A continuous production system of bisphenol f

Abstract

The utility model relates to a bisphenol F dephenol technology field especially relates to a kind of bisphenol F's continuous production system, including phenol storage device, formaldehyde storage device, catalyst storage device, premixing tank, preheater, tubular reactor and falling film evaporator;The discharge port of phenol storage device, the discharge port of formaldehyde storage device and the discharge port of catalyst storage device are all interconnected with the feed inlet of premixing tank by pipeline;Premixing tank, preheater, tubular reactor and the falling film evaporator are sequentially interconnected;Falling film evaporator is provided with water vapor inlet and first phenol steam outlet.The continuous production system of bisphenol F proposed in the utility model is beneficial to improve production efficiency and product quality consistency under the premise, to improve the purity of product, to overcome the deficiencies in the prior art.

Description

Technical Field

[0001] This utility model relates to the field of bisphenol F removal technology, and in particular to a continuous production system for bisphenol F. 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] The existing method for preparing bisphenol F involves first preparing crude bisphenol F using a batch process, and then separating and purifying the crude product using a batch evaporator to obtain bisphenol F. However, the above method for synthesizing bisphenol F has the following drawbacks: (1) During the synthesis stage, the batch production method requires each batch of reaction to go through feeding, reaction, discharge and cleaning, which consumes a lot of non-productive time and has low production efficiency. At the same time, the initial reaction conditions of each batch of material are different and the mixing and heat transfer in the middle and later stages of the reaction are uneven, which intensifies the side reactions, making the ratio of product isomers and the content of impurities unstable, resulting in large fluctuations in product quality. (2) In the dephenolization stage (i.e. purification stage), the material is processed in batches using a batch evaporator. Due to the low mass and heat transfer efficiency of the material in the batch evaporator and the presence of a thick liquid layer, the material takes a long time to reach the evaporation temperature. At the same time, the volatile components have a large resistance to escape, which leads to the prolonged residence time of heat-sensitive bisphenol F in the high-temperature environment, making it easier for decomposition and condensation reactions to occur, resulting in increased product impurities and reduced product purity.

[0006] In summary, the existing technology for producing bisphenol F suffers from drawbacks such as low production efficiency, large fluctuations in product quality, and low product purity. Utility Model Content

[0007] The purpose of this invention is to propose a continuous production system for bisphenol F, which is beneficial to improve product purity while increasing production efficiency and product quality consistency, thereby overcoming the shortcomings of the prior art.

[0008] To achieve this objective, the present invention adopts the following technical solution: A continuous production system for bisphenol F includes a phenol storage device, a formaldehyde storage device, a catalyst storage device, a premix tank, a preheater, a tubular reactor, and a falling film evaporator; the phenol storage device is used to store phenol, the formaldehyde storage device is used to store formaldehyde, and the catalyst storage device is used to store catalyst. The outlets of the phenol storage device, the formaldehyde storage device, and the catalyst storage device are all connected to the inlet of the premixing tank via pipelines; the premixing tank is used to mix phenol, formaldehyde, and catalyst evenly to obtain a mixture. The premix tank, the preheater, the tubular reactor, and the falling film evaporator are connected in sequence to each other. The preheater is used to preheat the mixture, and the tubular reactor is used to react the preheated mixture to obtain crude bisphenol F product. The falling film evaporator has a steam inlet and a first phenol vapor outlet. The steam inlet is connected to a steam supply source. The falling film evaporator is used to separate crude bisphenol F into phenol vapor and first bisphenol F liquid. The first phenol vapor outlet is used to discharge phenol vapor.

[0009] Furthermore, it also includes a high-temperature and high-pressure steam input pipe, which is connected between the steam supply source and the falling film evaporator; The high-temperature and high-pressure steam input pipe is equipped with a gas supply switch valve, which is used to open and close the high-temperature and high-pressure steam input pipe.

[0010] Furthermore, it also includes thin-film evaporators; The falling film evaporator is provided with a first liquid outlet; the thin film evaporator is provided with a heat transfer oil inlet, a liquid inlet, and a second phenol vapor outlet, and the liquid inlet is connected to the first liquid outlet. The heat transfer oil inlet is connected to the heat transfer oil supply source and is interconnected. The thin film evaporator is used to separate the first bisphenol F liquid into phenol vapor and the second bisphenol F liquid. The second phenol vapor outlet is used to discharge phenol vapor.

