coordinated temperature control strategy for the purification column; if the first temperature control strategy is executed for the rectification column, then synchronously execute the first stripping coordinated temperature control strategy for the stripping column; and, if the second temperature control strategy is executed for the rectification column, then synchronously execute the second stripping coordinated temperature control strategy for the stripping column and the second purification coordinated temperature control strategy for the purification column; if the first temperature control strategy or the second temperature control strategy is executed for the purification column, then synchronously execute the third stripping coordinated temperature control strategy for the stripping column.

[0103] In one embodiment, in terms of the first stripping coordinated temperature control strategy being executed for the stripping column, the second processing unit 820 is specifically configured to: synchronously control the vacuum module to increase the vacuum degree in the stripping column according to the decreasing rate of the internal pressure in the rectification column so that the internal pressure in the stripping column decreases at the same decreasing rate.

[0104] In one embodiment, in terms of the second stripping coordinated temperature control strategy being executed for the stripping column, the second processing unit 820 is specifically configured to: synchronously control the vacuum module to increase the vacuum degree in the stripping column according to the decreasing rate of the internal pressure in the rectification column so that the internal pressure in the stripping column decreases at the same decreasing rate; and, reduce the opening degree of the steam valve corresponding to the stripping column so that the decreasing amplitude of the hot steam delivery amount is the third preset amplitude to prevent excessive gas phase generation by the reboiler heating.

[0105] In one embodiment, for the aspect of implementing the third stripping collaborative 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 degree in the stripping column according to the decreasing rate of the air pressure in the rectifying column, so that the air pressure in the stripping column decreases at the same decreasing rate; and, reduce the opening degree of the steam valve corresponding to the stripping column, so that the decreased amplitude of the conveying amount of the hot steam is a fourth preset amplitude, to prevent excessive gas phase generated by the reboiler heating.

[0106] In one embodiment, for the aspect of implementing the first rectification collaborative temperature control strategy for the rectifying column, the second processing unit 820 is specifically configured to: synchronously control the vacuum module to increase the vacuum degree in the rectifying column according to the decreasing rate of the air pressure in the stripping column, so that the air pressure in the rectifying column decreases at the same decreasing rate until the decreased amplitude of the air pressure reaches a fifth preset amplitude; and, increase the opening degree of the reflux valve corresponding to the rectifying column, so that the increased amplitude of the reflux ratio of the second target liquid phase is a sixth preset amplitude, to reduce the temperature fluctuation at the top of the column.

[0107] In one embodiment, for the aspect of implementing the first refining collaborative temperature control strategy for the refining column, the second processing unit 820 is specifically configured to: stop transferring the second target liquid phase from the rectifying column to the refining column; and, increase the opening degree of the cold water valve corresponding to the refining column, so that the cold water flow rate increases, to avoid the reduction of the purity of the generated high-purity solvent caused by the gasification of water.

[0108] In one embodiment, for the aspect of implementing the second refining collaborative temperature control strategy for the refining column, the second processing unit 820 is specifically configured to: stop transferring the second target liquid phase from the rectifying column to the refining column; and, fully open the reflux valve corresponding to the refining column, so that the generated high-purity solvent in the refining column can be continuously transferred back into the refining column, to maintain the material balance in the refining column; and, increase the opening degree of the cold water valve corresponding to the refining column, so that the increased amplitude of the cold water flow rate is a seventh preset amplitude, to reduce the pressure fluctuation in the column.

[0109] Figure 9 is a structural block diagram of an electronic device provided by the present application. As Figure 9 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, where the memory 902 may store one or more computer programs, and one or more computer programs may be configured to be executed by one or more processors 901 to implement the methods described in the above examples. Among them, the electronic device 900 may be the terminal device in the above high-boiling solvent waste liquid recovery system.

