Production line system capable of realizing large-scale degradation of polyethylene
By designing a self-circulating flow reaction production line system, the problem of large-scale polyethylene degradation was solved, achieving efficient and environmentally friendly polyethylene degradation with high product purity and recyclable catalyst.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2025-04-09
- Publication Date
- 2026-03-24
AI Technical Summary
Existing technologies make it difficult to achieve large-scale degradation of polyethylene, and traditional methods are energy-intensive, produce complex products, and have difficulty separating catalysts, making it difficult to achieve efficient and environmentally friendly large-scale production.
A production line system including a feeding vessel, a buffer vessel, a plunger pump, and a fixed-bed reaction device was designed. Through a self-circulating flow reaction, using alkane dehydrogenation catalysts and olefin metathesis catalysts, polyethylene is degraded into polyethylene wax and liquid fuel under mild conditions. The catalysts and degradation products are easily separated.
It achieves efficient degradation of polyethylene, with high product purity, long catalyst life, and recyclable catalyst, making it suitable for large-scale production.
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Figure CN224024992U_ABST
Abstract
Description
TECHNICAL FIELD
[0001] The utility model relates to a production line system that can realize the degradation of polyethylene on a large scale, and belongs to the technical field of organic chemistry. BACKGROUND
[0002] Polyethylene plastic is the most common and widely used synthetic polymer plastic in modern life, and it plays an important role in the fields of agriculture, packaging, construction, automobiles, and even aerospace. However, due to the fact that the molecular chain of polyethylene is composed of extremely stable saturated C-C bonds and C-H bonds, it has relatively inert chemical properties, and therefore it is difficult to degrade without special treatment. As a result, most polyethylene plastic waste is currently buried, discarded, and becomes "white pollution", and a small number is incinerated or physically recycled, while the proportion of chemical recycling is very small.
[0003] In addition, traditional chemical recycling methods usually involve thermal cracking, hydrocracking, or oxidative cracking of polyethylene plastic at high temperatures. These methods require very high energy consumption or the use of environmentally unfriendly chemicals, and the resulting product components are complex and have low utilization value. Therefore, finding a polyethylene degradation technology that is mild in conditions, has good selectivity, produces fewer by-products, has high reaction conversion rate, produces products with high reuse value, is environmentally friendly, and is suitable for large-scale production, has been a technical problem that needs to be solved in the field.
[0004] A research group led by Huang Zheng of the Shanghai Institute of Organic Chemistry of the Chinese Academy of Sciences has disclosed in Chinese Patent No. 201410415203.7 a method for degrading polyethylene into liquid fuel or / and polyethylene wax by multiple cross-metathesis reactions between C2-C10 alkanes and polyethylene in the presence of an alkane dehydrogenation catalyst and an olefin metathesis catalyst. Although this patent technology can achieve the mild and controllable degradation and recycling of different types of polyethylene such as HDPE, LLDPE, and LDPE, and the reaction conditions are mild, it can overcome the disadvantages of traditional polyethylene degradation methods such as high reaction temperature, complex products, and low product application value. However, the research group found in subsequent large-scale experiments that the reaction system has a very high viscosity, and if traditional tank reactors are used, there are problems such as non-uniform reaction, low degradation efficiency, and difficulty in separating the catalyst from the material, making it difficult to achieve large-scale application. UTILITY MODEL CONTENTS
[0005] In view of the above problems existing in the prior art, the purpose of the utility model is to provide a production line system that can realize the degradation of polyethylene on a large scale.