[0011] Furthermore, it also includes a high-temperature heat transfer oil inlet pipe, which is connected between the heat transfer oil supply source and the thin-film evaporator; The high-temperature heat transfer oil inlet pipe is equipped with an oil supply switch valve, which is used to open and close the high-temperature heat transfer oil inlet pipe.

[0012] Furthermore, it also includes a first feed pipe and a first bisphenol F liquid collection tank; The inlet of the first conveying pipe is connected to the first outlet, and the outlet of the first conveying pipe is connected to both the inlet and the first bisphenol F liquid collection tank. A first valve is provided between the outlet of the first conveying pipe and the inlet of the liquid, and the first valve is used to adjust the liquid inlet flow rate. A second valve is provided between the outlet of the first conveying pipe and the first bisphenol F liquid collection tank. The second valve is used to adjust the liquid inflow of the first bisphenol F liquid collection tank.

[0013] Furthermore, it also includes an extruder; the thin film evaporator is provided with a second liquid outlet, the feed port of the extruder is connected to the second liquid outlet, and the extruder is used to convert the second bisphenol F liquid into bisphenol F solid.

[0014] Furthermore, it also includes a weighing and bagging machine, the inlet of which is connected to the outlet of the extruder.

[0015] Furthermore, it also includes a phenol recovery tank and a condenser; The first phenol vapor outlet and the second phenol vapor outlet are both connected to the feed inlet of the condenser through pipelines, and the discharge outlet of the condenser is connected to the feed inlet of the phenol recovery tank through a pipeline. The condenser is used to convert phenol vapor into phenol liquid, and the phenol recovery tank 500 is used to recover the phenol liquid.

[0016] Furthermore, the phenol recovery tank and the phenol storage device are arranged side by side, and the outlet of the phenol recovery tank is connected to the inlet of the premix tank.

[0017] Furthermore, it also includes a low-temperature, low-pressure steam output pipe; The falling film evaporator has a steam outlet, which is connected to the inlet of the low-temperature and low-pressure steam output pipe via a pipe. The low-temperature and low-pressure steam output pipe is used to output low-temperature and low-pressure steam.

[0018] The technical solution provided by this utility model can include the following beneficial effects: 1. This technology, through the coordinated operation of phenol storage devices, formaldehyde storage devices, catalyst storage devices, premixing tanks, preheaters, tubular reactors, and falling film evaporators, completely eliminates the waiting time between feeding, reaction, discharging, and cleaning processes in batch production, achieving continuous production throughout the entire process, keeping the system in operation at all times, and greatly improving production efficiency.

[0019] 2. The temperature, pressure, and residence time experienced by materials at any location within the tubular reactor remain consistent and can be precisely controlled. This means the tubular reactor provides a stable and uniform reaction environment, effectively avoiding quality fluctuations caused by initial temperature differences between batches and uneven heating / cooling rates during the reaction, as seen in batch production. Furthermore, the materials entering the tubular reactor are uniformly mixed in a premixing tank and preheated in a preheater, resulting in good temperature and concentration uniformity. In addition, the flow of materials from the preheater to the tubular reactor itself promotes further mixing, ensuring the overall temperature and concentration of the reaction system remain uniform and stable. Therefore, all materials react under essentially identical conditions, effectively suppressing side reactions and ensuring stable product isomer ratios, controllable impurity content, and ultimately, highly consistent product quality with minimal fluctuations.

[0020] 3. The falling film evaporator is equipped with a steam inlet, which is connected to a steam supply source. Since the boiling point of bisphenol F is generally greater than 250℃, while the boiling point of phenol is 182℃, the difference in boiling points is significant. Therefore, in the falling film evaporator, the high-temperature, high-pressure steam provided by the steam supply source exchanges heat with the crude bisphenol F product, allowing the phenol contained in the crude bisphenol F product to rapidly vaporize and be discharged through the first phenol steam outlet, thereby achieving efficient separation and purification of the crude bisphenol F product. Attached Figure Description

[0021] Figure 1 This is a schematic diagram of the structure of a continuous production system for bisphenol F according to this utility model.

[0022] Figure 2 This utility model relates to a continuous production system for bisphenol F. Figure 1 Enlarged view of point A in the middle.

