A high-efficiency separation and treatment device

Abstract

The utility model relates to separating equipment technical field, concretely relates to a kind of high-efficiency separation processing device, including negative pressure separating device, gas-liquid separating device, heat exchange device and collection device, heating mixed liquid needing separation is carried out by negative pressure separating device, according to the boiling point difference between the components in mixed liquid respectively distillation output, wherein temperature control device can carry out accurate adjustment to temperature, ensure separation effect;By being provided with gas-liquid separating device, multistage gas-liquid separation can be realized, and separation effect is more optimal;By setting heat exchange device, gaseous state material or mixed gaseous state material distilled out is condensed distillation, finally recycled by collection device;Realize the continuous separation of different boiling point mixed liquid, and separation efficiency is high, and separation effect is good, simultaneously enhance the recovery rate of low-boiling-point substance, facilitate heat recovery.

Description

Technical Field

[0001] This utility model relates to the field of separation equipment technology, specifically to a high-efficiency separation and processing device. Background Technology

[0002] In semiconductor manufacturing processes, key steps such as wafer cleaning, photolithography, and development require the use of large quantities of high-purity organic solvents, such as isopropanol, methanol, and ethanol, to remove particles, organic contaminants, and residual photoresist. These solvents, after use, form complex organic waste liquids. Direct discharge of such waste liquids not only significantly increases the load on subsequent wastewater treatment systems, causing secondary water pollution, but also results in a substantial waste of organic solvent resources. With increasingly stringent emission standards for industrial waste liquids, traditional simple treatment or direct discharge methods are no longer sufficient to meet regulatory requirements. Therefore, the efficient separation, recovery, and reuse of organic waste solvents has become a crucial issue for the semiconductor industry in terms of energy conservation, emission reduction, and cost reduction.

[0003] Currently, distillation technology is widely used in the recovery and treatment of organic waste solvents due to its relatively simple operation and wide applicability. Distillation utilizes the differences in volatility of components in a mixture, achieving separation through partial vaporization and condensation. However, existing distillation technologies still have many shortcomings in treating organic waste solvents from the semiconductor industry. Because organic solvents are complex in composition, often containing water, various alcohols, and other trace impurities, existing distillation equipment has low separation efficiency, making it difficult to obtain high-purity recovered solvents and affecting their reuse performance. Traditional distillation processes are energy-intensive, have low heat recovery rates, lack effective energy integration design, and are costly. Utility Model Content

[0004] The purpose of this invention is to provide a high-efficiency separation and processing device to solve the existing technical problems in the background art.

[0005] To solve the above-mentioned technical problems, the technical solution provided by this utility model is as follows: a high-efficiency separation and processing device is provided, including a negative pressure separation device, a gas-liquid separation device, a heat exchange device, and a collection device. The negative pressure separation device is used to heat and distill the liquid mixture for separation. The gas-liquid separation device is located at the end of the negative pressure separation device for gas-liquid separation. The heat exchange device is located at the end of the gas-liquid separation device for condensing and separating the substances after gas-liquid separation. The collection device is located at the end of the heat exchange device for collecting the liquid after condensation and separation.

[0006] Based on the above technical solution, the negative pressure separation device includes a separation tank, a heating mechanism, and a negative pressure mechanism. The separation tank is filled with a mixed liquid to be separated. The heating mechanism heats the separation tank, and the negative pressure mechanism extracts air from the separation tank to create a negative pressure environment. During the heating process, the mixed liquid is distilled and separated and enters the heat exchange device.

[0007] Based on the above technical solution, the negative pressure separation device further includes a temperature control device for temperature regulation. The temperature control device includes a conveying pipeline, a heating channel, and a cooling channel. One end of the conveying pipeline is connected to the separation tank via a transfer pump, and the other end is connected to the separation tank after passing through the heating channel and the cooling channel in sequence. A heating pipeline is sleeved on the outside of the heating channel, and a cooling pipeline is sleeved on the outside of the cooling channel. Circulating steam is provided in the heating pipeline, and a circulating cooling medium is provided in the cooling pipeline.

[0008] Based on the above technical solution, the gas-liquid separation device includes a separation tower, a packing layer and a venting layer. The packing layer and the venting layer are both arranged inside the separation tower and are arranged alternately. The packing layer is filled with mesh packing.