[0006] To achieve the above-mentioned purpose, the technical scheme adopted by the utility model is as follows:
[0007] The production line system can realize large-scale degradation of polyethylene, and comprises a feeding kettle, a buffer kettle, a plunger pump, a fixed bed type reaction device with constant temperature and heating function, and three-way ball valves V1, V2, V3 and V4, wherein: the three-way ball valve V1 and the three-way ball valve V4 are two-inlet one-outlet three-way ball valves, and the three-way ball valve V2 and the three-way ball valve V3 are one-inlet two-outlet three-way ball valves; and one inlet of the three-way ball valve V1 is connected with a discharge port of the feeding kettle through a fluid pipeline, the other inlet of the three-way ball valve V1 is connected with a discharge port of the buffer kettle through a fluid pipeline, an outlet of the three-way ball valve V1 is connected with a feeding inlet of the plunger pump through a fluid pipeline, an inlet of the three-way ball valve V2 is connected with a discharge port of the plunger pump through a fluid pipeline, one outlet of the three-way ball valve V2 is connected with a product receiver through a fluid pipeline, the other outlet of the three-way ball valve V2 is connected with an inlet of the three-way ball valve V3 through a fluid pipeline, one outlet of the three-way ball valve V3 is connected with a feeding inlet of the fixed bed type reaction device through a fluid pipeline, the other outlet of the three-way ball valve V3 is connected with one inlet of the three-way ball valve V4 through a fluid pipeline, the other inlet of the three-way ball valve V4 is connected with a discharge port of the fixed bed type reaction device through a fluid pipeline, and an outlet of the three-way ball valve V4 is connected with a feeding inlet of the buffer kettle through a fluid pipeline.
[0008] In an embodiment, the production line system further comprises a vacuum oil pump, and the kettle covers of the feeding kettle and the buffer kettle are each provided with an exhaust port, and the exhaust ports are each connected with the vacuum oil pump through a silica gel pipe.
[0009] In an embodiment, the production line system further comprises an inert gas cylinder, and the kettle covers of the feeding kettle and the buffer kettle are each provided with an air inlet, and the air inlets are each connected with a pressure reducing valve of the inert gas cylinder through a silica gel pipe.
[0010] In an embodiment, the feeding kettle and the buffer kettle are each provided with an electric heating jacket of aluminum silicate fiber insulation.
[0011] In an embodiment, the feeding kettle and the buffer kettle are each provided with a magnetic coupling mechanical stirrer.
[0012] In an embodiment, the feeding kettle and the buffer kettle are each provided with a digital display controller for monitoring the internal temperature, pressure and mechanical stirring speed of the kettle in real time.
[0013] In an embodiment, the fixed bed type reaction device with constant temperature and heating function is composed of a fixed bed reactor and an oven with constant temperature and heating function, the fixed bed reactor is fixed in the oven through a clamp, and a perforation for connecting the fluid pipeline with the feeding inlet and the discharge port of the fixed bed reactor is formed in the side wall of the oven.
[0014] In an embodiment, the fixed bed reactor is an axial adiabatic fixed bed reactor.
[0015] Preferably, the outlet of the fixed bed reactor is arranged at the top end of the fixed bed reactor, and the inlet of the fixed bed reactor is arranged at the bottom end of the fixed bed reactor.
[0016] Preferably, the fluid pipeline is a stainless steel pipe.
[0017] Preferably, a heating belt is wound on the fluid pipeline.
[0018] Further preferably, the heating belt is a glass fiber electric heating belt.
[0019] Compared with the prior art, the utility model has the beneficial technical effects that:
[0020] The production line system can realize polyethylene self-circulation flow degradation reaction, can obtain polyethylene wax products with high yield, can effectively avoid the difficulty in separating the catalyst and the degradation products, can significantly improve the service life of the catalyst, can ensure the high purity of the degradation products, and can realize efficient recycling of the catalyst. BRIEF DESCRIPTION OF DRAWINGS
[0021] Figure 1 is a structure schematic view of a production line system capable of realizing polyethylene large-scale degradation provided by the embodiment;
[0022] Figure 2 is a structure schematic view of the feeding kettle in the embodiment;
[0023] Figure 3 is a structure schematic view of the buffer kettle in the embodiment;
[0024] Figure 4 is a structure schematic view of the fixed bed type reaction device with constant temperature and heating function in the embodiment;
[0025] Figure 5 is a principle diagram of the production line system provided by the embodiment for realizing feeding and conveying into the buffer kettle;
[0026] Figure 6 is a principle diagram of the production line system provided by the embodiment for realizing circulation flow reaction;
[0027] Figure 7 is a principle diagram of the production line system provided by the embodiment for realizing reaction monitoring sampling or degradation product collection. DETAILED DESCRIPTION
[0028] The technical scheme of the utility model will be described in further detail in connection with the drawings and embodiments. In addition, it should be noted that the terms used in the utility model are merely for the purpose of describing specific embodiments and are not intended to limit the utility model. Unless otherwise defined, the technical terms or scientific terms used in the utility model should be understood as the general meaning understood by those with ordinary skills in the art. The experimental methods in the following embodiments are not specified, and are selected according to conventional methods and conditions or according to the instructions of the commodity.
