Reactive extrusion device for continuously preparing phenolic resin

Abstract

The utility model relates to the technical field of phenolic resin, and discloses a reactive extrusion device for continuously preparing phenolic resin, which comprises a horizontal reactor, the horizontal reactor is connected with a melt gear pump, the melt gear pump is connected with a reaction devolatilization extruder, the horizontal reactor is provided with a liquid feeding machine, and the liquid feeding machine is connected with the reaction devolatilization extruder. The reaction devolatilization extruder is provided with a powder feeding machine, the reaction devolatilization extruder is sequentially provided with a vacuum device and a template, and compared with a traditional batch-type reaction kettle method, the continuous preparation of phenolic resin is realized by adopting a continuous production process, the production efficiency and the yield are remarkably improved, and the production cost is reduced. The vacuum exhaust ports are formed in the horizontal reactor and the reaction devolatilization extruder, gas generated in the reaction process is effectively exhausted, volatile components are reduced, the resin quality is improved, meanwhile, the pressure sensor is installed at the key position of the extruder, the pressure change in the reaction process is monitored in real time, and the safety and stability of the production process are ensured.

Description

Technical Field

[0001] This utility model relates to the field of phenolic resin technology, specifically to a reactive extrusion device for continuous preparation of phenolic resin. Background Technology

[0002] Phenolic resin is an important thermosetting polymer material with excellent mechanical properties, heat resistance, chemical corrosion resistance, and insulation properties, and is widely used in composite materials, adhesives, coatings, electronic packaging, and other fields. Traditional phenolic resin preparation processes typically employ a batch reactor method, where phenol and formaldehyde undergo a polycondensation reaction in a reactor under the action of acidic or alkaline catalysts. However, this traditional method has the following limitations: the batch reactor method has a long reaction time, typically requiring several hours or even longer to complete the polycondensation reaction, resulting in low production efficiency; continuous heating and stirring are required during the reaction, leading to high energy consumption, and subsequent processing such as cooling and separation after the reaction further increases energy consumption; and the difficulty in precisely controlling the temperature, pressure, and stirring conditions within the reactor can lead to uneven reaction, affecting the molecular weight distribution and performance consistency of the resin.

[0003] To address the aforementioned issues, reactive extrusion technology has been increasingly introduced into the preparation of phenolic resins in recent years. Reactive extrusion is a novel process that combines chemical reaction with extrusion molding, using a twin-screw extruder to achieve continuous feeding, mixing, reaction, and molding of raw materials. Compared to the traditional batch reactor method, reactive extrusion technology offers the following advantages: Reactive screw extruders enable continuous feeding and reaction of raw materials, significantly improving production efficiency and making them suitable for large-scale industrial production; the temperature, pressure, and shear force within the screw extruder can be precisely controlled by adjusting the screw speed, heating temperature, and die design, facilitating the acquisition of products with stable performance; the reactive extrusion process integrates the reaction and molding processes, reducing intermediate steps and lowering energy consumption and production costs; and the reactive extrusion process is a closed system, effectively reducing the emission of volatile organic compounds and minimizing environmental pollution.

[0004] However, existing reactive screw extruders still face some challenges in the preparation of phenolic resins. The polycondensation reaction of phenolic resins is an exothermic reaction, which is prone to local overheating during the reaction, leading to premature curing or performance degradation of the resin. In addition, the devolatilization process requires high pressure in the barrel, necessitating the regulation and monitoring of the pressure within the screw extruder.

[0005] Therefore, developing a reactive extrusion apparatus suitable for the preparation of phenolic resins has significant theoretical and practical value. Utility Model Content

[0006] In view of the problems mentioned above in the background art, the purpose of this utility model is to provide a reactive extrusion device for continuous preparation of phenolic resin.

[0007] To achieve the above-mentioned technical objectives, the technical solution adopted by this utility model is as follows:

[0008] A reactive extrusion apparatus for continuous preparation of phenolic resin includes a horizontal reactor, a melt gear pump connected to the output end of the horizontal reactor, a reactive devolatilization extruder connected to the output end of the melt gear pump, a liquid feeder installed in the horizontal reactor, a powder feeder installed in the reactive devolatilization extruder, and a vacuum device and a template sequentially arranged in the reactive devolatilization extruder.

[0009] Further specified, the nominal diameter of the screw in the horizontal reactor is 100-150 mm, and the length-to-diameter ratio of the screw is 5-20:1.