[0110] The processor 901 may include one or more processing cores. The processor 901 connects various parts within the entire electronic device 900 using various interfaces and circuits. By running or executing instructions, programs, code sets, or instruction sets stored in the memory 902, and by invoking the data stored in the memory 902, it performs various functions of the electronic device 900 and processes data. Optionally, the processor 901 may be implemented in at least one hardware form of digital signal processing (DSP), field-programmable gate array (FPGA), or programmable logic array (PLA). The processor 901 may integrate a combination of one or several of a central processing unit (CPU), a graphics processing unit (GPU), and a modem, etc. It can be understood that the above-mentioned modem may not be integrated into the processor 901 and may be implemented separately through a communication chip.

[0111] The memory 902 may include random access memory (RAM) and may also include read-only memory (ROM). The memory 902 is 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. Among them, the program storage area may store instructions for implementing an operating system, instructions for implementing at least one function (such as a touch function, a sound playback function, an image playback function, etc.), instructions for implementing each of the above method examples, etc. The data storage area may also store data created during the use of the electronic device 900.

[0112] It can be understood that the electronic device 900 may include more or fewer structural elements than those in the above structural block diagram. For example, it includes a power module, physical buttons, a WiFi (Wireless Fidelity) module, a speaker, a Bluetooth module, sensors, etc., which are not limited herein.

[0113] The embodiments of this application also provide a computer storage medium, on which computer programs / instructions are stored. When the computer programs / instructions are executed by a processor, they implement part or all of the steps of any of the methods described in the above method embodiments.

[0114] The embodiments of the present application further provide a computer program product. The computer program product includes a non-transitory computer-readable storage medium storing a computer program. The computer program is operable to cause a computer to execute some or all of the steps of any one of the methods described in the above method embodiments.

[0115] It should be understood that in various embodiments of the present application, the order numbers of the above processes do not mean the order of execution. The execution order of each process should be determined according to its function and internal logic, and should not constitute any limitation to the implementation process of the embodiments of the present application.

[0116] In several embodiments provided by the present application, it should be understood that the disclosed methods, devices and systems can be implemented in other ways. For example, the device embodiments described above are only illustrative; for example, the division of units is only a logical function division, and there may be other division methods in actual implementation; for example, multiple units or components can be combined or integrated into another system, or some features can be ignored or not executed. Another point, the displayed or discussed mutual coupling or direct coupling or communication connection can be through some interfaces, and the indirect coupling or communication connection of devices or units can be in electrical, mechanical or other forms.

[0117] The units described as separate components may or may not be physically separated, and the components displayed as units may or may not be physical units, that is, they may be located in one place, or may be distributed to multiple network units. Some or all of the units can be selected according to actual needs to achieve the purpose of the solution of this embodiment.

[0118] In addition, in each embodiment of the present invention, the functional units can be integrated in a processing unit, or each unit can be physically included separately, or two or more units can be integrated in one unit. The above integrated unit can be implemented in the form of hardware, or in the form of hardware plus software functional units.

[0119] The integrated unit implemented in the form of software functional units can be stored in a computer-readable storage medium. The above-mentioned software functional units are stored in a storage medium and include several instructions for causing a computer device (which may be a personal computer, a server, or a network device, etc.) to execute some steps of the methods of various embodiments of the present invention. The foregoing storage medium includes: USB flash drive, mobile hard disk, magnetic disk, optical disk, volatile memory or non-volatile memory. Among them, the non-volatile memory may 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 may 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 (DDR SDRAM), enhanced synchronous dynamic random access memory (ESDRAM), synchronous link dynamic random access memory (SLDRAM), and direct rambus random access memory (DRRAM), etc., all of which are media that can store program code.

[0120] Although the present invention is disclosed as above, the present invention is not limited thereto. Any person skilled in the art can easily think of changes or substitutions without departing from the spirit and scope of the present invention, and can make various changes and modifications, including combinations of the above different functions and implementation steps, including software and hardware implementation manners, all within the protection scope of the present invention.