[0029] Embodiment
[0030] Please see Figure 1 As shown in the drawings, the production line system capable of realizing large-scale degradation of polyethylene provided by the embodiment comprises a feeding kettle 1, a buffer kettle 2, a plunger pump 3, a fixed bed type reaction device 4 with constant temperature and heating functions, and three-way ball valves V1, V2, V3 and V4. The three-way ball valve V1 and the three-way ball valve V4 are both two-inlet one-outlet three-way ball valves, and the three-way ball valve V2 and the three-way ball valve V3 are both one-inlet two-outlet three-way ball valves. The inlet of the three-way ball valve V1 is connected with the outlet of the feeding kettle 1 through a fluid pipeline 6-1, the other inlet of the three-way ball valve V1 is connected with the outlet of the buffer kettle 2 through a fluid pipeline 6-2, the outlet of the three-way ball valve V1 is connected with the inlet of the plunger pump 3 through a fluid pipeline 6-3, the inlet of the three-way ball valve V2 is connected with the outlet of the plunger pump 3 through a fluid pipeline 6-4, one outlet of the three-way ball valve V2 is connected with the product receiver 5 through a fluid pipeline 6-5, the other outlet of the three-way ball valve V2 is connected with the inlet of the three-way ball valve V3 through a fluid pipeline 6-6, one outlet of the three-way ball valve V3 is connected with the inlet of the fixed bed type reaction device 4 through a fluid pipeline 6-7, the other outlet of the three-way ball valve V3 is connected with the other inlet of the three-way ball valve V4 through a fluid pipeline 6-8, the other inlet of the three-way ball valve V4 is connected with the outlet of the fixed bed type reaction device 4 through a fluid pipeline 6-9, and the outlet of the three-way ball valve V4 is connected with the inlet of the buffer kettle 2 through a fluid pipeline 6-10.
[0031] Specifically, please see Figure 2As shown, the feeding kettle 1 described in the embodiment includes a kettle body 1-1 made of stainless steel and a kettle cover 1-2. An electric heating jacket 1-3 made of aluminum silicate fiber is arranged outside the kettle body 1-1. An anchor stirring paddle 1-4 is arranged inside the kettle body 1-1. A discharge port 1-5 is arranged at the bottom of the kettle body 1-1. The discharge port 1-5 is provided with a stainless steel pipe 1-51. The lower end of the stainless steel pipe 1-51 is provided with a ball valve 1-52 for controlling discharge. The stainless steel pipe 1-51 at the lower end of the ball valve 1-52 is connected with a fluid pipe 6-1 connected with a three-way ball valve V1 through a reducing joint. The side of the kettle body 1-1 is provided with a pressure-resistant glass observation window 1-6. The pressure-resistant glass observation window 1-6 is provided with a liquid level scale. A magnetic coupling mechanical stirrer 1-7 is further arranged on the kettle body 1-1. The magnetic coupling mechanical stirrer 1-7 is a commercially available product known in the art, which includes a stirring head 1-71 and a driving motor 1-72. A liquid feeding port 1-21 is arranged on the kettle cover 1-2. The liquid feeding port 1-21 is provided with a stainless steel pipe 1-211. The lower end of the stainless steel pipe 1-211 extends to a depth of about 50 mm inside the kettle body 1-1. The upper end of the stainless steel pipe 1-211 is provided with a two-way ball valve 1-212. A solid feeding port 1-22 is further arranged on the kettle cover 1-2. The upper end of the solid feeding port 1-22 is sealed by a stud 1-221 and a rubber gasket 1-222. The position of the solid feeding port 1-22 is not specially limited, as long as it does not interfere with other designs on the kettle cover 1-2. An air inlet 1-23 is further arranged on the kettle cover 1-2. The air inlet 1-23 is provided with a stainless steel pipe 1-231. The lower end of the stainless