[0009] Based on the above technical solution, the height of the packing layer is 50-200mm, the height of the venting layer is 50-100mm, and the specific surface area of ​​the mesh packing is 700-1000m². 2 / m 3 Fiber web.

[0010] Based on the above technical solution, the heat exchange device includes at least a first heat exchanger and a second heat exchanger. The first heat exchanger is provided with a heat exchange channel that allows the flow of substances, which flow from top to bottom within the heat exchange channel. A cooling channel is sleeved on the outside of the heat exchange channel, and a cooling medium circulates from bottom to top within the cooling channel. The second heat exchanger is connected in series at the end of the first heat exchanger and has the same structure. The second heat exchanger and the first heat exchanger are connected by a first diameter reducing assembly.

[0011] Based on the above technical solution, the first variable diameter assembly includes an output pipe, a first connecting pipe, and a second connecting pipe. The diameter of the output pipe is smaller than the diameters of the first and second connecting pipes. One end of the output pipe is connected to the outlet of the heat exchange channel, and the other end is connected to the inlet of the first and second connecting pipes respectively. The outlet of the first connecting pipe is connected to the inlet of the heat exchange channel of the second heat exchanger. The outlet of the second connecting pipe is connected to the first collecting pipe. The outlet of the heat exchange channel of the second heat exchanger is also connected to the first collecting pipe.

[0012] Based on the above technical solution, a third heat exchanger is also included, which is connected in series at the end of the second heat exchanger and has the same structure. The third heat exchanger and the second heat exchanger are connected by a second diameter-changing assembly, which has the same structure as the first diameter-changing assembly. The outlet of the first connecting pipe of the second diameter-changing assembly is connected to the inlet of the heat exchange channel of the third heat exchanger, the outlet of the second connecting pipe of the second diameter-changing assembly is connected to the first collecting pipe, and the outlet of the heat exchange channel of the third heat exchanger is connected to the second collecting pipe.

[0013] Based on the above technical solutions, the first collection tube and the second collection tube are arranged in parallel and are independent of each other, or the first collection tube and the second collection tube are connected in series and are interconnected.

[0014] Based on the above technical solution, the negative pressure separation device is also equipped with a circulation device, which includes a circulation pipeline, a circulation pump and a cooling sleeve. One end of the circulation pipeline is connected to the bottom end of the separation tank and the other end is connected to the top end of the separation tank. The circulation pump is installed on the circulation pipeline, and the cooling sleeve is installed on the circulation pipeline. Circulating cooling water is installed inside the cooling sleeve.

[0015] Based on the above technical solution, the collection device includes a collection tank, a second vent valve, a vacuum valve, and a storage tank. The collection tank is connected to the end of the heat exchange device through a collection pipeline. The collection tank is equipped with a second vent valve and a vacuum valve. The second vent valve is used to introduce nitrogen into the collection tank to assist in draining the liquid. The vacuum valve is used to create a vacuum to achieve a negative pressure environment. The storage tank is located at the end of the collection tank.

[0016] The beneficial effects of the technical solution provided by this utility model are as follows: This invention provides a high-efficiency separation and processing device. A negative pressure separation device heats the mixed liquid to be separated, and distills and outputs the components according to their different boiling points. A temperature control device allows for precise temperature adjustment to ensure separation efficiency. A gas-liquid separation device enables multi-stage gas-liquid separation, resulting in superior separation performance. A heat exchange device condenses and distills the distilled gaseous or mixed gaseous substances, which are then recovered through a collection device. This invention achieves continuous separation of mixed liquids with different boiling points, resulting in high separation efficiency and good separation effect, while also enhancing the recovery rate of low-boiling-point substances and facilitating heat recovery. Attached Figure Description

[0017] Figure 1 This is a schematic diagram of the overall structure of this utility model; Figure 2 This is a schematic diagram of the temperature control device and the gas-liquid separation device in this utility model; Figure 3This is a schematic diagram of one possible structure of the heat exchange device in this utility model; Figure 4 This is another structural schematic diagram of the heat exchange device in this utility model; Detailed Implementation The present invention will be further described below with reference to the accompanying drawings and embodiments: In this utility model, unless otherwise explicitly specified and limited, the terms "installation," "connection," "joining," and "fixing," etc., should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components. For those skilled in the art, the specific meaning of the above terms in this utility model can be understood according to the specific circumstances.

