Recycled waste liquid separation and dehydration system

Abstract

The utility model discloses a separation and dehydration system for recycled waste liquid. An evaporator is configured to evaporate and vaporize a flowing organic solvent; a gas inlet of the supergravity rectification bed is connected with a gas outlet of the evaporator through a pipeline, and a liquid outlet of the supergravity rectification bed is connected with a first liquid inlet of the evaporator through a pipeline; one end of the circulating pipeline D is connected with a gas outlet of the supergravity rectification bed, the other end of the circulating pipeline D is connected with a reflux inlet of the supergravity rectification bed, and a first condenser and an acid value instrument are arranged on the circulating pipeline; the membrane assembly is connected with a gas outlet of the supergravity rectification bed through a first pipeline, a fourth control valve is arranged on the first pipeline, and the membrane assembly is configured to dehydrate a solvent flowing through the membrane assembly to obtain a finished product organic solvent; and the feeding pipe group is configured to convey recovered waste liquid to the evaporator or the supergravity rectification bed. According to the scheme, the product precision and the processing efficiency can be improved, and the operation cost and system energy consumption are reduced.

Description

Technical Field

[0001] This utility model relates to the field of waste liquid treatment technology, and in particular to a waste liquid recycling, separation and dehydration system. Background Technology

[0002] The recovered organic solvents have high acid values ​​and water content, making them unsuitable for recycling as production raw materials. While some related technologies utilize high-gravity distillation beds combined with membrane separation to separate and dehydrate the recovered organic solvents, these methods suffer from low automation, require frequent manual sampling and testing, and rely heavily on human experience. This results in substandard separation and dehydration products with poor precision, stability, and efficiency.

[0003] The information disclosed in this background section is only intended to enhance the understanding of the background technology of this application, and therefore may include prior art that is not known to those skilled in the art. Summary of the Invention

[0004] In response to the problems pointed out in the background art, this utility model proposes a waste liquid recycling separation and dehydration system to improve product accuracy and processing efficiency, and reduce operating costs and system energy consumption.

[0005] To achieve the above-mentioned objectives, the present invention employs the following technical solution:

[0006] In some embodiments of this application, a waste liquid separation and dehydration system is provided, comprising:

[0007] An evaporator is configured to evaporate and vaporize the flowing organic solvent;

[0008] A supergravity distillation bed, wherein the gas inlet of the supergravity distillation bed is connected to the gas outlet of the evaporator via a pipeline, and the liquid outlet of the supergravity distillation bed is connected to the first liquid inlet of the evaporator via a pipeline;

[0009] The circulation pipeline is connected at one end to the gas outlet of the supergravity distillation bed and at the other end to the reflux port of the supergravity distillation bed. A first condenser and an acid value meter are installed on the circulation pipeline.

[0010] The membrane module is connected to the gas outlet of the supergravity distillation bed via a first pipeline. A fourth control valve is provided on the first pipeline. The membrane module is configured to dehydrate the flowing solvent to obtain the finished organic solvent.

[0011] The feed pipe assembly is configured to deliver recycled waste liquid to the evaporator or the high-gravity distillation bed.

[0012] In some embodiments of this application, the feed pipe assembly includes a first feed pipe, which is connected to the second liquid inlet of the evaporator, and a first control valve is provided on the first feed pipe.

[0013] The feed pipe assembly includes a second feed pipe, which is connected to the liquid inlet of the supergravity distillation bed, and a second control valve is provided on the second feed pipe.

[0014] In some embodiments of this application, the second feed pipe includes a second feed pipe I, a second control valve I is provided on the second feed pipe I, and the second feed pipe I is connected to the lower part of the supergravity distillation bed;

[0015] The second feed pipe includes a second feed pipe II, and a second control valve II is provided on the second feed pipe II. The second feed pipe II is connected to the middle part of the supergravity distillation bed.

[0016] In some embodiments of this application, a balancing pump is provided on the pipeline between the liquid outlet of the supergravity distillation bed and the first liquid inlet of the evaporator.

[0017] In some embodiments of this application, a reflux tank and a reflux pump are also provided on the circulation pipeline.

[0018] In some embodiments of this application, a superheater is provided on the first pipeline between the membrane module and the gas outlet of the supergravity distillation bed.