steel pipe 1-231 extends to a depth of about 50 mm inside the kettle body 1-1. The upper end of the stainless steel pipe 1-231 is provided with a two-way needle valve 1-232. An exhaust port 1-24 is further arranged on the kettle cover 1-2. The exhaust port 1-24 is provided with a stainless steel pipe 1-241. The lower end of the stainless steel pipe 1-241 is parallel to the top end of the kettle body 1-1. The upper end of the stainless steel pipe 1-241 is provided with a two-way needle valve 1-242. A temperature probe insertion pipe 1-25 is further arranged on the kettle cover 1-2. The lower end of the temperature probe insertion pipe 1-25 extends to the middle section inside the kettle body 1-1. A pressure gauge 1-26 is further arranged on the kettle cover 1-2. In addition, the feeding kettle 1 is further provided with a digital display controller (not shown in the figure, the position of the digital display controller can be designed according to the prior art) for real-time monitoring of the temperature, pressure and mechanical stirring speed inside the kettle body 1-1. The kettle body 1-1 can withstand a pressure of 0.5 MPa and can work at a temperature of up to 200℃.
[0032] See Figure 3As shown, the buffer kettle 2 also includes a kettle body 2-1 and a kettle cover 2-2 made of stainless steel, an electric heating jacket 2-3 made of aluminum silicate fiber is arranged outside the kettle body 2-1, and an anchor stirring paddle 2-4 is arranged inside the kettle body 2-1; a magnetic coupling mechanical stirrer 2-5 is further arranged on the kettle body 2-1, the magnetic coupling mechanical stirrer 2-5 is a commercially available product, which includes a stirring head 2-51 and a driving motor 2-52; a feeding port 2-21 is arranged on the kettle cover 2-2, the feeding port 2-21 is provided with a stainless steel pipe 2-211, the lower end of the stainless steel pipe 2-211 extends to about 50 mm deep inside the kettle body 2-1, and the upper end of the stainless steel pipe 2-211 is provided with a two-way ball valve 2-212, the upper end of the two-way ball valve 2-212 is connected with a fluid pipeline 6-10 connected with a three-way ball valve V4; a discharging port 2-22 is further arranged on the kettle cover 2-2, the discharging port 2-22 is provided with a stainless steel pipe 2-221, the lower end of the stainless steel pipe 2-221 extends to the bottom of the kettle body 2-1, and the upper end of the stainless steel pipe 2-221 is provided with a two-way ball valve 2-222, the upper end of the two-way ball valve 2-222 is connected with a fluid pipeline 6-2 connected with a three-way ball valve V1; an air inlet 2-23 is further arranged on the kettle cover 2-2, the air inlet 2-23 is provided with a stainless steel pipe 2-231, the lower end of the stainless steel pipe 2-231 extends to about 50 mm deep inside the kettle body 2-1, and the upper end of the stainless steel pipe 2-231 is provided with a two-way needle valve 2-232; an air outlet 2-24 is further arranged on the kettle cover 2-2, the air outlet 2-24 is provided with a stainless steel pipe 2-241, the lower end of the stainless steel pipe 2-241 is parallel to the top end of the kettle body 2-1, and the upper end of the stainless steel pipe 2-241 is provided with a two-way needle valve 2-242; a temperature probe insertion pipe 2-25 is further arranged on the kettle cover 2-2, which extends to the middle section inside the kettle body 2-1; a pressure gauge 2-26 is further arranged on the kettle cover 2-2; in addition, the buffer kettle 2 is further provided with a digital display controller (not shown in the figure, the position of the digital display controller can be designed according to the prior art) for real-time monitoring of the temperature, pressure and mechanical stirring speed inside the kettle body 2-1, the kettle body 2-1 can withstand a pressure of 4 Mpa and the working temperature can reach 200℃.