[0018] In the description of this utility model, it should be understood that the terms "left", "right", "front", "rear", "top", "bottom", 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 utility model 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 utility model.

[0019] like Figures 1 to 4 As shown, a high-efficiency separation and processing device includes a negative pressure separation device 1, a gas-liquid separation device 5, a heat exchange device 3, and a collection device 4. The negative pressure separation device 1 is used to heat and distill liquid mixtures for separation. The gas-liquid separation device 5 is located at the end of the negative pressure separation device 1 and is used for gas-liquid separation. The heat exchange device 3 is located at the end of the gas-liquid separation device 5 and is used to condense and separate the substances after gas-liquid separation. The collection device 4 is located at the end of the heat exchange device 3 and is used to collect the liquid after condensation and separation.

[0020] This invention provides a high-efficiency separation and processing device. A negative pressure separation device heats the mixed liquid to be separated, and distills and outputs the components according to their different boiling points. A temperature control device allows for precise temperature adjustment to ensure separation efficiency. A gas-liquid separation device 5 enables multi-stage gas-liquid separation, resulting in superior separation performance. A heat exchange device condenses and distills the distilled gaseous or mixed gaseous substances, which are then recovered through a collection device. This invention achieves continuous separation of mixed liquids with different boiling points, resulting in high separation efficiency and good separation effect, while also enhancing the recovery rate of low-boiling-point substances and facilitating heat recovery.

[0021] Based on the above technical solution, the negative pressure separation device 1 includes a separation tank 11, a heating mechanism, and a negative pressure mechanism. The separation tank 11 is filled with a mixed liquid to be separated. The heating mechanism heats the separation tank 11, and the negative pressure mechanism extracts air from the separation tank 11 to form a negative pressure environment in the separation tank 11. During the heating process, the mixed liquid is distilled and separated and enters the heat exchange device 3.

[0022] Preferably, the heating mechanism can be an electric heating bath or an electric heating mantle, etc.

[0023] The mixed liquid in the separator 11 is heated by a heating mechanism. Different components in the mixed liquid have different boiling points, so substances with lower boiling points evaporate first and enter the subsequent heat exchange device. The vapor phase that evaporates preferentially may also contain liquid phase substances, but these condense as the vapor rises and flow back into the separator 11 for further distillation and separation. A negative pressure environment is created inside the separator 11 by a negative pressure mechanism, which can increase the distillation rate within the separator and also reduce the temperature required for distillation, thus reducing energy consumption. More preferably, the negative pressure mechanism uses a vacuum pump to provide a vacuum environment within the separation system.

[0024] A temperature sensor is installed inside the separation tank 11, and the temperature sensor is electrically connected to the temperature control device. By installing a temperature sensor inside the separation tank, the temperature inside the separation tank can be monitored in real time, which helps to accurately control the temperature inside the tank.

[0025] More preferably, the top of the separation tank 11 is provided with a first vent valve 12 for introducing nitrogen gas to assist in draining the liquid.

[0026] Based on the above technical solution, the negative pressure separation device 1 further includes a temperature control device for temperature regulation. The temperature control device includes a conveying pipeline 21, a heating channel 22, and a cooling channel 23. One end of the conveying pipeline 21 is connected to the separation tank 11 via a transfer pump 24, and the other end is connected to the separation tank 11 after passing through the heating channel 22 and the cooling channel 23 in sequence. A heating pipeline is sleeved on the outside of the heating channel 22, and a cooling pipeline is sleeved on the outside of the cooling channel 23. Circulating steam is provided in the heating pipeline, and a circulating cooling medium is provided in the cooling pipeline.

[0027] When temperature control of the liquid in separation tank 11 is required, the mixed liquid in the separation tank is output through a delivery pipeline. If the temperature is too high, only the cooling channel can be opened; if the temperature is too low, only the heating channel can be opened. The mixed liquid is circulated by a transfer pump, and the temperature in the tank is precisely controlled in conjunction with the heating and cooling channels. The temperature control device in this embodiment has better temperature control effect, with independent control of heating and cooling, making it easier to accurately control the temperature. It has excellent practical performance, especially for drug separation where high temperature control accuracy is required. Compared with common heating mechanisms such as electric heating that directly heat the separation tank, temperature control is more convenient; it also avoids the problem of long natural cooling time and inconvenience caused by overheating when using conventional heating mechanisms.