[0023] The system includes: phenol storage device 1, formaldehyde storage device 2, catalyst storage device 3, premix tank 4, preheater 5, tubular reactor 6, falling film evaporator 7, steam inlet 71, first liquid outlet 72, first phenol vapor outlet 73, steam outlet 74, high temperature and high pressure steam input pipe 8, thin film evaporator 9, heat transfer oil inlet 91, liquid inlet 92, second liquid outlet 93, second phenol vapor outlet 94, first conveying pipe 10, first bisphenol F liquid collection tank 100, extruder 200, high temperature heat transfer oil input pipe 300, weighing and bagging machine 400, phenol recovery tank 500, and low temperature and low pressure steam output pipe 600. Detailed Implementation

[0024] 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.

[0025] This technical solution provides a continuous production system for bisphenol F, including a phenol storage device 1, a formaldehyde storage device 2, a catalyst storage device 3, a premix tank 4, a preheater 5, a tubular reactor 6, and a falling film evaporator 7; the phenol storage device 1 is used to store phenol, the formaldehyde storage device 2 is used to store formaldehyde, and the catalyst storage device 3 is used to store catalyst. The outlets of the phenol storage device 1, the formaldehyde storage device 2, and the catalyst storage device 3 are all connected to the inlet of the premixing tank 4 via pipelines; the premixing tank 4 is used to mix phenol, formaldehyde, and catalyst evenly to obtain a mixture. The premix tank 4, the preheater 5, the tubular reactor 6 and the falling film evaporator 7 are connected to each other in sequence. The preheater 5 is used to preheat the mixture, and the tubular reactor 6 is used to react the preheated mixture to obtain crude bisphenol F product. The falling film evaporator 7 has a steam inlet 71 and a first phenol vapor outlet 73. The steam inlet 71 is connected to a steam supply source. The falling film evaporator 7 is used to separate the crude bisphenol F product into phenol vapor and first bisphenol F liquid. The first phenol vapor outlet 73 is used to discharge phenol vapor.

[0026] To address the technical problems of low production efficiency, large product quality fluctuations, and low product purity in the existing bisphenol F production technology, this technical solution proposes a continuous production system for bisphenol F. By improving the production system, it is beneficial to improve product purity while increasing production efficiency and product quality consistency.

[0027] Specifically, in this technical solution, the outlets of the phenol storage device 1, formaldehyde storage device 2, and catalyst storage device 3 are all connected to the inlet of the premixing tank 4 via pipelines; the premixing tank 4, preheater 5, tubular reactor 6, and falling film evaporator 7 are sequentially connected to each other; the falling film evaporator 7 has a steam inlet 71 and a first phenol vapor outlet 73, and the steam inlet 71 is connected to a steam supply source. Through the above arrangement, the raw materials (phenol, formaldehyde, and catalyst) in this technical solution are continuously mixed in the premixing tank 4 to form a mixture. After passing through the preheater 5, the mixture continuously enters the tubular reactor 6 to react and generate crude bisphenol F product. Subsequently, the crude bisphenol F product continuously flows into the falling film evaporator 7 for separation and purification. This technology, through the coordinated operation of phenol storage device 1, formaldehyde storage device 2, catalyst storage device 3, premix tank 4, preheater 5, tubular reactor 6, and falling film evaporator 7, completely eliminates the waiting time between feeding, reaction, discharging, and cleaning processes in batch production, realizing continuous production throughout the entire process, keeping the system in operation at all times, and greatly improving production efficiency.

[0028] Furthermore, the temperature, pressure, and residence time experienced by materials at any location within the tubular reactor 6 are consistent and precisely controllable. This means the tubular reactor 6 provides a stable and uniform reaction environment, effectively avoiding quality fluctuations caused by initial temperature differences in each batch and uneven heating / cooling rates during the reaction, common in batch production. Simultaneously, the materials entering the tubular reactor 6 are uniformly mixed in the premixing tank 4 and preheated by the preheater 5, resulting in good temperature and concentration uniformity. Moreover, the flow of materials from the preheater 5 to the tubular reactor 6 further promotes mixing, ensuring the overall temperature and concentration of the reaction system remain uniform and stable. Therefore, all materials react under essentially uniform conditions, side reactions are effectively suppressed, ensuring stable product isomer ratios, controllable impurity content, and ultimately, highly consistent product quality with minimal fluctuations.