Claims

1. A temperature adaptive regulation strategy in a high boiling point solvent waste liquid recovery process, characterized in that Applied to a high-boiling solvent waste liquid recovery system, the system includes a vacuum module, a rectification module, and a control module. The rectification module includes a plurality of gas-liquid separation towers connected in sequence. The bottom of a single gas-liquid separation tower is connected to a steam valve, and the top of the tower is connected to a cold water valve. The steam valve is used to control the steam to heat the waste liquid at the bottom of the tower. The waste liquid contains the high-boiling solvent. The cold water valve is used to control the cold water to condense the gas phase at the top of the tower. The vacuum module is respectively connected to the plurality of gas-liquid separation towers, and the control module is respectively connected to the vacuum module, a plurality of steam valves, and a plurality of cold water valves; wherein, The vacuum module is used to regulate the vacuum degree in the plurality of gas-liquid separation towers to inhibit the thermal decomposition rate by reducing the boiling point of the waste liquid in the tower; The rectification module is used to perform multi-stage rectification treatment on the waste liquid in the tower through the plurality of gas-liquid separation towers to obtain a high-purity solvent; The control module is used to, when the absolute value of the difference between the temperature in the single gas-liquid separation tower and the first preset temperature is 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 and the cold water valve corresponding to the single gas-liquid separation tower; and, When it is detected that the temperature in the single gas-liquid separation tower reaches the second preset temperature, execute a second temperature control strategy 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, and the first preset temperature is lower than the second preset temperature; Execute 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 to achieve the linkage control of the temperature in the plurality of gas-liquid separation towers during the recovery process of the high-boiling solvent waste liquid.

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

3. The strategy according to claim 2, wherein The multiple gas-liquid separation towers include a stripping column, a rectifying column, and a refining column connected in sequence; the multi-stage rectification process includes performing a first-stage rectification on the waste liquid in the stripping column bottom through the first reboiler and the first condenser corresponding to the stripping column to obtain a first target liquid phase, and transferring the first target liquid phase to the rectifying column bottom; And, performing a second-stage rectification on the first target liquid phase in the rectifying column bottom through the second reboiler and the second condenser corresponding to the rectifying column to obtain a second target liquid phase, and transferring the second target liquid phase to the refining column bottom; And, performing a third-stage rectification on the second target liquid phase in the refining column bottom through the third reboiler and the third condenser corresponding to the refining column to obtain the high-purity solvent, which is the product obtained by rectifying and purifying the high-boiling solvent in the waste liquid.

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

5. The strategy according to claim 2, characterized in that, The first temperature control strategy is to increase the vacuum degree in the single gas-liquid separation tower through the vacuum module to reduce the tower internal pressure; and, at the same time, reduce the opening degree of the steam valve corresponding to the single gas-liquid separation tower, so that the decrease amplitude of the hot steam delivery volume is the first preset amplitude to reduce the heating load in the reboiler; and, at the same time, increase the opening degree of the cold water valve corresponding to the single gas-liquid separation tower, so that the increase amplitude of the cold water flow rate is the second preset amplitude to accelerate the condensation of the gas phase at the top of the tower; The second temperature control strategy is to increase the vacuum degree in the single gas-liquid separation tower through the vacuum module to reduce the tower internal pressure to the preset safe range within a preset time; and, at the same time, close the opening degree of the steam valve corresponding to the single gas-liquid separation tower to cut off the heat source; And, at the same time, fully open the cold water valve corresponding to the single gas-liquid separation tower so that the cold water flow rate reaches the maximum value.

6. The strategy according to claim 3, wherein The control module is used to execute a cooperative temperature control strategy for the remaining multiple gas-liquid separation towers according to the first temperature control strategy or the second temperature control strategy, specifically including: If the second temperature control strategy is executed for the stripping column, then the first rectification cooperative temperature control strategy is synchronously executed for the rectifying column, and the first refining cooperative temperature control strategy is executed for the refining column; If the first temperature control strategy is executed for the rectifying column, then the first stripping cooperative temperature control strategy is synchronously executed for the stripping column; and, if the second temperature control strategy is executed for the rectifying column, then the second stripping cooperative temperature control strategy is synchronously executed for the stripping column, and the second refining cooperative temperature control strategy is executed for the refining column; If the first temperature control strategy or the second temperature control strategy is executed for the refining column, then a third stripping collaborative temperature control strategy is synchronously executed for the stripping column.