[0028] Based on the above technical solution, the gas-liquid separation device 5 includes a separation tower 51, a packing layer 52 and a venting layer 53. The packing layer 52 and the venting layer 53 are both arranged inside the separation tower 51 and are arranged alternately. The packing layer 52 is filled with mesh packing.

[0029] Based on the above technical solution, the height of the packing layer 52 is 50-200mm, the height of the venting layer 53 is 50-100mm, and the specific surface area of ​​the mesh packing is 700-1000m². 2 / m 3 The fibrous mesh is formed by winding it into a ring structure, and then the surface is fixed with a shell.

[0030] More preferably, the mesh packing material can be selected from PTFE, PE, or PP materials depending on the temperature of the separated substances, because its specific surface area is much larger than that of metal perforated plate corrugated packing (250-500 μm²). 2 / m 3 This greatly improves separation accuracy and processing capacity.

[0031] Gas-liquid separation can be achieved by incorporating a gas-liquid separation device 5. This device features a multi-layered packing layer 52 and a venting layer 53. The use of a high-surface-area fiber mesh structure as packing material significantly improves separation accuracy and processing capacity. Simultaneously, the staggered arrangement of the venting layer and packing layer prevents airflow accumulation and enhances separation efficiency. Furthermore, compared to existing technologies, the height of the separation tower can be significantly reduced. Traditional separation towers require a height of 30m to achieve the desired gas-liquid separation, while this application reduces the height to less than 2m, demonstrating excellent practical performance.

[0032] Based on the above technical solution, the heat exchange device 3 includes at least a first heat exchanger 31 and a second heat exchanger 32. The first heat exchanger 31 is provided with a heat exchange channel 311 that allows the flow of substances. The substances flow from top to bottom in the heat exchange channel 311. A cooling channel 312 is sleeved on the outside of the heat exchange channel 311. A cooling medium circulates from bottom to top in the cooling channel 312. The second heat exchanger 32 is connected in series at the end of the first heat exchanger 31 and has the same structure.

[0033] Based on the above technical solution, the first variable diameter assembly 33 includes an output pipe 331, a first connecting pipe 332, and a second connecting pipe 333. The diameter of the output pipe 331 is smaller than the diameters of the first connecting pipe 332 and the second connecting pipe 333. One end of the output pipe 331 is connected to the outlet of the heat exchange channel 311, and the other end is connected to the inlet of the first connecting pipe 332 and the inlet of the second connecting pipe 333. The outlet of the first connecting pipe 332 is connected to the inlet of the heat exchange channel of the second heat exchanger 32. The outlet of the second connecting pipe 333 is connected to the first collecting pipe 34. The outlet of the heat exchange channel of the second heat exchanger 32 is also connected to the first collecting pipe 34.

[0034] Preferably, multiple second heat exchangers 32 are provided, with multiple second heat exchangers 32 connected in series at the end of the first heat exchanger 31. The raw liquid (i.e., the liquid to be treated) is used for cooling and preheating simultaneously, thus recovering more than 50% of the heat. Multi-stage cooling is then achieved using a temperature difference of more than 20°C between ice water (7-9°C) and the refrigerant (ethylene glycol, below -15°C). This allows for the condensation of a single gaseous substance and the separation of two gaseous substances or two mixed gases, enhancing the recovery rate of low-boiling-point substances and reducing emissions. Staged cooling is particularly practical for separating waste liquids containing small amounts of light-boiling substances.

[0035] By detecting the temperature at the condensate outlet, the flow rate of the coolant is intelligently controlled to reduce overcooling and overheating of the condensate, thereby achieving an efficient and stable heat exchange process.

[0036] Specifically, the substance introduced into the heat exchange channel 311 of the first heat exchanger 31 is condensed. The condensed high-temperature substance enters the heat exchange channel of the second heat exchanger 32 through the first connecting pipe 332 after passing through the output pipe, and then undergoes another condensation. The condensed liquid flows into the collection pipe through the second connecting pipe and the condensed liquid of the second heat exchanger together with the liquid condensed by the second heat exchanger.

