A bisphenol F dephenolization system

Abstract

This utility model relates to the field of bisphenol F removal technology, and more particularly to a bisphenol F removal system, comprising an evaporator, a steam compressor, a falling film evaporator, a circulating pump, and a phenol recovery tank. The evaporator has a first feed inlet and a live steam inlet. A first outlet is located at the top of the evaporator, and a first inlet is located at the top of the falling film evaporator; the first outlet, the steam compressor, and the first inlet are sequentially connected. A first discharge outlet is located at the bottom of the evaporator, and a second feed inlet is located at the top of the evaporator; the first discharge outlet, the circulating pump, the falling film evaporator, and the second feed inlet are sequentially connected. The falling film evaporator has a phenol liquid outlet, which is connected to the phenol recovery tank. This utility model provides a bisphenol F removal system that effectively recovers and utilizes the latent heat of low-temperature, low-pressure phenol vapor, while avoiding the consumption of cooling water resources required for condensing this vapor, thereby reducing energy consumption and production costs.

Description

Technical Field

[0001] This utility model relates to the field of bisphenol F removal technology, and in particular to a bisphenol F removal system. Background Technology

[0002] Bisphenol F (BPF), chemically known as bis-(hydroxyphenyl)methane, is a chemical raw material with a similar chemical structure to bisphenol A (BPA) but with different substituents. It has been gradually developed and applied in the industrial field since the 1980s.

[0003] The synthesis of bisphenol F is mainly achieved through a condensation reaction between phenol and formaldehyde in the presence of an acidic catalyst (such as sulfuric acid or phosphoric acid). The main reaction equation is shown below:

[0004] Although bisphenol F was prepared in the laboratory as early as the 1970s, the reaction appears simple but its actual mechanism is complex, with numerous side reactions and a high tendency to generate phenolic resins. To suppress side reactions and increase the yield of bisphenol F, a large excess of phenol is usually required, with the phenol-formaldehyde molar ratio (i.e., the molar ratio of phenol to formaldehyde) often exceeding 10:1. When producing high-purity products, the phenol-formaldehyde molar ratio can even reach 20:1, resulting in the need to remove a large amount of unreacted phenol during subsequent purification.

[0005] Currently, the vacuum steam stripping method is commonly used in industry to remove excess phenol from the bisphenol F reaction mixture. This involves heating the bisphenol F reaction mixture with steam under vacuum conditions, causing the phenol to evaporate and separate, thus obtaining a high-purity bisphenol F product. However, due to the large initial excess of phenol, this process is extremely energy-intensive. Furthermore, the heat energy of the phenol vapor generated during the stripping process is usually absorbed by cooling water and directly discharged after condensation, failing to achieve effective recovery. This not only leads to the consumption of cooling water resources but also results in low overall energy utilization efficiency and high production costs. Utility Model Content

[0006] The purpose of this invention is to provide a bisphenol F dephenolization system. This system pressurizes and heats the low-temperature, low-pressure phenol vapor generated during the dephenolization process using a steam compressor, converting it into high-temperature, high-pressure phenol vapor. This high-temperature, high-pressure vapor is then used as a heat source to replace external live steam for evaporating residual phenol in the bisphenol F dephenolization reaction mixture. This achieves effective recovery and utilization of the latent heat of the low-temperature, low-pressure phenol vapor, while avoiding the cooling water resources required for condensing the low-temperature, low-pressure phenol vapor. This significantly reduces energy consumption and production costs, overcoming the shortcomings of existing technologies.