[0033] As a preferred solution, please see Figure 1As shown, the production line system described in the embodiment further comprises a vacuum oil pump 7 and an inert gas cylinder 8, the gas inlet 1-23 of the feeding kettle 1 is connected to the pressure reducing valve of the inert gas cylinder 8 via a two-way needle valve 1-232 and a silica gel tube 9-1, and the gas outlet 1-24 of the feeding kettle 1 is connected to the vacuum oil pump 7 via a two-way needle valve 1-242 and a silica gel tube 9-2; the gas inlet 2-23 of the buffer kettle 2 is connected to the pressure reducing valve of the inert gas cylinder 8 via a two-way needle valve 2-232 and a silica gel tube 9-3, and the gas outlet 2-24 of the buffer kettle 2 is connected to the vacuum oil pump 7 via a two-way needle valve 2-242 and a silica gel tube 9-4, which is conducive to achieving inert atmosphere operation in the feeding kettle 1 and the buffer kettle 2.
[0034] In addition, please refer to Figure 4 As shown, the fixed bed reaction device 4 with constant temperature and heating function described in the embodiment is composed of a fixed bed reactor 4-1 and an oven 4-2 with constant temperature and heating function, the fixed bed reactor 4-1 is fixed in the oven 4-2 by a clamp 4-3 (in the figure, it is composed of a fixed rod 4-31 and a plurality of fixed clamps 4-32, the fixed rod 4-31 is fixedly connected to the inner rear wall of the oven 4-2, a plurality of fixed clamps 4-31 are fixedly arranged on the fixed rod 4-31 at intervals, and the fixed clamps 4-32 can clamp the pipe body of the fixed bed reactor 4-1), and the side wall of the oven 4-2 is provided with a through hole 4-21 for connecting the fluid pipeline 6-7 connected to the feed inlet 4-11 of the fixed bed reactor and the fluid pipeline 6-9 connected to the discharge outlet 4-12 of the fixed bed reactor. The fixed bed reactor 4-1 selects an existing axial adiabatic fixed bed reactor, the discharge outlet 4-12 of the fixed bed reactor is arranged at the top end of the fixed bed reactor 4-1, and the feed inlet 4-11 of the fixed bed reactor is arranged at the bottom end of the fixed bed reactor 4-1. The oven 4-2 is transformed from an existing oven, and the transformation is only to add the clamp 4-3 to the rear inner wall 4-22 of the oven and add the through hole 4-21 to the side wall 4-23 of the oven.
[0035] In addition, the fluid pipelines 6-1 to 6-10 described in the embodiment are stainless steel pipes, heating tapes are wound on the fluid pipelines 6-1 to 6-10 (the part of the fluid pipelines 6-7 and 6-9 located in the oven 4-2 does not need to be wound), the heating tapes are selected from commercially available glass fiber electric heating tapes, the heating tapes are provided with a controller and a temperature measuring probe, and the maximum use temperature can reach 200°C. The plunger pump 3 described in the embodiment preferably has a flow rate range of 0.1 mL / min to 100 mL / min, can withstand a temperature of 140°C, and can withstand a pressure of 20 MPa.
[0036] The production line system described in the embodiment can be used to degrade polyethylene into polyethylene wax main product and liquid fuel byproduct in the presence of alkane dehydrogenation catalyst and olefin metathesis catalyst, using alkane as solvent and common reaction substrate.