[0037] Based on the above technical solution, a third heat exchanger 35 is also included, which is connected in series at the end of the second heat exchanger 32 and has the same structure. The third heat exchanger 35 and the second heat exchanger 32 are connected by a second diameter-changing assembly 36, which has the same structure as the first diameter-changing assembly 33. The outlet of the first connecting pipe of the second diameter-changing assembly 36 is connected to the inlet of the heat exchange channel of the third heat exchanger 35, the outlet of the second connecting pipe of the second diameter-changing assembly 36 is connected to the first collecting pipe 34, and the outlet of the heat exchange channel of the third heat exchanger 35 is connected to the second collecting pipe 37.

[0038] Based on the above technical solution, the first collection tube 34 and the second collection tube 37 are arranged in parallel and are independent of each other, or the first collection tube 34 and the second collection tube 37 are arranged in series and are interconnected.

[0039] More preferably, a third heat exchanger 35 is connected in series at the end of the last second heat exchanger 32, which can achieve condensation and separation between two gaseous substances or gas mixtures in addition to multi-stage cooling.

[0040] Preferably, the circulating cooling media in the first heat exchanger 31, the second heat exchanger 32, and the third heat exchanger 35 are different to achieve optimal heat collection and cooling effects. Specifically, the first heat exchanger 31, due to its higher temperature, is generally cooled using the raw liquid (the liquid being processed, at room temperature) to recover heat and increase the temperature of the raw liquid. The second heat exchanger 32 uses ice water (7-9℃), and the third heat exchanger 35 uses a refrigerant (such as ethylene glycol, -15℃) to achieve optimal collection effects.

[0041] The heat exchange device in this application has two specific implementation methods, corresponding to the separation and condensation of different substances. Taking a device containing three heat exchangers as an example, the specific implementation methods are described below: In one preferred embodiment, when condensing and separating a gaseous substance, if the condensation temperature difference between the two solvents is greater than 10 degrees Celsius, the two gaseous solvents are separated by precisely controlling the flow rate and temperature of the coolant. The heat exchange device includes a first heat exchanger 31, a second heat exchanger 32, and a third heat exchanger 35. The gaseous substance enters from the inlet of the heat exchange channel 311 of the first heat exchanger 31, and then flows out from the outlet of the heat exchange channel, passing through the first diameter reducing component and flowing backward. Specifically, the gaseous substance that has undergone one condensation and becomes liquid flows into the second connecting pipe 333 and flows backward, through the first collecting pipe 34 and into the collecting tank. The gaseous portion flows into the heat exchange channel of the second heat exchanger 32 through the first connecting pipe 332 for further condensation. This process continues, and the substance flowing out of the second heat exchanger 32 flows into the third heat exchanger 35. Finally, the liquids that have all been condensed, along with the liquids condensed by the first heat exchanger 31 and the second heat exchanger 32, flow into the collecting tank.

[0042] In another preferred embodiment, when condensing and separating two different gaseous substances or two mixed gases, the heat exchange device 3 includes a first heat exchanger 31 (cooled by ambient temperature raw liquid), a second heat exchanger 32 (cooled by ice water), and a third heat exchanger 35 (cooled by refrigerant such as ethylene glycol). Due to the large temperature difference between the three refrigerants, the mixed substance enters from the inlet of the heat exchange channel of the first heat exchanger 31 and then flows out from the outlet of the heat exchange channel, passing through the first diameter-reducing component 33 and flowing backward. Specifically, the portion of the gaseous substance that has undergone one condensation and becomes liquid flows into the second heat exchanger 35. After passing through connecting pipe 333, the liquid enters the first collecting pipe 34. The gaseous portion flows through the first connecting pipe 332 into the heat exchange channel of the second heat exchanger 32 for further condensation. The liquid flowing out from the outlet of the second connecting pipe of the second reducing assembly 36 enters the first collecting pipe and flows out, thus achieving the condensation of one gaseous or gaseous substance. The other substance then enters the heat exchange channel of the third heat exchanger, flows out from the outlet of the third heat exchanger, and enters the second collecting pipe. That is, the first and second collecting pipes collect the two liquids after condensation and separation. More preferably, if the second substance needs further cooling, another heat exchanger can be connected in series at the end of the third heat exchanger to achieve a better condensation effect.