[0019] In some embodiments of this application, the liquid phase gas outlet of the membrane module is connected to a second pipeline, and the second pipeline is provided with a second condenser, a regeneration solvent tank and a product pump.

[0020] In some embodiments of this application, a moisture meter is also provided on the second pipeline.

[0021] In some embodiments of this application, the aqueous gas outlet of the membrane module is connected to a third pipeline, and the third pipeline is equipped with a third condenser, a vacuum buffer tank, and a wastewater pump.

[0022] In some embodiments of this application, the waste liquid outlet of the evaporator is connected to a waste liquid pump via a pipeline.

[0023] Compared with the prior art, the advantages and positive effects of this utility model are:

[0024] This system automatically monitors the acid value of the solvent online in real time and uses a feedback mechanism to automatically optimize the operating parameters of the system, thereby improving the system's operating efficiency.

[0025] This system automatically monitors the acid value and moisture content of the solvent online in real time, enabling fully automated operation of the entire process, ensuring stable operation, and reducing manual labor costs.

[0026] Based on the different acid values ​​of the recovered solvent, the control system automatically adjusts the feed position, shortens the operation time to reach the standard, and saves energy.

[0027] This system automatically monitors the acid value of the solvent online in real time, controls the system to automatically adjust the reflux ratio, optimize operating parameters, and improve operating efficiency.

[0028] This system links the power supply load of the supergravity system with the power of the balancing pump to ensure the continuous and stable operation of the supergravity distillation bed;

[0029] This system operates fully automatically, reducing human error and saving labor costs.

[0030] The system has simple and easy-to-operate processes and meets the requirements for the recycling of raw materials in the production line.

[0031] Other features and advantages of this utility model will become clearer after reading the detailed embodiments of this utility model in conjunction with the accompanying drawings. Attached Figure Description

[0032] To more clearly illustrate the technical solutions in the embodiments of this utility model or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0033] Figure 1 This is a schematic diagram of a waste liquid separation and dehydration system according to some embodiments.

[0034] Figure label:

[0035] 610. Feed pipe assembly; 611. First feed pipe; 612. Second feed pipe; 613. First control valve; 614. Second control valve; 615. Solvent pump;

[0036] 620. Evaporator; 621. Waste liquid pump; 622. Balancing pump;

[0037] 630. Ultragravity distillation bed;

[0038] 640. Circulation piping; 641. First condenser; 642. Acid value meter; 643. Reflux tank; 644. Reflux pump;

[0039] 650. Membrane module;

[0040] 660. First pipeline; 661. Fourth control valve; 662. Superheater;

[0041] 670. Second piping; 671. Second condenser; 672. Regenerated solvent tank; 673. Moisture meter; 674. Product pump;

[0042] 680. Third pipeline; 681. Third condenser; 682. Vacuum buffer tank; 683. Vacuum pump; 684. Wastewater pump. Detailed Implementation

[0043] The technical solutions of the embodiments of this application will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of this application, and not all embodiments. Based on the embodiments of this application, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this application.

[0044] In the description of this application, it should be understood that the terms "center", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are only for the convenience of describing this application and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this application.

[0045] The terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Therefore, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of this application, unless otherwise stated, "a plurality of" means two or more.

[0046] In the description of this application, it should be noted that, unless otherwise expressly specified and limited, the terms "installation," "connection," and "linking" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection between two components. Those skilled in the art can understand the specific meaning of the above terms in this application based on the specific circumstances.

[0047] In this invention, unless otherwise explicitly specified and limited, "above" or "below" the second feature can include direct contact between the first and second features, or contact between the first and second features through another feature between them. Furthermore, "above," "over," and "on top" of the second feature includes the first feature directly above or diagonally above the second feature, or simply indicates that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" the second feature includes the first feature directly below or diagonally below the second feature, or simply indicates that the first feature is at a lower horizontal level than the second feature.

[0048] The following disclosure provides many different embodiments or examples for implementing various structures of this invention. To simplify the disclosure, specific examples of components and arrangements are described below. These are merely examples and are not intended to limit the scope of the invention. Furthermore, reference numerals and / or letters may be repeated in different examples; such repetition is for simplification and clarity and does not in itself indicate a relationship between the various embodiments and / or arrangements discussed. In addition, examples of various specific processes and materials are provided in this invention, but those skilled in the art will recognize the application of other processes and / or the use of other materials.