[0029] Furthermore, the falling film evaporator 7 is equipped with a steam inlet 71, which is connected to a steam supply source. Since the boiling point of bisphenol F is generally greater than 250℃, while the boiling point of phenol is 182℃, the two have a significant difference in boiling points. Therefore, in the falling film evaporator 7, the high-temperature, high-pressure steam provided by the steam supply source exchanges heat with the crude bisphenol F product, allowing the phenol contained in the crude bisphenol F product to rapidly vaporize and be discharged through the first phenol steam outlet 73, thereby achieving efficient separation and purification of the crude bisphenol F product.

[0030] The working principle of the falling film evaporator 7 is as follows: After the crude bisphenol F product enters the equipment, it is evenly distributed on the inner wall of the heat exchange tube and forms a downward-flowing thin liquid film under the action of gravity. Since the liquid evaporates in the form of a thin film, the heat transfer efficiency is extremely high, and the required heating time is extremely short (usually only a few seconds to tens of seconds). This avoids the long time required for the crude bisphenol F product to reach the evaporation temperature, which would prolong its residence time in a high-temperature environment and lead to thermal decomposition or condensation side reactions. This effectively reduces the generation of impurities and helps to ensure the purity of the final first bisphenol F liquid.

[0031] Further explanation: It also includes a high-temperature and high-pressure steam input pipe 8, which is connected between the steam supply source and the falling film evaporator 7; The high-temperature and high-pressure steam input pipe 8 is equipped with a gas supply switch valve, which is used to open and close the high-temperature and high-pressure steam input pipe 8.

[0032] This technical solution uses a high-temperature, high-pressure steam input pipe 8 to deliver high-temperature, high-pressure steam to the falling film evaporator 7 during system operation. The high-temperature, high-pressure steam heats the crude bisphenol F product, thereby separating the crude bisphenol F product into phenol vapor and first bisphenol F liquid, which is beneficial for the separation and purification of the crude bisphenol F product.

[0033] Furthermore, by setting a gas supply switch valve (not shown in the figure), the high-temperature and high-pressure steam input pipe 8 can be opened and closed according to actual needs, thereby controlling whether high-temperature and high-pressure steam enters the falling film evaporator 7. For example, during system operation, by opening the gas supply switch valve, high-temperature and high-pressure steam enters the falling film evaporator 7 and heats the bisphenol F reaction mixture to achieve its separation and purification; after the crude bisphenol F product is separated and purified, the gas supply switch valve is closed to stop the supply of high-temperature and high-pressure steam, thereby improving the flexibility of the device.

[0034] Further explanation includes a thin-film evaporator 9; The falling film evaporator 7 is provided with a first liquid outlet 72; the thin film evaporator 9 is provided with a heat transfer oil inlet 91, a liquid inlet 92, and a second phenol vapor outlet 94, wherein the liquid inlet 92 is connected to the first liquid outlet 72. The heat transfer oil inlet 91 is connected to the heat transfer oil supply source and is interconnected. The thin film evaporator 9 is used to separate the first bisphenol F liquid into phenol vapor and the second bisphenol F liquid. The second phenol vapor outlet 94 is used to discharge phenol vapor.

[0035] This technical solution further separates and purifies the first bisphenol F liquid by setting up a thin-film evaporator 9, and allows the phenol vapor generated during the separation process to be discharged through the second phenol vapor outlet 94, thereby improving the obtained bisphenol F liquid and meeting the requirements for higher purity of bisphenol F liquid.

[0036] Further explanation: It also includes a high-temperature heat transfer oil inlet pipe 300, which is connected between the heat transfer oil supply and the thin-film evaporator 9; The high-temperature heat transfer oil inlet pipe 300 is equipped with an oil supply switch valve, which is used to open and close the high-temperature heat transfer oil inlet pipe 300.

[0037] This technical solution uses a high-temperature heat transfer oil inlet pipe 300 to deliver high-temperature heat transfer oil to the thin-film evaporator 9 during system operation. The high-temperature heat transfer oil heats the first bisphenol F liquid, thereby separating the first bisphenol F liquid into phenol vapor and the second bisphenol F liquid, which is beneficial for further separation and purification of the first bisphenol F liquid.