[0037] The operation of degrading polyethylene by using the production line system described in the embodiment comprises the following sequential steps:
[0038] a) Put the proportioned polyethylene and alkane as solvent and common reaction substrate into the feeding kettle 1, then replace the inside of the feeding kettle 1 with inert atmosphere and heat it to the preset temperature and start stirring at the preset stirring speed; and replace the inside of the buffer kettle 2 with inert atmosphere and heat it to the preset temperature and start stirring at the preset stirring speed; and pre-mix the proportioned alkane dehydrogenation catalyst and olefin metathesis catalyst uniformly to obtain the dual-component alkane metathesis heterogeneous catalyst, and then fill it into the fixed bed reactor 4-1 in the fixed bed type reaction device 4 with constant temperature and heating function;
[0039] b) Switch the inlet of the three-way ball valve V1 to communicate with the outlet of the feeding kettle 1, switch the outlet of the three-way ball valve V2 to communicate with the inlet of the three-way ball valve V3, switch the outlet of the three-way ball valve V3 to communicate with the inlet of the fixed bed type reaction device 4, switch the inlet of the three-way ball valve V4 to communicate with the outlet of the fixed bed type reaction device 4, and set the flow rate of the plunger pump 3 to 10-30 mL / min to input 100-300 mL of material into the fixed bed reactor 4-1 in the fixed bed type reaction device 4, and then preheat the fixed bed type reaction device 4, the plunger pump 3 and the fluid pipeline to the respective set temperature;
[0040] c) Keep the inlet of the three-way ball valve V1 to communicate with the outlet of the feeding kettle 1, keep the outlet of the three-way ball valve V2 to communicate with the inlet of the three-way ball valve V3, and switch the outlet of the three-way ball valve V3 to communicate with the inlet of the three-way ball valve V4, and set the flow rate of the plunger pump 3 to 90-110 mL / min to deliver the remaining material in the feeding kettle 1 into the buffer kettle 2; the principle diagram of delivering the material in the feeding kettle 1 into the buffer kettle 2 is shown in Figure 5 The arrow in the diagram represents the fluid flow direction;
[0041] d) Switch the inlet of the three-way ball valve V1 to communicate with the outlet of the buffer tank 2, keep the outlet of the three-way ball valve V2 to communicate with the inlet of the three-way ball valve V3, switch the outlet of the three-way ball valve V3 to communicate with the inlet of the fixed bed reactor 4, switch the inlet of the three-way ball valve V4 to communicate with the outlet of the fixed bed reactor 4, and set the flow rate of the piston pump 3 to 10-30 mL / min, so that the material realizes circulation flow reaction between the buffer tank 2 and the fixed bed reactor 4; Figure 6 The arrow in the figure indicates the fluid flow direction;
[0042] e) After the circulation flow reaction starts, sample and monitor the number average molecular weight (Mn) of the degradation product at intervals, and the interval time can be set according to the production needs;
[0043] f) When the number average molecular weight (Mn) of the degradation product reaches the predetermined target (which is determined by the number average molecular weight of the polyethylene wax required by the production), keep the inlet of the three-way ball valve V1 to communicate with the outlet of the buffer tank 2, switch the outlet of the three-way ball valve V2 to communicate with the product receiver 5, and set the flow rate of the piston pump 3 to 90-110 mL / min, to stop the circulation flow reaction, so that the degradation product in the buffer tank 2 is completely output to the product receiver 5, and the fluid flow diagram is as shown in Figure 7 ;
[0044] g) The degradation product collected in step f) is first diluted and dispersed with n-pentane, then filtered through a sand core funnel, and the filter cake is washed with n-pentane several times and then vacuum dried at 70-80°C to constant weight, to obtain the main product of polyethylene wax, and the filtrate obtained at room temperature after removing the n-pentane solvent by rotary evaporation is the liquid fuel byproduct.
[0045] In addition, the sampling operation in step e) is as follows:
[0046] Please refer to Figure 7 , switch the outlet of the three-way ball valve V2 to communicate with the product receiver 5, and keep the flow rate of the piston pump 3 at 10-30 mL / min, and keep the three-way ball valves V1, V3 and V4 in the current state; the amount of each collected sample is 4-6 mL, and after each sampling is completed, switch the outlet of the three-way ball valve V2 to communicate with the inlet of the fixed bed reactor 4, so that the material continues to realize circulation flow reaction between the buffer tank 2 and the fixed bed reactor 4.