[0049] In some embodiments of this application, a waste liquid separation and dehydration system is provided, referring to... Figure 1 It includes an evaporator 620, which is configured to evaporate and vaporize the flowing organic solvent.

[0050] The waste liquid recovery separation and dehydration system also includes a supergravity distillation bed 630, the gas inlet of which is connected to the gas outlet of the evaporator 620 via a pipeline, and the liquid outlet of which is connected to the first liquid inlet of the evaporator 620 via a pipeline.

[0051] The waste liquid recovery separation and dehydration system also includes a circulation pipeline 640, one end of which is connected to the gas outlet of the supergravity distillation bed 630, and the other end of which is connected to the reflux port of the supergravity distillation bed 630.

[0052] A first condenser 641 and an acid value meter 642 are installed on the circulation pipeline 640. The acid value meter 642 is located downstream of the first condenser 641 along the flow direction of the fluid in the circulation pipeline 640.

[0053] A return pump 644 is also installed on the circulation pipeline 640 to provide the power for fluid flow.

[0054] The waste liquid recovery and dehydration system also includes a membrane module 650, for example, a pervaporation membrane. The membrane module 650 is connected to the gas outlet of the supergravity distillation bed 630 via a first pipeline 660, on which a fourth control valve 661 is provided. The membrane module 650 is configured to dehydrate the flowing solvent to obtain the finished organic solvent.

[0055] The waste liquid recovery separation and dehydration system also includes a feed pipe assembly 610, which is configured to deliver the recovered solvent to the evaporator 620 or the high gravity distillation bed 630.

[0056] Specifically, after the waste liquid separation and dehydration system is started, the waste liquid is fed into the evaporator 620 through the feed pipe group 610. When the liquid level in the evaporator 620 reaches the set value, the feed pipe group 610 stops feeding the waste liquid into the evaporator 620.

[0057] Evaporator 620 evaporates and vaporizes the recycled waste liquid inside it;

[0058] The gas inside the evaporator 620 flows out from the gas outlet of the evaporator 620 and flows into the supergravity distillation bed 630 through the gas inlet of the supergravity distillation bed 630. The gas enters the bottom of the supergravity distillation bed 630 and is separated by the supergravity distillation bed 630 to obtain light component gas and heavy component liquid.

[0059] The light component gas flows out from the gas outlet of the supergravity distillation bed 630 and enters the circulation pipeline 640. After being condensed by the first condenser 641, the gas is circulated back into the supergravity distillation bed 630.

[0060] The heavy component liquid flows out from the liquid outlet of the supergravity distillation bed 630 and enters the evaporator 620.

[0061] The acid value meter 642 monitors the acid value of the solvent exiting the first condenser 641 in real time. When the solvent acid value does not reach the set value, the control system repeats the above steps and the system performs full reflux operation.

[0062] The acid value meter 642 monitors the acid value of the solvent exiting the first condenser 641 in real time. When the solvent acid value reaches the set value and the value is stable, the fourth control valve 661 opens, and the light component gas with qualified acid value enters the membrane module 650 for dehydration, thereby obtaining the finished organic solvent.

[0063] When the solvent acid value reaches the set value and the value is stable, the system adjusts the opening of the fourth control valve 661 and the reflux pump 644 in conjunction with the feedback data of the acid value meter 642, thereby dynamically adjusting the reflux ratio of the system operation, improving the equipment's processing capacity and stability, and precisely adjusting parameters according to the characteristics of different recovered solvents.

[0064] A balancing pump 622 is installed on the pipeline between the liquid outlet of the high gravity distillation bed 630 and the first liquid inlet of the evaporator 620. During the separation and distillation process, the operating power of the balancing pump 622 is controlled by the current of the high gravity distillation bed 630. The operating power of the balancing pump 622 is automatically adjusted according to the power supply load of the high gravity distillation bed 630 to ensure the normal operation of the high gravity distillation bed 630. In some embodiments, the solvent acid value of the separated and purified product is <300ppm, and the water content is <0.5%.

[0065] In some embodiments of this application, the feed pipe assembly 610 includes a first feed pipe 611, which is connected to the second liquid inlet of the evaporator 620, and a first control valve 613 is provided on the first feed pipe 611.

[0066] The feed pipe assembly 610 includes a second feed pipe 612, which is connected to the liquid inlet of the supergravity distillation bed 630. A second control valve 614 is provided on the second feed pipe 612.