[0038] Further explanation: It also includes a first conveying pipe 10 and a first bisphenol F liquid collection tank 100; The inlet of the first conveying pipe 10 is connected to the first outlet 72, and the outlet of the first conveying pipe 10 is connected to the inlet 92 and the first bisphenol F liquid collection tank 100, respectively. A first valve is provided between the outlet of the first conveying pipe 10 and the inlet 92, and the first valve is used to adjust the liquid inlet 92. A second valve is provided between the outlet of the first conveying pipe 10 and the first bisphenol F liquid collection tank 100. The second valve is used to adjust the liquid inflow of the first bisphenol F liquid collection tank 100.

[0039] This technical solution sets up a first feed pipe 10 and a first bisphenol F liquid collection tank 100. When further separation and purification are needed, the first valve is opened and the second valve is closed, so that the first bisphenol F liquid can be further separated and purified using the thin-film evaporator 9. When the first bisphenol F liquid needs to be collected, the first valve is closed and the second valve is opened, so that the first bisphenol F liquid can be collected using the first bisphenol F liquid collection tank 100, thereby increasing the flexibility of the system.

[0040] Further explanation includes an extruder 200; the thin film evaporator 9 is provided with a second liquid outlet 93, the feed inlet of the extruder 200 is connected to the second liquid outlet 93, and the extruder 200 is used to convert the second bisphenol F liquid into bisphenol F solid.

[0041] This technical solution involves setting up an extruder 200, where the second bisphenol F liquid flows to and is cooled in the extruder 9. The extruder 9 then granulates the cooled second bisphenol F liquid to obtain bisphenol F solid, which improves the storage convenience of the bisphenol F liquid.

[0042] To further explain, it also includes a weighing and bagging machine 400, the inlet of which is connected to the outlet of the extruder 200.

[0043] This technical solution uses a weighing and bagging machine 400 to collect and weigh bisphenol F solids, which not only provides a centralized collection point for bisphenol F solids, but also facilitates the packaging of bisphenol F solids according to actual needs.

[0044] Further details include the phenol recovery tank 500 and the condenser; The first phenol vapor outlet 73 and the second phenol vapor outlet 94 are both connected to the feed inlet of the condenser through pipelines, and the discharge outlet of the condenser is connected to the feed inlet of the phenol recovery tank 500 through a pipeline. The condenser is used to convert phenol vapor into phenol liquid, and the phenol recovery tank 500 is used to recover the phenol liquid.

[0045] This application includes a phenol recovery tank 500 and a condenser (not shown in the figure). The condenser converts the phenol vapor output from the first phenol vapor outlet and the second phenol vapor outlet into phenol liquid and recovers it to the phenol recovery tank 500, thereby improving the recovery rate of raw materials.

[0046] To further explain, the phenol recovery tank 500 is arranged in parallel with the phenol storage device 1, and the outlet of the phenol recovery tank 500 is connected to the inlet of the premix tank 4.

[0047] This technical solution, through the above-mentioned setup, facilitates the use of phenol liquid collected in phenol recovery tank 500 in the production of bisphenol F, thereby improving the utilization rate of phenol liquid and reducing the raw material cost of bisphenol F production.

[0048] Further explanation includes a low-temperature, low-pressure steam output pipe 600; The falling film evaporator 7 has a steam outlet 74, which is connected to the inlet of the low-temperature and low-pressure steam output pipe 600 through a pipe. The low-temperature and low-pressure steam output pipe 600 is used to output low-temperature and low-pressure steam.

[0049] This technical solution collects the low-temperature, low-pressure water vapor obtained during the heat exchange process between high-temperature, high-pressure water vapor and crude bisphenol F product by setting up a low-temperature, low-pressure water vapor output pipe 600. This facilitates the collection and utilization of low-temperature, low-pressure water vapor and improves its utilization rate.

[0050] It should be noted that the terms "high-temperature, high-pressure steam" and "low-temperature, low-pressure steam" in this technical solution are relative. Specifically, the high-temperature, high-pressure steam has a temperature of 160-170℃ and a pressure of 6-8 kg / cm². 2 Low-temperature, low-pressure water vapor has a temperature of 130-140℃ and a pressure of 2.7-3.6 kg / cm³. 2 Furthermore, all of the above parameters are standard parameters within the field.

[0051] 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.

[0052] 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.

[0053] 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.

[0054] 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.

[0055] 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.

[0056] 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.