[0047] The monitoring method of the number average molecular weight (Mn) of the degradation product is as follows: the collected sample is first diluted and dispersed with n-pentane, then filtered through a sand core funnel, and the collected solid is dried to constant weight at 70-80 DEG C under vacuum, and then the number average molecular weight is measured by GPC.
[0048] It should be noted that the alkane, alkane dehydrogenation catalyst, olefin metathesis catalyst and reaction temperature in this embodiment can be disclosed in the Chinese patent with the patent number 201410415203.7. In addition, the polyethylene includes at least one of linear low density polyethylene (LLDPE), low density polyethylene (LDPE), high density polyethylene (HDPE), and low molecular weight polyethylene, and the polyethylene can be derived from waste polyethylene products in the form of polyethylene plastic boxes, polyethylene cling film, polyethylene shopping bags, etc.
[0049] Finally, it is necessary to point out here that: the above only for the preferred specific embodiments of the present application, but the scope of protection of the present application is not limited to this, any skilled in the art of the technical personnel in the technical range disclosed by the present application, can easily think of changes or replacement, should be covered in the scope of protection of the present application.
Claims
1. A production line system capable of achieving scaleable degradation of polyethylene, characterized by: The production line system comprises a feeding kettle, a buffer kettle, a plunger pump, a fixed bed type reaction device with constant temperature and heating function, and three-way ball valves V1, V2, V3 and V4.
2. The production line system capable of achieving scale degradation of polyethylene according to claim 1, characterized in that: The production line system further comprises a vacuum oil pump, and the kettle covers of the feeding kettle and the buffer kettle are each provided with an exhaust port connected to the vacuum oil pump through a silica gel pipe.
3. The production line system capable of achieving scale degradation of polyethylene according to claim 1, wherein: The production line system further comprises an inert gas cylinder, and the kettle covers of the feeding kettle and the buffer kettle are each provided with an air inlet connected to a pressure reducing valve of the inert gas cylinder through a silica gel pipe.
4. The production line system capable of achieving scale degradation of polyethylene according to claim 1, wherein: The feeding kettle and the buffer kettle are each provided with an electric heating jacket made of aluminum silicate fiber.
5. The production line system that enables scaling down of polyethylene degradation according to claim 1, characterized by: The feeding kettle and the buffer kettle are each provided with a magnetic coupling mechanical stirrer.
6. The production line system that enables scaling down of polyethylene degradation according to claim 1, characterized by: The feeding kettle and the buffer kettle are each provided with a digital display controller for real-time monitoring of the internal temperature, pressure and mechanical stirring speed of the kettle.
7. The production line system that enables scaling down of polyethylene degradation according to claim 1, characterized by: The fixed bed type reaction device with constant temperature and heating function is composed of a fixed bed reactor and an oven with constant temperature and heating function.
8. The production line system capable of achieving scale degradation of polyethylene according to claim 7, characterized in that: The fixed bed reactor is fixed in the oven by a clamp, and a through hole for connecting the fluid pipeline to the inlet and outlet of the fixed bed reactor is formed in the side wall of the oven.
9. The production line system that enables scaling down of polyethylene degradation according to claim 1, characterized by: The fixed bed reactor is an axial adiabatic fixed bed reactor, and the outlet of the fixed bed reactor is arranged at the top end of the fixed bed reactor, and the inlet of the fixed bed reactor is arranged at the bottom end of the fixed bed reactor.
10. The production line system enabling scaleable degradation of polyethylene according to claim 9, characterized in that: The fluid pipeline is a stainless steel pipe. A heating belt is wound around the fluid pipeline.
Citation Information
Patent Citations
Polyethylene degradation method, product and application thereof
CN105348557A