[0067] Specifically, the first feed pipe 611 delivers the recovered waste liquid to the evaporator 620, and the second feed pipe 612 delivers the recovered waste liquid to the supergravity distillation bed 630.

[0068] When the system is initially running, if the acid value meter 642 detects that the initial acid value of the recovered waste liquid is in the first range, such as 4%-10%, the acid value is relatively high. The first control valve 613 is opened and the second control valve 614 is closed. The recovered waste liquid enters the evaporator 620 through the first feed pipe 611. After being evaporated and vaporized in the evaporator 620, it enters the bottom of the supergravity distillation bed 630 in a gas phase state for distillation separation.

[0069] If the acid value meter 642 detects that the initial acid value of the recovered waste liquid is within the second range, such as 1%-4%, the acid value is not very high. The first control valve 613 is closed and the second control valve 614 is opened. The recovered waste liquid does not pass through the evaporator 620, but directly enters the supergravity distillation bed 630 for distillation separation through the second feed pipe 612.

[0070] In this way, automatically adjusting the feed position based on the acid value of the recycled waste liquid helps to reduce energy consumption and improve efficiency.

[0071] In some embodiments of this application, the second feed pipe 612 includes a second feed pipe 612Ⅰ, a second control valve 614Ⅰ is provided on the second feed pipe 612Ⅰ, and the second feed pipe 612Ⅰ is connected to the lower part of the supergravity distillation bed 630.

[0072] The second feed pipe 612 includes a second feed pipe 612Ⅱ, and a second control valve 614Ⅱ is provided on the second feed pipe 612Ⅱ. The second feed pipe 612Ⅱ is connected to the middle part of the supergravity distillation bed 630.

[0073] Specifically, if the acid value meter 642 detects that the initial acid value of the recovered waste liquid is within the third range, such as 1%-2%, then the first control valve 613 is closed, the second control valve 614Ⅰ is closed, and the second control valve 614Ⅱ is opened. The recovered waste liquid enters the middle of the supergravity distillation bed 630 in liquid phase through the second feed pipe 612Ⅱ for distillation separation.

[0074] If the acid value meter 642 detects that the initial acid value of the recovered waste liquid is within the fourth range, for example, 2%-4%, then the first control valve 613 is closed, the second control valve 614Ⅱ is closed, and the second control valve 614Ⅰ is opened. The recovered waste liquid enters the bottom of the supergravity distillation bed 630 in liquid phase through the second feed pipe 612Ⅰ for distillation separation.

[0075] In this way, automatically adjusting the feed position based on the acid value of the recycled waste liquid helps to reduce energy consumption and improve efficiency.

[0076] In some embodiments of this application, a reflux tank 643 is also provided on the circulation pipeline 640. Along the flow direction of the fluid in the circulation pipeline 640, the first condenser 641, the acid value meter 642, the reflux tank 643, and the reflux pump 644 are arranged in sequence.

[0077] In some embodiments of this application, a superheater 662 is provided on a first pipeline 660 between the membrane module and the gas outlet of the supergravity distillation bed 630. The superheater 662 is located downstream of the fourth control valve 661 along the flow direction of the fluid within the first pipeline 660.

[0078] Light component gas with qualified acid value flowing out of the supergravity distillation bed 630 first flows into the superheater 662 for heating and pressurization, and then flows into the membrane module 650 for dehydration treatment.

[0079] In some embodiments of this application, the liquid-gas outlet of the membrane module 650 is connected to a second pipeline 670, on which a second condenser 671, a regeneration solvent tank 672, and a product pump 674 are sequentially arranged. A moisture meter 673 is also arranged on the second pipeline 670.

[0080] The liquid gas flowing out of the membrane module is condensed by the second condenser 671 and then enters the regeneration solvent tank 672. The moisture meter 673 detects the water content of the regeneration solvent online in real time. When the set value is reached, the product pump 674 is turned on to discharge the regeneration solvent of the finished product.

[0081] In some embodiments of this application, the aqueous gas outlet of the membrane module 650 is connected to a third pipeline 680, and a third condenser 681, a vacuum buffer tank 682, and a wastewater pump 684 are sequentially arranged on the third pipeline 680. The vacuum buffer tube is connected to a vacuum pump 683.