[0007] To achieve this objective, the present invention adopts the following technical solution: A bisphenol F dephenolization system includes an evaporator, a steam compressor, a falling film evaporator, a circulating pump, and a phenol recovery tank; The evaporator is provided with a first feed port for feeding the bisphenol F reaction mixture and a live steam inlet for entering the live steam. The live steam conveying pipe is used to convey live steam. The evaporator is used to use live steam to separate the bisphenol F reaction mixture to be purified into low-temperature, low-pressure phenol vapor and a liquid enriched with bisphenol F. The top of the evaporator is provided with a first air outlet, and the upper part of the falling film evaporator is provided with a first air inlet. The first air outlet, the steam compressor and the first air inlet are connected in sequence through a pipe. The steam compressor is used to compress low-temperature and low-pressure phenol vapor into high-temperature and high-pressure phenol vapor. The bottom of the evaporator has a first discharge port, and the top of the evaporator has a second inlet port. The first discharge port, the circulating pump, the falling film evaporator, and the second inlet port are connected in sequence by a pipeline. The circulating pump is used to pump the bisphenol F-enriched liquid into the falling film evaporator. The falling film evaporator is used to exchange heat between the high-temperature and high-pressure phenol vapor and the bisphenol F-enriched liquid. The falling film evaporator has a phenol liquid outlet, and the phenol liquid outlet is connected to the phenol recovery tank.

[0008] Furthermore, the falling film evaporator has a second discharge port at the bottom, which is connected to the second inlet. The falling film evaporator has a first liquid inlet at the top, which is connected to the outlet of the circulating pump.

[0009] Furthermore, it also includes a condensate drain valve, which is located between the falling film evaporator and the phenol recovery tank, and the phenol liquid outlet, the condensate drain valve, and the phenol recovery tank are interconnected; The condensate trap is used for the one-way passage of phenol condensate.

[0010] Furthermore, it also includes a condenser; The phenol recovery tank is provided with a second gas outlet and a second liquid inlet. The second gas outlet, the condenser, and the second liquid inlet are connected to each other in sequence through pipelines.

[0011] Furthermore, it also includes a circulating cooling water pipe, wherein the circulating cooling water output end of the circulating cooling water pipe is connected to the circulating cooling water input end of the condenser; The circulating cooling water pipe is equipped with a circulating cooling water regulating valve, which is used to open and close the circulating cooling water pipe.

[0012] Furthermore, it also includes a vacuum pump, a shut-off valve, a first pipe, and a second pipe; The inlet of the first pipe is connected to the outlet of the phenol liquid, the outlet of the first pipe is connected to the steam trap, and the outlet of the first pipe, the second pipe and the vacuum pump are sequentially connected to each other. The shut-off valve is disposed in the second pipeline, and the shut-off valve is used to open and close the second pipeline.

[0013] Furthermore, it also includes a pressure gauge, which is installed on top of the evaporator and is used to detect the pressure of the evaporator.

[0014] Furthermore, it also includes a live steam conveying pipe, the outlet of which is connected to the live steam inlet, and the live steam conveying pipe is used to transport live steam. The live steam transmission pipe is equipped with a gas transmission switch valve, which is used to open and close the live steam transmission pipe.

[0015] Furthermore, it also includes a conveying pipe, the inlet of which is connected to the outlet of the bisphenol F production device, and the outlet of which is connected to the first inlet. The feed pipe is equipped with a liquid infusion switch valve, which is used to open and close the feed pipe.

[0016] The technical solution provided by this utility model can include the following beneficial effects: 1. The system of this technical solution only requires the evaporator to generate steam in the initial stage of system operation. The low-temperature and low-pressure phenol vapor generated during the evaporation process, which originally required cooling water for condensation, is compressed and its quality is improved by the steam compressor. Then it is reused as its own heat source, thereby constructing a highly efficient separation system with high self-circulation, low energy consumption, and low operating cost. It realizes the effective recovery and utilization of the latent heat of low-temperature and low-pressure phenol vapor, while avoiding the cooling water resources required for condensing low-temperature and low-pressure phenol vapor, thereby reducing energy consumption and production costs.

[0017] 2. The bisphenol F reaction mixture is fed into the evaporator through the first inlet. Since the boiling point of bisphenol F in the reaction mixture is generally greater than 250℃, while the boiling point of phenol is 182℃, the two boiling points differ significantly. Therefore, in the initial stage of system operation, live steam is used to heat the bisphenol F reaction mixture, separating it into a bisphenol F-enriched liquid and low-temperature, low-pressure phenol vapor. This achieves the initial separation of the bisphenol F reaction mixture and yields low-temperature, low-pressure phenol vapor that can be compressed.