7. The strategy according to claim 6, wherein The first stripping collaborative temperature control strategy is to synchronously control the vacuum module to increase the vacuum degree in the stripping column according to the decreasing rate of the air pressure in the rectifying column, so that the air pressure in the stripping column decreases at the same decreasing rate; The second stripping collaborative temperature control strategy is to synchronously control the vacuum module to increase the vacuum degree in the stripping column according to the decreasing rate of the air pressure in the rectifying column, so that the air pressure in the stripping column decreases at the same decreasing rate; and, reduce the opening degree of the steam valve corresponding to the stripping column, so that the decreasing amplitude of the conveying amount of the hot steam is a third preset amplitude, to prevent excessive gas phase generated by the reboiler heating; The third stripping collaborative temperature control strategy is to synchronously control the vacuum module to increase the vacuum degree in the stripping column according to the decreasing rate of the air pressure in the refining column, so that the air pressure in the stripping column decreases at the same decreasing rate; and, reduce the opening degree of the steam valve corresponding to the stripping column, so that the decreasing amplitude of the conveying amount of the hot steam is a fourth preset amplitude, to prevent excessive gas phase generated by the reboiler heating.

8. The strategy according to claim 6, wherein The first rectifying collaborative temperature control strategy is to synchronously control the vacuum module to increase the vacuum degree in the rectifying column according to the decreasing rate of the air pressure in the stripping column, so that the air pressure in the rectifying column decreases at the same decreasing rate until the decreasing amplitude of the air pressure reaches a fifth preset amplitude; and, increase the opening degree of the reflux valve corresponding to the rectifying column, so that the increasing amplitude of the reflux ratio of the second target liquid phase is a sixth preset amplitude, to reduce the temperature fluctuation at the top of the column.

9. The strategy according to claim 7, wherein The first refining collaborative temperature control strategy is to stop transferring the second target liquid phase from the rectifying column to the refining column; and, increase the opening degree of the cold water valve corresponding to the refining column, so that the cold water flow increases, to avoid the reduction of the purity of the generated high-purity solvent caused by the gasification of water; The second refining collaborative temperature control strategy is to stop transferring the second target liquid phase from the rectifying column to the refining column; and, fully open the reflux valve corresponding to the refining column, so that the generated high-purity solvent in the refining column can be continuously transferred back into the refining column, to maintain the material balance in the refining column; and, increase the opening degree of the cold water valve corresponding to the refining column, so that the increasing amplitude of the cold water flow is a seventh preset amplitude, to reduce the pressure fluctuation in the column.

10. A temperature adaptive adjustment device in a high-boiling solvent waste liquid recovery process, characterized in that, Applied to a high-boiling solvent waste liquid recovery system, the system includes a vacuum module, a rectifying module and a control module. The rectifying module includes a plurality of gas-liquid separation columns connected in sequence. The bottom of a single gas-liquid separation column is connected to a steam valve, and the top is connected to a cold water valve. The steam valve is used to control the steam to heat the waste liquid at the bottom of the column. The waste liquid contains the high-boiling solvent. The cold water valve is used to control the cold water to condense the gas phase at the top of the column. The vacuum module is respectively connected to the plurality of gas-liquid separation columns. The control module is respectively connected to the vacuum module, a plurality of steam valves and a plurality of cold water valves; The device includes: A first processing unit, configured to, when the absolute value of the difference between the temperature in the single gas-liquid separation tower and a first preset temperature is 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 and the cold water valve corresponding to the single gas-liquid separation tower; and, when the temperature in the single gas-liquid separation tower reaches 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 and the cold water valve corresponding to the single gas-liquid separation tower, wherein the first preset temperature is lower than the second preset temperature; A second processing unit, configured to execute a cooperative temperature control strategy 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 the linkage control of the temperatures in the multiple gas-liquid separation towers during the recovery process of the high-boiling solvent waste liquid.

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