[0010] Further specified, the horizontal reactor is divided into at least 5 temperature control zones, and an exhaust port connected to the vacuum device is provided above the discharge port of the horizontal reactor.

[0011] Further specified, the nominal diameter of the screw of the reactive devouring extruder is 30-50 mm and the length-to-diameter ratio of the screw is 28-64:1.

[0012] Furthermore, the barrel of the reactive devouring extruder has 1 to 6 vacuum vents and pressure sensors.

[0013] Furthermore, the reactive devolatilization extruder adopts an electric-oil dual-circuit temperature control system, with each barrel corresponding to a temperature control zone.

[0014] Furthermore, each section of the reactive devolatilization extruder is equipped with a thermocouple.

[0015] The beneficial effects of using this utility model are as follows:

[0016] (1) Compared with the traditional batch reactor method, this utility model adopts a continuous production process, realizes the continuous preparation of phenolic resin, and significantly improves production efficiency and output.

[0017] (2) Vacuum exhaust ports are installed on the horizontal reactor and the reaction devolatilization extruder to effectively discharge the gas generated during the reaction, reduce volatile components, and improve the quality of the resin. At the same time, pressure sensors are installed at key positions of the extruder to monitor pressure changes during the reaction in real time, ensuring the safety and stability of the production process.

[0018] (3) The extruder barrel adopts a zoned temperature control system, which can more accurately control the reaction temperature and adapt to the temperature requirements of different reaction stages, thereby optimizing the performance of the resin.

[0019] (4) The use of a melt gear pump to pressurize, meter and transport the melt ensures the stability and accuracy of material flow, which is conducive to the uniformity of product quality. Attached Figure Description

[0020] This utility model can be further illustrated by the non-limiting embodiments given in the accompanying drawings;

[0021] Figure 1 This is a schematic diagram of an embodiment of a reactive extrusion apparatus for continuous preparation of phenolic resin according to the present invention;

[0022] The symbols for the main components are explained below:

[0023] Horizontal reactor 1; melt gear pump 2; reactive devolatilization extruder 3; vacuum device 4. Detailed Implementation

[0024] To enable those skilled in the art to better understand this utility model, the technical solution of this utility model will be further described below in conjunction with the accompanying drawings and embodiments.

[0025] like Figure 1 As shown, the present invention provides a reaction extrusion device for continuous preparation of phenolic resin, comprising a horizontal reactor 1, a melt gear pump 2 connected to the output end of the horizontal reactor 1, a reaction devolatilization extruder 3 connected to the output end of the melt gear pump 2, a liquid feeder installed in the horizontal reactor 1, a powder feeder installed in the reaction devolatilization extruder 3, and a vacuum device 4 and a template sequentially arranged in the reaction devolatilization extruder 3.

[0026] The nominal diameter of the screw in the preferred horizontal reactor 1 is 100-150 mm and the length-to-diameter ratio is 5-20:1. In practice, the nominal diameter of the screw and the length-to-diameter ratio of the screw in the horizontal reactor 1 can also be considered according to the specific circumstances.

[0027] Preferably, the horizontal reactor 1 is divided into at least 5 temperature control zones. An exhaust port connected to the vacuum device 4 is provided above the discharge port of the horizontal reactor 1. In practice, the structure of the horizontal reactor 1 and the structure for connecting to the vacuum device 4 can also be considered according to the specific situation.

[0028] The nominal screw diameter of the reactive devouring extruder 3 is preferably 30-50 mm and the screw length-to-diameter ratio is preferably 28-64:1. In practice, the nominal screw diameter and screw length-to-diameter ratio of the reactive devouring extruder 3 can also be considered according to specific circumstances.

[0029] Preferably, the barrel of the reactive devolatilization extruder 3 has 1 to 6 vacuum exhaust ports and pressure sensors. In practice, the number of vacuum exhaust ports and pressure sensors on the barrel of the reactive devolatilization extruder 3 can also be considered according to the specific situation.

[0030] The preferred reactive devolatilization extruder 3 adopts an electric-oil dual-circuit temperature control system, with each barrel corresponding to a temperature control zone. In practice, temperature control measures for the reactive devolatilization extruder 3 can also be considered according to specific circumstances.

[0031] Ideally, a thermocouple is installed under each section of the barrel of the reactive devolatilization extruder 3. In practice, the installation measures and positions of the thermocouples can also be considered according to specific circumstances.