[0018] 3. This technical solution forms a material circulation channel through the first discharge port, circulating pump, falling film evaporator and the second inlet. The first air outlet, steam compressor and the first air inlet form a system that compresses low-temperature and low-pressure phenol vapor into high-temperature and high-pressure phenol vapor, and provides high-temperature and high-pressure phenol vapor for heat exchange. After heat exchange, the high-temperature and high-pressure phenol vapor condenses into phenol liquid, which facilitates phenol recovery and phenol removal treatment. Attached Figure Description

[0019] Figure 1 This is a schematic diagram of the structure of a bisphenol F dephenolization system according to this utility model.

[0020] The components include: 1. Evaporator, 11. First inlet, 12. First outlet, 13. Second outlet, 14. Live steam inlet, 15. Steam compressor, 2. Falling film evaporator, 3. First inlet, 31. Phenol liquid outlet, 32. First liquid inlet, 33. Circulation pump, 4. Phenol recovery tank, 5. Second outlet, 51. Second liquid inlet, 52. Drain valve, 6. Condenser, 7. Vacuum pump, 8. Shut-off valve, 9. Live steam transmission pipe, 10. First pipeline, 100. Second pipeline, 200. Feed pipe, 300. Detailed Implementation

[0021] The embodiments of this utility model are described in detail below. Examples of these embodiments are shown in the accompanying drawings, wherein the same or similar reference numerals denote the same or similar elements or elements having the same or similar functions throughout. The embodiments described below with reference to the accompanying drawings are exemplary and are only used to explain this utility model, and should not be construed as limiting this utility model.

[0022] This technical solution provides a bisphenol F dephenolization system, including an evaporator 1, a steam compressor 2, a falling film evaporator 3, a circulating pump 4, and a phenol recovery tank 5; The evaporator 1 is provided with a first feed port 11 for feeding the bisphenol F reaction mixture and a live steam inlet 15 for the entry of live steam. The live steam conveying pipe 10 is used to convey live steam. The evaporator 1 is used to separate the bisphenol F reaction mixture to be purified into low-temperature and low-pressure phenol vapor and a liquid enriched with bisphenol F using live steam. The top of the evaporator 1 is provided with a first air outlet 12, and the upper part of the falling film evaporator 3 is provided with a first air inlet 31. The first air outlet 12, the steam compressor 2 and the first air inlet 31 are connected in sequence through a pipe. The steam compressor 2 is used to compress low-temperature and low-pressure phenol vapor into high-temperature and high-pressure phenol vapor. The evaporator 1 has a first discharge port 13 at the bottom and a second inlet port 14 at the top. The first discharge port 13, the circulating pump 4, the falling film evaporator 3, and the second inlet port 14 are connected in sequence by a pipeline. The circulating pump 4 is used to pump the bisphenol F-enriched liquid into the falling film evaporator 3. The falling film evaporator 3 is used to exchange heat between the high-temperature and high-pressure phenol vapor and the bisphenol F-enriched liquid. The falling film evaporator 3 has a phenol liquid outlet 32, and the phenol liquid outlet 32 ​​is connected to the phenol recovery tank 5.

[0023] To address the high energy consumption and inability to recover the latent heat of phenol vapor at low temperatures and pressures in the existing bisphenol F reaction mixture dephenolization process, resulting in high production costs, this technical solution proposes a bisphenol F dephenolization system, such as... Figure 1 As shown, this system converts the low-temperature, low-pressure phenol vapor generated during the phenol removal process into high-temperature, high-pressure phenol vapor by pressurizing and heating it through a steam compressor. This high-temperature, high-pressure steam is then used as a heat source to replace external live steam for evaporating residual phenol in the bisphenol F phenol removal reaction mixture. This achieves effective recovery and utilization of the latent heat of the low-temperature, low-pressure phenol vapor, while avoiding the cooling water resources required for condensing the low-temperature, low-pressure phenol vapor, thereby significantly reducing energy consumption and production costs.