[0082] The aqueous phase gas flowing out of the membrane module 650 is condensed by the third condenser 681 and then enters the vacuum buffer tank 682. When the liquid level in the vacuum buffer tank 682 reaches the set value, the wastewater pump 684 is turned on to discharge the wastewater.

[0083] In some embodiments of this application, the waste liquid outlet of the evaporator 620 is connected to a waste liquid pump 621 via a pipeline. When the liquid level of the waste liquid in the evaporator 620 reaches a set value, the waste liquid pump 621 is turned on to discharge the waste liquid.

[0084] Case 1

[0085] The acid value (calculated as acetic acid) of the recycled solvent in the coating industry is 1.5%, and the moisture content is 5%. The recycled solvent enters the evaporator 620 from the solvent pump 615 and the first feed pipe 611. After the liquid level of the evaporator 620 is reached, the control system automatically shuts off the solvent pump 615.

[0086] The gas exiting evaporator 620 enters the bottom of the centrifugal distillation bed 630, where it undergoes centrifugal distillation to separate light component gas and heavy component liquid. The light component gas enters the first condenser 641, and the solvent at the condensation outlet enters the reflux tank 643. The reflux solvent, after passing through the reflux pump 644, enters from the top of the centrifugal distillation bed 630. The acid value meter 642 monitors the acid value of the solvent at the condensation outlet in real time. When the solvent value does not reach the set value, the control system repeats the above steps, and the equipment operates under full reflux.

[0087] When the acid value of the solvent at the condenser outlet is <300ppm and the value is stable, the control system opens the second control valve 614Ⅱ, the fourth control valve 661, the vacuum pump 683, and the solvent pump 615 in the middle of the side line, and the equipment operates with continuous feeding. The light component gas with qualified acid value enters the superheater 662 for heating and pressurization. The membrane inlet gas that reaches the set parameters enters the membrane module 650 for dehydration treatment. The aqueous phase gas is liquefied through the third condenser 681 and enters the vacuum buffer tank 682. When the liquid level in the vacuum buffer tank 682 reaches the set value, the control system automatically starts the wastewater pump 684 to discharge the wastewater. The oil phase gas enters the second condenser 671 and is liquefied to enter the regeneration solvent tank 672. The moisture meter 673 monitors the water content of the regeneration solvent in real time. When the moisture content is <0.5%, the value is stable, and the control system automatically starts the product pump 674 to discharge the regeneration solvent.

[0088] Case 2

[0089] The recycled solvent in the lithium battery industry has an acid value (calculated as acetic acid) of 5% and a moisture content of 8%. The recycled solvent enters the evaporator 620 from the solvent pump 615 and the first feed pipe 611. After the liquid level of the evaporator 620 is reached, the control system automatically shuts off the solvent pump 615.

[0090] The gas exiting evaporator 620 enters the bottom of the centrifugal distillation bed 630, where it undergoes centrifugal distillation to separate light component gas and heavy component liquid. The light component gas enters the first condenser 641, and the solvent at the condensation outlet enters the reflux tank 643. The reflux solvent, after passing through the reflux pump 644, enters from the top of the centrifugal distillation bed 630. The acid value meter 642 monitors the acid value of the solvent at the condensation outlet in real time. When the solvent value does not reach the set value, the control system repeats the above steps, and the equipment operates under full reflux.

[0091] When the solvent acid value at the condenser outlet is <200ppm and stable, the control system activates the fourth control valve 661, the first control valve 613, the vacuum pump 683, and the solvent pump 615 based on the feedback signal from the online acid value meter 642, allowing the equipment to continuously feed. Light component gases with acceptable acid values ​​enter the superheater 662 for heating and pressurization. Gases reaching the set parameters at the membrane inlet enter the membrane module 650 for dehydration. Aqueous phase gases are liquefied in the third condenser 681 and enter the vacuum buffer tank 682. When the liquid level in the vacuum buffer tank 682 reaches the set value, the control system automatically activates the wastewater pump 684 to discharge wastewater. Oil phase gases enter the second condenser 671 and are liquefied before entering the regenerated solvent tank 672. The online moisture meter 673 monitors the water content of the regenerated solvent in real time. When the moisture content is <0.3% and stable, the control system automatically activates the product pump 674 to discharge the regenerated solvent.

[0092] The waste liquid separation and dehydration system of this application has the following advantages:

[0093] This system automatically monitors the acid value of the solvent online in real time and uses a feedback mechanism to automatically optimize the operating parameters of the system, thereby improving the system's operating efficiency.