[0043] The heat exchange channel 311 is uniformly provided with heat exchange plates, and guide vanes are provided between the heat exchange plates. Preferably, the guide vanes between the heat exchange plates guide the fluid to flow along a spiral path, thereby prolonging the heat exchange time.

[0044] The heat exchange plates in the first heat exchanger 31 are configured as herringbone corrugated plates, while the heat exchange plates in the second heat exchanger 32 and the third heat exchanger 35 are configured as parallel corrugated plates. More preferably, the first heat exchanger uses herringbone corrugated plates to enhance turbulence intensity and improve heat exchange efficiency; the second and third heat exchangers use parallel corrugated plates to reduce secondary pressure drop.

[0045] Based on the above technical solution, the negative pressure separation device 1 is also equipped with a circulation device, which includes a circulation pipeline 61, a circulation pump 62, and a cooling sleeve 63. One end of the circulation pipeline 61 is connected to the bottom end of the separation tank 11, and the other end is connected to the top end of the separation tank 11. The circulation pump 62 is installed on the circulation pipeline 61, and the cooling sleeve 63 is sleeved on the circulation pipeline 61. Circulating cooling water is installed inside the cooling sleeve 63.

[0046] Preferably, a circulation device is provided in the separator 11 to realize the circulation and agitation of the liquid, avoid the concentration difference or temperature difference between the upper and lower liquid layers, and effectively prevent the problem of low concentration of the upper liquid and high concentration of the lower liquid layer; at the same time, a cooling sleeve is provided on the circulation pipeline to effectively prevent the liquid temperature from being too high and ensure the distillation separation effect.

[0047] Based on the above technical solution, the collection device 4 includes a collection tank 41, a second vent valve 42, a vacuum valve 43, and a storage tank 44. The collection tank 41 is connected to the end of the heat exchange device 3. The collection tank 41 is respectively equipped with a second vent valve 42 and a vacuum valve 43. The second vent valve 42 is used to introduce nitrogen into the collection tank 41 to assist in liquid drainage. The vacuum valve 43 is used to create a vacuum to achieve a negative pressure environment. The storage tank 44 is located at the end of the collection tank 41.

[0048] Preferably, the collection tank 41 is used to collect the liquid after condensation and separation, and is connected through a first collection pipe 34 or a second collection pipe 37. The collection tank 41 is equipped with a vacuum valve 43 to maintain the same vacuum environment as the system. At the same time, a second vent valve 42 is also provided to facilitate the introduction of nitrogen into the collection tank 41 to assist in the drainage of the liquid, and to transfer the collected liquid to the storage tank 44 for storage. After the liquid is drained, a negative pressure environment is achieved by the vacuum valve to facilitate the continued subsequent separation operation.

[0049] The foregoing has shown and described the basic principles and main features of this utility model. It is obvious to those skilled in the art that this utility model is not limited to the details of the above exemplary embodiments. Therefore, the embodiments should be regarded as exemplary and non-limiting. The scope of this utility model is defined by the appended claims rather than the foregoing description. Therefore, it is intended to include all changes that fall within the meaning and scope of the equivalents of the claims within this utility model.

[0050] Furthermore, it should be understood that although this specification describes embodiments, not every embodiment contains only one independent technical solution. This narrative style is merely for clarity. Those skilled in the art should consider the specification as a whole, and the technical solutions in each embodiment can also be appropriately combined to form other embodiments that can be understood by those skilled in the art.

Claims

1. A high-efficiency separation processing device, characterized by comprising: It includes a negative pressure separation device, a gas-liquid separation device, a heat exchange device, and a collection device. The negative pressure separation device is used to heat and distill the liquid mixture for separation. The gas-liquid separation device is located at the end of the negative pressure separation device for gas-liquid separation. The heat exchange device is located at the end of the gas-liquid separation device for condensing and separating the substances after gas-liquid separation. The collection device is located at the end of the heat exchange device for collecting the liquid after condensation and separation.