[0024] Specifically, the bisphenol F dephenolization system includes an evaporator 1, a steam compressor 2, a falling film evaporator 3, a circulating pump 4, and a phenol recovery tank 5. The first inlet 11 feeds the bisphenol F reaction mixture into the evaporator 1. Since the boiling point of bisphenol F in the bisphenol F reaction mixture is generally greater than 250℃, while the boiling point of phenol is 182℃, the two boiling points differ significantly. Therefore, in the initial stage of system operation, live steam is used to heat the bisphenol F reaction mixture, separating it into a bisphenol F-enriched liquid and low-temperature, low-pressure phenol vapor. This achieves the initial separation of the bisphenol F reaction mixture and yields low-temperature, low-pressure phenol vapor that can be compressed.

[0025] Furthermore, the top of the evaporator 1 is provided with a first air outlet 12, and the upper part of the falling film evaporator 3 is provided with a first air inlet 31. The first air outlet 12, the steam compressor 2, and the first air inlet 31 are connected in sequence through pipes. Simultaneously, the bottom of the evaporator 1 is provided with a first discharge outlet 13, and the top of the evaporator 1 is provided with a second feed inlet 14. The first discharge outlet 13, the circulating pump 4, the falling film evaporator 3, and the second feed inlet 14 are connected in sequence through pipes. This technical solution forms a material circulation channel through the first discharge outlet 13, the circulating pump 4, the falling film evaporator 3, and the second feed inlet 14. The first air outlet 12, the steam compressor 2, and the first air inlet 31 compress low-temperature, low-pressure phenol vapor into high-temperature, high-pressure phenol vapor, and provide this high-temperature, high-pressure phenol vapor for heat exchange. After heat exchange, the high-temperature, high-pressure phenol vapor condenses into phenol liquid, facilitating phenol recovery and system dephenolization.

[0026] The operating principle of this technical solution is as follows: In the initial stage of system operation, the bisphenol F reaction mixture is heated by the live steam entering from the live steam inlet 15, causing the bisphenol F reaction mixture to separate into a bisphenol F-enriched liquid and low-temperature, low-pressure phenol vapor. Then, utilizing the pressure difference between the inside of the evaporator 1 and the inlet of the steam compressor 2, the low-temperature, low-pressure phenol vapor automatically flows to the steam compressor 2, where it is compressed into high-temperature, high-pressure phenol vapor. After the steam compressor 2 stabilizes, the supply of live steam is stopped. During the automatic flow of the low-temperature, low-pressure phenol vapor to the steam compressor 2, the circulation pump 4 is simultaneously started, pumping the bisphenol F-enriched liquid into the falling film evaporator 3. The high-temperature, high-pressure phenol vapor enters the falling film evaporator 3 through the first inlet 31. After heat exchange between the high-temperature, high-pressure phenol vapor and the bisphenol F-enriched liquid, the phenol vapor condenses into phenol liquid, and the bisphenol F-enriched liquid is then added... The heat source is a gas-liquid mixture (the gas phase of the gas-liquid mixture originates from phenol, which is vaporized by heating a bisphenol F-enriched liquid with high-temperature and high-pressure phenol vapor). The phenol liquid is recovered to the phenol recovery tank 5 through the phenol liquid outlet 32. The gas-liquid mixture is returned to the evaporator 1 through the second inlet 14. Then, the gas-liquid mixture is separated in the evaporator 1 to obtain low-temperature and low-pressure phenol vapor and bisphenol F-enriched liquid. The low-temperature and low-pressure phenol vapor enters the steam compressor 2 and is compressed into high-temperature and high-pressure phenol vapor. The bisphenol F-enriched liquid is pumped into the falling film evaporator 3 by the circulating pump 4. The high-temperature and high-pressure phenol vapor and the bisphenol F-enriched liquid undergo heat exchange again in the falling film evaporator 3. This process is repeated to gradually achieve phenol removal.