[0032] In this implementation case, when using a reaction extrusion device for continuous preparation of phenolic resin, the horizontal reactor 1 mainly undertakes the functions of melting, mixing and pre-reaction of materials, the melt gear pump 2 is responsible for the stable conveying of melt materials, and the reaction devouring extruder 3 realizes the functions of deep reaction and devouring of materials.

[0033] It should be noted that: the liquid feeder is used to transport methanol and phenol, and the powder feeder is used to transport processing aids, including but not limited to sodium hydroxide. Thermocouples are used for temperature feedback. The extrusion die of the template is a circular die with rectangular die holes, a hole diameter of 0.5 to 4 mm, and a hole spacing of 3 to 10 mm.

[0034] Specifically, based on the different heating effects of electricity and oil, the dual-loop temperature control system of the horizontal reactor 1 and the reactive devolatilization extruder 3 is activated. Electric heating is activated first, followed by oil heating. The first to third zones of the horizontal reactor 1 are heated to 60–90°C and held for 1 hour to maintain the fluidity of the raw material. Then, the fourth to fifth zones of the horizontal reactor 1 are heated to 90–120°C for preliminary reaction and held for 1 hour. The first to fourth zones of the reactive devolatilization extruder 3 are heated to 90–120°C, the fifth to eighth zones to 120–150°C, and finally the ninth to twelfth zones to 80–110°C. The rotation speed of the horizontal reactor 1 is set to... The rotation speed of the reaction devolatilization extruder 3 is set to 30-80 rpm, with a lower speed contributing to a more complete reaction and better devolatilization effect. The material is fed into the horizontal reactor 1 at a rate of 5-10 kg / h using a liquid feeder. In the horizontal reactor 1, the material completes melting, mixing, and pre-reaction. The material is then fed into the reaction devolatilization extruder 3 using a melt pump. At the same time, the vacuum device 4 at the outlet of the horizontal reactor 1 is turned on to collect the waste gas generated during the pre-reaction. The colloidal material generated after the pre-reaction is transported to the reaction devolatilization extruder 3 through the melt gear pump 2. Under the shearing and conveying action of the screw, the material further completes the deep reaction and devolatilization process, and is finally extruded and formed through a template.

[0035] The above embodiments are merely illustrative of the principles and effects of this utility model and are not intended to limit the scope of this utility model. Any person skilled in the art can modify or alter the above embodiments without departing from the spirit and scope of this utility model. Therefore, all equivalent modifications or alterations made by those skilled in the art without departing from the spirit and technical concept disclosed in this utility model should still be covered by the claims of this utility model.

Claims

1. A reactive extrusion apparatus for continuous preparation of phenolic resin, characterized in that: The system includes a horizontal reactor (1), the output end of which is connected to a melt gear pump (2), the output end of which is connected to a reactive devolatilization extruder (3), the horizontal reactor (1) is equipped with a liquid feeder, the reactive devolatilization extruder (3) is equipped with a powder feeder, and the reactive devolatilization extruder (3) is sequentially equipped with a vacuum device (4) and a template.

2. The reactive extrusion apparatus for continuous preparation of phenolic resin according to claim 1, characterized in that: The nominal diameter of the screw in the horizontal reactor (1) is 100-150 mm and the length-to-diameter ratio of the screw is 5-20:

1.

3. The reactive extrusion apparatus for continuous preparation of phenolic resin according to claim 2, characterized in that: The horizontal reactor (1) is divided into at least 5 temperature control zones, and an exhaust port connected to the vacuum device (4) is provided above the discharge port of the horizontal reactor (1).

4. The reactive extrusion apparatus for continuous preparation of phenolic resin according to claim 3, characterized in that: The nominal diameter of the screw of the reactive devouring extruder (3) is 30-50 mm and the length-to-diameter ratio of the screw is 28-64:

1.

5. The reactive extrusion apparatus for continuous preparation of phenolic resin according to claim 4, characterized in that: The barrel of the reactive devouring extruder (3) has 1 to 6 vacuum exhaust ports and pressure sensors.

6. The reactive extrusion apparatus for continuous preparation of phenolic resin according to claim 5, characterized in that: The reactive devouring extruder (3) adopts an electric-oil dual-circuit temperature control system, with each barrel corresponding to a temperature control zone.

7. The reactive extrusion apparatus for continuous preparation of phenolic resin according to claim 6, characterized in that: A thermocouple is installed under each section of the reactive devouring extruder (3).

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