[0094] This system automatically monitors the acid value and moisture content of the solvent online in real time, enabling fully automated operation of the entire process, ensuring stable operation, and reducing manual labor costs.

[0095] Based on the different acid values ​​of the recovered solvent, the control system automatically adjusts the feed position, shortens the operation time to reach the standard, and saves energy.

[0096] This system automatically monitors the acid value of the solvent online in real time, controls the system to automatically adjust the reflux ratio, optimize operating parameters, and improve operating efficiency.

[0097] This system links the power supply load of the hypergravity system and the power of the balancing pump 622 to ensure the continuous and stable operation of the hypergravity distillation bed 630.

[0098] This system operates fully automatically, reducing human error and saving labor costs.

[0099] The system has simple and easy-to-operate processes and meets the requirements for the recycling of raw materials in the production line.

[0100] In the description of the above embodiments, specific features, structures, materials, or characteristics may be combined in any suitable manner in one or more embodiments or examples.

[0101] The above are merely specific embodiments of this utility model, but the protection scope of this utility model is not limited thereto. Any variations or substitutions that can be easily conceived by those skilled in the art within the technical scope disclosed in this utility model should be included within the protection scope of this utility model. Therefore, the protection scope of this utility model should be determined by the scope of the claims.

Claims

1. A waste liquid recovery separation and dehydration system, characterized in that, Including: An evaporator is configured to evaporate and vaporize the flowing organic solvent; A supergravity distillation bed, wherein the gas inlet of the supergravity distillation bed is connected to the gas outlet of the evaporator via a pipeline, and the liquid outlet of the supergravity distillation bed is connected to the first liquid inlet of the evaporator via a pipeline; The circulation pipeline is connected at one end to the gas outlet of the supergravity distillation bed and at the other end to the reflux port of the supergravity distillation bed. A first condenser and an acid value meter are installed on the circulation pipeline. The membrane module is connected to the gas outlet of the supergravity distillation bed via a first pipeline. A fourth control valve is provided on the first pipeline. The membrane module is configured to dehydrate the flowing solvent to obtain the finished organic solvent. The feed pipe assembly is configured to deliver recycled waste liquid to the evaporator or the high-gravity distillation bed.

2. The waste liquid separation and dehydration system according to claim 1, characterized in that, The feed pipe assembly includes a first feed pipe, which is connected to the second liquid inlet of the evaporator, and a first control valve is provided on the first feed pipe; The feed pipe assembly includes a second feed pipe, which is connected to the liquid inlet of the supergravity distillation bed, and a second control valve is provided on the second feed pipe.

3. The waste liquid separation and dehydration system according to claim 2, characterized in that, The second feed pipe includes a second feed pipe I, on which a second control valve I is provided, and the second feed pipe I is connected to the lower part of the supergravity distillation bed; The second feed pipe includes a second feed pipe II, and a second control valve II is provided on the second feed pipe II. The second feed pipe II is connected to the middle part of the supergravity distillation bed.

4. The waste liquid separation and dehydration system according to claim 1, characterized in that, A balancing pump is installed on the pipeline between the liquid outlet of the supergravity distillation bed and the first liquid inlet of the evaporator.

5. The waste liquid separation and dehydration system according to claim 1, characterized in that, The circulation pipeline is also equipped with a reflux tank and a reflux pump.

6. The waste liquid separation and dehydration system according to claim 1, characterized in that, An overheater is provided on the first pipeline between the membrane module and the gas outlet of the supergravity distillation bed.

7. The waste liquid separation and dehydration system according to any one of claims 1 to 6, characterized in that, The liquid phase gas outlet of the membrane module is connected to a second pipeline, which is equipped with a second condenser, a regeneration solvent tank, and a product pump.

8. The waste liquid separation and dehydration system according to claim 7, characterized in that, A moisture meter is also installed on the second pipeline.

9. The waste liquid separation and dehydration system according to any one of claims 1 to 6, characterized in that, The aqueous gas outlet of the membrane module is connected to a third pipeline, which is equipped with a third condenser, a vacuum buffer tank, and a wastewater pump.

10. The waste liquid separation and dehydration system according to any one of claims 1 to 6, characterized in that, The waste liquid outlet of the evaporator is connected to a waste liquid pump via a pipeline.

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