[0027] In summary, the system of this technical solution only requires the evaporator 1 to generate steam during the initial operation phase of the system. The low-temperature and low-pressure phenol vapor generated during the evaporation process, which originally required cooling water for condensation, is compressed and its quality is improved by the steam compressor 2. It is then reused as its own heat source, thereby constructing a highly efficient separation system with high self-circulation, low energy consumption, and low operating costs. This achieves effective recovery and utilization of the latent heat of low-temperature and low-pressure phenol vapor, while avoiding the cooling water resources required for condensing low-temperature and low-pressure phenol vapor, thus reducing energy consumption and production costs.

[0028] Furthermore, the working principle of the falling film evaporator 3 is as follows: the bisphenol F-enriched liquid enters the falling film evaporator through the first inlet 33. The bisphenol F-enriched liquid is then uniformly distributed onto the inner wall of the heat exchange tubes, forming a thin liquid film flowing downwards under gravity. This liquid film greatly increases the contact area between the liquid and the high-temperature, high-pressure phenol vapor. Compared to immersing the bisphenol F-enriched liquid in a heat source (such as a jacketed vessel), the heat transfer efficiency and evaporation rate are improved by orders of magnitude, which is beneficial for improving the phenol removal efficiency. In addition, the bisphenol F-enriched liquid flows down rapidly in the form of a thin film, with a very short residence time in the equipment. This minimizes the risk of bisphenol F decomposition, polymerization, or deterioration due to prolonged heating, ensuring the quality of the final bisphenol F obtained.

[0029] To further explain, the falling film evaporator 3 has a second discharge port at its bottom, and the second discharge port is connected to the second inlet 14. The falling film evaporator 3 has a first liquid inlet 33 at its top, and the first liquid inlet 33 is connected to the outlet of the circulating pump 4.

[0030] This technical solution features a second outlet at the bottom of the falling film evaporator 3, through which the gas-liquid mixture is discharged into the evaporation vessel 1. A first inlet 33 is located at the top of the falling film evaporator 3, through which the bisphenol F-enriched liquid enters the evaporator 3. This "top-in, bottom-out" path avoids mixing of the high-purity bisphenol F gas-liquid mixture obtained after heat exchange with the untreated bisphenol F-enriched liquid, thus improving the purity of the final bisphenol F product and the overall system separation efficiency.

[0031] Further explanation: It also includes a steam trap 6, which is located between the falling film evaporator 3 and the phenol recovery tank 5, and the phenol liquid outlet 32, the steam trap 6 and the phenol recovery tank 5 are interconnected; The hydrophobic valve 6 is used for the one-way passage of phenol condensate.

[0032] This technical solution, by setting up a steam trap 6, ensures that the condensed phenol liquid passes through while the phenol vapor does not. This not only helps to ensure the phenol vapor pressure in the falling film evaporator 3, but also helps to ensure that the phenol recovered to the phenol recovery tank 5 is liquid phenol, which is beneficial for the recovery of liquid phenol.

[0033] Further explanation includes condenser 7; The phenol recovery tank 5 has a second air outlet 51 and a second liquid inlet 52. The second air outlet 51, the condenser 7 and the second liquid inlet 52 are connected to each other in sequence through pipes.

[0034] After high-temperature, high-pressure phenol vapor undergoes heat exchange with a bisphenol F-enriched liquid, the resulting phenol liquid still retains pressure and a high temperature. When it is discharged through the steam trap 6 to the phenol recovery tank 5, a flash evaporation effect occurs, generating a small amount of phenol vapor. Therefore, this application incorporates a condenser 7 to condense and recover the phenol vapor generated during flash evaporation to the phenol recovery tank 5, thereby improving the raw material recovery rate.

[0035] Further explanation: It also includes a circulating cooling water pipe, the circulating cooling water output end of which is connected to the circulating cooling water input end of the condenser 7; The circulating cooling water pipe is equipped with a circulating cooling water regulating valve, which is used to open and close the circulating cooling water pipe.

[0036] This technical solution uses circulating cooling water pipes (not shown in the figure) to make the condenser 7 use circulating cooling water as a cold source, so that the phenol vapor generated by flash evaporation can be fully condensed in the condenser 7 to obtain phenol vapor and improve condensation efficiency.