[0057] 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 continuous production system for bisphenol F, characterized in that: It includes a phenol storage device, a formaldehyde storage device, a catalyst storage device, a premix tank, a preheater, a tubular reactor, and a falling film evaporator; the phenol storage device is used to store phenol, the formaldehyde storage device is used to store formaldehyde, and the catalyst storage device is used to store catalyst. The outlets of the phenol storage device, the formaldehyde storage device, and the catalyst storage device are all connected to the inlet of the premixing tank via pipelines; the premixing tank is used to mix phenol, formaldehyde, and catalyst evenly to obtain a mixture. The premix tank, the preheater, the tubular reactor, and the falling film evaporator are connected in sequence to each other. The preheater is used to preheat the mixture, and the tubular reactor is used to react the preheated mixture to obtain crude bisphenol F product. The falling film evaporator has a steam inlet and a first phenol vapor outlet. The steam inlet is connected to a steam supply source. The falling film evaporator is used to separate crude bisphenol F into phenol vapor and first bisphenol F liquid. The first phenol vapor outlet is used to discharge phenol vapor.

2. The continuous production system for bisphenol F according to claim 1, characterized in that: It also includes a high-temperature and high-pressure steam input pipe, which is connected between the steam supply source and the falling film evaporator; The high-temperature and high-pressure steam input pipe is equipped with a gas supply switch valve, which is used to open and close the high-temperature and high-pressure steam input pipe.

3. The continuous production system for bisphenol F according to claim 2, characterized in that: It also includes thin-film evaporators; The falling film evaporator is provided with a first liquid outlet; the thin film evaporator is provided with a heat transfer oil inlet, a liquid inlet, and a second phenol vapor outlet, and the liquid inlet is connected to the first liquid outlet. The heat transfer oil inlet is connected to the heat transfer oil supply source and is interconnected. The thin film evaporator is used to separate the first bisphenol F liquid into phenol vapor and the second bisphenol F liquid. The second phenol vapor outlet is used to discharge phenol vapor.

4. The continuous production system for bisphenol F according to claim 3, characterized in that: It also includes a high-temperature heat transfer oil inlet pipe, which is connected between the heat transfer oil supply and the thin-film evaporator; The high-temperature heat transfer oil inlet pipe is equipped with an oil supply switch valve, which is used to open and close the high-temperature heat transfer oil inlet pipe.

5. A continuous production system for bisphenol F according to claim 3, characterized in that: It also includes a first feed pipe and a first bisphenol F liquid collection tank; The inlet of the first conveying pipe is connected to the first outlet, and the outlet of the first conveying pipe is connected to both the inlet and the first bisphenol F liquid collection tank. A first valve is provided between the outlet of the first conveying pipe and the inlet of the liquid, and the first valve is used to adjust the liquid inlet flow rate. A second valve is provided between the outlet of the first conveying pipe and the first bisphenol F liquid collection tank. The second valve is used to adjust the liquid inflow of the first bisphenol F liquid collection tank.

6. A continuous production system for bisphenol F according to claim 5, characterized in that: It also includes an extruder; the thin film evaporator is provided with a second liquid outlet, the feed port of the extruder is connected to the second liquid outlet, and the extruder is used to convert the second bisphenol F liquid into bisphenol F solid.

7. A continuous production system for bisphenol F according to claim 6, characterized in that: It also includes a weighing and bagging machine, the inlet of which is connected to the outlet of the extruder.

8. A continuous production system for bisphenol F according to claim 3, characterized in that: It also includes phenol recovery tanks and condensers; The first phenol vapor outlet and the second phenol vapor outlet are both connected to the feed inlet of the condenser through pipelines, and the discharge outlet of the condenser is connected to the feed inlet of the phenol recovery tank through a pipeline. The condenser is used to convert phenol vapor into phenol liquid, and the phenol recovery tank is used to recover the phenol liquid.

9. A continuous production system for bisphenol F according to claim 8, characterized in that: The phenol recovery tank and the phenol storage device are arranged side by side, and the outlet of the phenol recovery tank is connected to the inlet of the premix tank.

10. A continuous production system for bisphenol F according to claim 3, characterized in that: It also includes a low-temperature, low-pressure steam output pipe; The falling film evaporator has a steam outlet, which is connected to the inlet of the low-temperature and low-pressure steam output pipe via a pipe. The low-temperature and low-pressure steam output pipe is used to output low-temperature and low-pressure steam.

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