2. The high-efficiency separation treatment device according to claim 1, characterized by The negative pressure separation device includes a separation tank, a heating mechanism, and a negative pressure mechanism. The separation tank is filled with a mixed liquid to be separated. The heating mechanism heats the separation tank, and the negative pressure mechanism extracts air from the separation tank to create a negative pressure environment. During the heating process, the mixed liquid is distilled and separated and enters the heat exchange device.

3. The high efficiency separation processing device of claim 2, wherein, The negative pressure separation device also includes a temperature control device for temperature regulation. The temperature control device includes a delivery pipeline, a heating channel, and a cooling channel. One end of the delivery pipeline is connected to the separation tank via a transfer pump, and the other end is connected to the separation tank after passing through the heating channel and the cooling channel in sequence. A heating pipeline is sleeved on the outside of the heating channel, and a cooling pipeline is sleeved on the outside of the cooling channel. Circulating steam is installed in the heating pipeline, and a circulating cooling medium is installed in the cooling pipeline.

4. The high efficiency separation processing device of claim 1, wherein, The gas-liquid separation device includes a separation tower, a packing layer, and a venting layer. The packing layer and the venting layer are both arranged inside the separation tower and are arranged alternately. The packing layer is filled with mesh packing.

5. The high efficiency separation processing device of claim 4, wherein, The height of the filler layer is 50-200 mm, the height of the emptying layer is 50-100 mm; the specific surface area of the reticular filler is 700-1000 m 2 / m 3 The fiber web has a basis weight of 50-200 g / m2.

6. The high efficiency separation processing device of claim 1, wherein, The heat exchange device includes at least a first heat exchanger and a second heat exchanger. The first heat exchanger has a heat exchange channel that allows the flow of substances from top to bottom. A cooling channel is sleeved on the outside of the heat exchange channel, and a cooling medium circulates from bottom to top in the cooling channel. The second heat exchanger is connected in series at the end of the first heat exchanger and has the same structure. The second heat exchanger and the first heat exchanger are connected by a first diameter reducing assembly.

7. The high efficiency separation processing device of claim 6, wherein, The first variable diameter assembly includes an output pipe, a first connecting pipe, and a second connecting pipe. The diameter of the output pipe is smaller than the diameters of the first and second connecting pipes. One end of the output pipe is connected to the outlet of the heat exchange channel, and the other end is connected to the inlet of the first and second connecting pipes respectively. The outlet of the first connecting pipe is connected to the inlet of the heat exchange channel of the second heat exchanger, and the outlet of the second connecting pipe is connected to the first collecting pipe. The outlet of the heat exchange channel of the second heat exchanger is also connected to the first collecting pipe.

8. The high efficiency separation processing device of claim 7, wherein, It also includes a third heat exchanger connected in series at the end of the second heat exchanger and having the same structure. The third heat exchanger and the second heat exchanger are connected by a second diameter-changing assembly, which has the same structure as the first diameter-changing assembly. The outlet of the first connecting pipe of the second diameter-changing assembly is connected to the inlet of the heat exchange channel of the third heat exchanger, the outlet of the second connecting pipe of the second diameter-changing assembly is connected to the first collecting pipe, and the outlet of the heat exchange channel of the third heat exchanger is connected to the second collecting pipe.

9. The high efficiency separation processing device of claim 8, wherein, The first collection tube and the second collection tube are arranged in parallel and are independent of each other, or the first collection tube and the second collection tube are arranged in series and are interconnected.

10. The high efficiency separation processing device of claim 2, wherein, The negative pressure separation device is also equipped with a circulation device, which includes a circulation pipeline, a circulation pump and a cooling sleeve. One end of the circulation pipeline is connected to the bottom of the separation tank and the other end is connected to the top of the separation tank. The circulation pump is installed on the circulation pipeline, and the cooling sleeve is installed on the circulation pipeline. Circulating cooling water is installed inside the cooling sleeve.

11. The high efficiency separation processing device of claim 1, wherein, The collection device includes a collection tank, a second vent valve, a vacuum valve, and a storage tank. The collection tank is connected to the end of the heat exchange device through a collection pipeline. The collection tank is equipped with a second vent valve and a vacuum valve. The second vent valve is used to introduce nitrogen into the collection tank to assist in draining the liquid. The vacuum valve is used to create a vacuum to achieve a negative pressure environment. The storage tank is located at the end of the collection tank.

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