[0037] Furthermore, by setting a circulating cooling water regulating valve on the liquid nitrogen pipe, the flow rate of circulating cooling water in the circulating cooling water pipe is controlled by the circulating cooling water regulating valve to ensure that the temperature of the phenol liquid obtained by condensing the phenol vapor generated by flash evaporation is not lower than 43°C, thus avoiding phenol crystallization and blockage.

[0038] Further explanation: It also includes a vacuum pump 8, a shut-off valve 9, a first pipe 100, and a second pipe 200; The inlet of the first pipe 100 is connected to the phenol liquid outlet 32, the outlet of the first pipe 100 is connected to the steam trap 6, and the outlet of the first pipe 100, the second pipe 200 and the vacuum pump 8 are sequentially connected to each other. The shut-off valve 9 is disposed in the second pipeline 200, and the shut-off valve 9 is used to open and close the second pipeline 200.

[0039] The boiling point of phenol is positively correlated with ambient pressure (approximately 182°C at normal pressure). This technical solution adds a vacuum pump 8, which is connected to the phenol liquid outlet 32 ​​via a second pipe 200 and a first pipe 100, effectively connecting the vacuum pump 8 to the falling film evaporator 3. Since the falling film evaporator 3 is interconnected with the evaporation vessel 1, turning on the vacuum pump 8 allows for depressurization of the evaporation vessel 1, effectively lowering the boiling point of phenol within the system. This reduction in the phenol boiling point allows for heating the solution in the vaporization vessel with lower-pressure live steam, while simultaneously lowering the operating temperature of the steam compressor 2, thereby reducing operating costs and equipment investment.

[0040] Furthermore, this technical solution incorporates a shut-off valve 9. When a vacuum is required inside the evaporator 1, the shut-off valve 9 is opened; when the vacuum level in the evaporator 1 is sufficient or when phenol droplets need to be recovered, the shut-off valve 9 is closed. During the phenol recovery process, closing the shut-off valve 9 allows the phenol liquid to enter the phenol recovery tank 5 through the condensate trap 6. Additionally, by controlling the vacuuming speed through the shut-off valve 9, the vacuum level of the evaporator 1 can be made controllable.

[0041] Further explanation: It also includes a pressure gauge, which is installed on the top of the evaporator 1 and is used to detect the pressure of the evaporator 1.

[0042] By using a pressure gauge (not shown in the diagram) to monitor the pressure in evaporator 1 during the vacuuming process, the operator can precisely adjust the vacuuming speed using shut-off valve 9 based on pressure changes. If the pressure gauge shows a high pressure, the vacuum level in evaporator 1 is insufficient; in this case, the opening of shut-off valve 9 can be increased to accelerate the vacuuming process. Conversely, if the pressure is low, the vacuum level in evaporator 1 is too low; in this case, the opening of shut-off valve 9 can be decreased or even closed to reduce the vacuuming speed. This precise adjustment ensures that the vacuum level in evaporator 1 can be adjusted promptly according to actual needs, improving the flexibility of the system.

[0043] Further explanation: It also includes a live steam transmission pipe 10, the outlet of which is connected to the live steam inlet 15, and the live steam transmission pipe 10 is used to transport live steam. The live steam transmission pipe 10 is equipped with a gas transmission switch valve, which is used to open and close the live steam transmission pipe 10.

[0044] This technical solution involves setting up a live steam supply pipe 10. In the initial stage of system operation, the live steam supply pipe 10 is used to pass live steam through the evaporation kettle 1. The live steam heats the bisphenol F reaction mixture, thereby separating the bisphenol F reaction mixture into a liquid enriched with bisphenol F and low-temperature, low-pressure phenol vapor, which is beneficial for the separation and purification of the bisphenol F reaction mixture.

[0045] Furthermore, by setting a gas supply switch valve (not shown in the figure), the live steam supply pipe 10 can be opened and closed according to actual needs, thereby controlling whether live steam enters the evaporator 1. For example, at the initial stage of system operation, the gas supply switch valve is opened to allow live steam to enter the evaporator 1 to heat the bisphenol F reaction mixture, achieving its separation into a bisphenol F-enriched liquid and low-temperature, low-pressure phenol vapor; after the steam compressor 2 is running stably, the gas supply switch valve is closed to stop the supply of live steam, thereby improving the flexibility of the device.

[0046] Further explanation includes a conveying pipe 300, the inlet of which is connected to the outlet of the bisphenol F production device, and the outlet of which is connected to the first inlet 11. The feed pipe 300 is equipped with a liquid infusion switch valve, which is used to open and close the feed pipe 300.

[0047] By setting a liquid inlet switch valve (not shown in the figure), the feed pipe 300 can be opened and closed according to actual needs, thereby controlling whether the bisphenol F reaction mixture enters the evaporator 1. For example, at the initial stage of system operation, the liquid inlet switch valve is opened to allow the bisphenol F reaction mixture to enter the evaporator 1; while during peak system operation, when the amount of bisphenol F reaction mixture increases, the liquid inlet switch valve can be closed to prevent excessive bisphenol F reaction mixture from entering the system and being unable to be processed in time, thus ensuring the stability of system operation.

[0048] It should be noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to limit the exemplary embodiments according to this application. As used herein, the singular form is intended to include the plural form as well, unless the context clearly indicates otherwise. Furthermore, it should be understood that when the terms "comprising" and / or "including" are used in this specification, they indicate the presence of features, steps, operations, devices, components, and / or combinations thereof.

[0049] Unless otherwise specifically stated, the relative arrangement, numerical expressions, and values ​​of the components and steps described in these embodiments do not limit the scope of this invention. It should also be understood that, for ease of description, the dimensions of the various parts shown in the drawings are not drawn to actual scale. Techniques, methods, and devices known to those skilled in the art may not be discussed in detail, but where appropriate, such techniques, methods, and devices should be considered part of the specification. In all examples shown and discussed herein, any specific values ​​should be interpreted as merely exemplary and not as limitations. Therefore, other examples of exemplary embodiments may have different values. It should be noted that similar reference numerals and letters in the following drawings denote similar items; therefore, once an item is defined in one drawing, it need not be further discussed in subsequent drawings.

[0050] In the description of this utility model, it should be understood that the directional terms such as "front, back, up, down, left, right", "horizontal, vertical, horizontal" and "top, bottom" 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. Unless otherwise stated, these directional terms 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, and therefore should not be construed as a limitation on the scope of protection of this utility model. The directional terms "inner" and "outer" refer to the inner and outer contours of each component itself.

[0051] For ease of description, spatial relative terms such as "above," "on top of," "on the upper surface of," "above," etc., are used herein to describe the spatial positional relationship of a device or feature as shown in the figures to other devices or features. It should be understood that spatial relative terms are intended to encompass different orientations in use or operation beyond the orientation of the device as described in the figures. For example, if the device in the figures were inverted, a device described as "above" or "on top of" other devices or structures would subsequently be positioned as "below" or "under" other devices or structures. Thus, the exemplary term "above" can include both "above" and "below." The device may also be positioned in other different ways (rotated 90 degrees or in other orientations), and the spatial relative descriptions used herein will be interpreted accordingly.

[0052] Furthermore, it should be noted that the use of terms such as "first" and "second" to define components is merely for the purpose of distinguishing the corresponding components. Unless otherwise stated, the above terms have no special meaning and therefore cannot be construed as limiting the scope of protection of this utility model.

[0053] It should be noted that the terms "first," "second," etc., used in the specification, claims, and accompanying drawings of this application are used to distinguish similar objects and are not necessarily used to describe a specific order or sequence. It should be understood that such data can be interchanged where appropriate so that the embodiments of this application described herein can be implemented in sequences other than those illustrated or described herein.

[0054] The technical principles of this utility model have been described above with reference to specific embodiments. These descriptions are merely for explaining the principles of this utility model and should not be construed as limiting the scope of protection of this utility model in any way. Based on this explanation, those skilled in the art can readily conceive of other specific embodiments of this utility model without any inventive effort, and these embodiments will all fall within the scope of protection of this utility model.

Claims

1. A bisphenol F dephenolization system, characterized in that: Includes an evaporator, a steam compressor, a falling film evaporator, a circulating pump, and a phenol recovery tank; The evaporator is provided with a first feed port for feeding the bisphenol F reaction mixture and a live steam inlet for entering the live steam. The live steam conveying pipe is used to convey live steam. The evaporator is used to use live steam to separate the bisphenol F reaction mixture to be purified into low-temperature, low-pressure phenol vapor and a liquid enriched with bisphenol F. The top of the evaporator is provided with a first air outlet, and the upper part of the falling film evaporator is provided with a first air inlet. The first air outlet, the steam compressor and the first air inlet are connected in sequence through a pipe. The steam compressor is used to compress low-temperature and low-pressure phenol vapor into high-temperature and high-pressure phenol vapor. The bottom of the evaporator has a first discharge port, and the top of the evaporator has a second inlet port. The first discharge port, the circulating pump, the falling film evaporator, and the second inlet port are connected in sequence by a pipeline. The circulating pump is used to pump the bisphenol F-enriched liquid into the falling film evaporator. The falling film evaporator is used to exchange heat between the high-temperature and high-pressure phenol vapor and the bisphenol F-enriched liquid. The falling film evaporator has a phenol liquid outlet, and the phenol liquid outlet is connected to the phenol recovery tank.

2. The bisphenol F dephenolization system according to claim 1, characterized in that: The falling film evaporator has a second discharge port at the bottom, and the second discharge port is connected to the second inlet port. The falling film evaporator has a first liquid inlet at the top, which is connected to the outlet of the circulating pump.

3. The bisphenol F dephenolization system according to claim 1, characterized in that: It also includes a condensate drain valve, which is located between the falling film evaporator and the phenol recovery tank, and the phenol liquid outlet, the condensate drain valve and the phenol recovery tank are interconnected; The condensate trap is used for the one-way passage of phenol condensate.

4. The bisphenol F dephenolization system according to claim 1, characterized in that: It also includes the condenser; The phenol recovery tank is provided with a second gas outlet and a second liquid inlet. The second gas outlet, the condenser, and the second liquid inlet are connected to each other in sequence through pipelines.

5. The bisphenol F dephenolization system according to claim 4, characterized in that: It also includes a circulating cooling water pipe, wherein the circulating cooling water output end of the circulating cooling water pipe is connected to the circulating cooling water input end of the condenser; The circulating cooling water pipe is equipped with a circulating cooling water regulating valve, which is used to open and close the circulating cooling water pipe.

6. The bisphenol F dephenolization system according to claim 3, characterized in that: It also includes a vacuum pump, a shut-off valve, a first pipe, and a second pipe; The inlet of the first pipe is connected to the outlet of the phenol liquid, the outlet of the first pipe is connected to the steam trap, and the outlet of the first pipe, the second pipe and the vacuum pump are sequentially connected to each other. The shut-off valve is disposed in the second pipeline, and the shut-off valve is used to open and close the second pipeline.

7. A bisphenol F dephenolization system according to claim 6, characterized in that: It also includes a pressure gauge, which is installed on top of the evaporator and is used to detect the pressure of the evaporator.

8. The bisphenol F dephenolization system according to claim 1, characterized in that: It also includes a live steam transmission pipe, the outlet of which is connected to the live steam inlet, and the live steam transmission pipe is used to transport live steam. The live steam transmission pipe is equipped with a gas transmission switch valve, which is used to open and close the live steam transmission pipe.

9. A bisphenol F dephenolization system according to claim 1, characterized in that: It also includes a conveying pipe, the inlet of which is connected to the outlet of the bisphenol F production device, and the outlet of which is connected to the first inlet. The feed pipe is equipped with a liquid infusion switch valve, which is used to open and close the feed pipe.

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