Tower type reaction system for producing PAO or POE through ethylene polymerization and reaction method of tower type reaction system

Abstract

The invention provides a tower type reaction system for producing PAO or POE through ethylene polymerization and a reaction method thereof. The reaction system comprises a tower type reactor; wherein a baffling assembly and a strengthening unit are sequentially arranged in the tower type reactor, the baffling assembly comprises a plurality of arc-shaped baffle plates and buckles used for fixedly connecting the arc-shaped baffle plates with the tower type reactor, and the arc-shaped baffle plates are distributed in the tower type reactor in a staggered manner; the distance between the arc-shaped baffle plate positioned at the bottom in the plurality of arc-shaped baffle plates and the strengthening unit is 0.8-1.2 times of the tower diameter of the tower reactor; the top of the tower reactor is also provided with a product outlet, the bottom of the tower reactor is provided with a feed port and a circulating feed port, the bottom of the tower reactor is also provided with a circulating discharge port, and the feed port and the circulating feed port are both communicated into the strengthening unit. According to the invention, the polymerization degree and the reaction time of the polymerization reaction are controlled by using the tower reactor and the arc-shaped baffle plate.

Description

Technical Field

[0001] The present invention belongs to the technical field of chemical engineering and technology, and more specifically, it belongs to a tower reaction system for ethylene polymerization to produce PAO or POE and its reaction method. Background Art

[0002] In the field of chemical materials, poly-α-olefins (PAO) and polyolefin elastomers (POE) are increasingly widely used due to their unique properties. As a synthetic lubricant base oil, PAO plays a key role in high-end lubrication fields such as automotive engine oils and industrial lubricants. It has excellent viscosity-temperature properties, low-temperature fluidity, oxidation stability, and thermal stability. POE is a thermoplastic elastomer with excellent performance, combining the easy processability of plastics and the high elasticity of rubbers, and is widely used in industries such as automotive parts, wire and cable, and plastic modification.

[0003] The traditional production processes of PAO and POE mainly use coiled tube reactors. Although they are widely used in industry, one of their biggest disadvantages is that it is impossible to control the residence time of the reaction liquid and the fluid dead zone is relatively large. If the residence time is short, the flow rate of the reaction liquid in the coiled tube is relatively fast, resulting in insufficient ethylene polymerization and failure to reach the desired conversion rate of the target product. If the residence time is too long, the generated product will continue to polymerize in the coiled tube, leading to a decrease in product selectivity. Moreover, coiled tube reactors are more difficult to clean, occupy a large indoor area, and have high equipment costs. The size of the fluid dead zone will affect the residence time of the material in the reaction tower to a certain extent, resulting in local high concentration or overheating, thus triggering side reactions.

[0004] With the continuous growth of the demand for high-performance and low-cost PAO and POE products in various industries, developing new and efficient ethylene polymerization production technologies to overcome the deficiencies of existing technologies has become an urgent problem to be solved.

[0005] In view of this, the present invention is specifically proposed. Summary of the Invention

[0006] The first object of the present invention is to provide a tower reaction system for ethylene polymerization to produce PAO or POE. By combining a strengthening unit and a baffle component, this device increases the mass transfer resistance between gas-liquid two phases while reducing the fluid dead zone in the reaction tower. It better avoids backmixing of the reaction liquid while making the reaction liquid continuously climb, thereby effectively controlling the degree of polymerization and reaction time of the polymerization reaction. In addition, the present invention innovatively uses a tower reactor, which can more effectively control the degree of ethylene polymerization compared to the reaction towers in traditional processes, realizing efficient and precise production of PAO or POE with high conversion rates and high selectivities, and overcoming the problem of large floor area in traditional reactors.

[0007] The second object of the present invention is to provide a method for carrying out reactions in a tower reaction system for ethylene polymerization to produce PAO or POE. This method is simple to operate, has mild operating conditions, and a high product yield.

[0008] In order to achieve the above objects of the present invention, the following technical solutions are specifically adopted: A tower reaction system for ethylene polymerization to produce PAO or POE includes a tower reactor; wherein a baffle assembly and a strengthening unit are sequentially arranged in the tower reactor. The baffle assembly includes a plurality of arc-shaped baffle plates and buckles for fixedly connecting the arc-shaped baffle plates to the tower reactor. The arc-shaped baffle plates are staggeredly distributed in the tower reactor. The distance between the arc-shaped baffle plate at the bottom among the plurality of arc-shaped baffle plates and the strengthening unit is 0.8 - 1.2 times the tower diameter of the tower reactor; a product outlet is further arranged at the top of the tower reactor, a feed inlet and a circulating feed inlet are arranged at the bottom of the tower reactor, a circulating discharge outlet is further arranged at the bottom of the tower reactor, and both the feed inlet and the circulating feed inlet communicate with the strengthening unit.

[0009] In the reaction system of the present invention, by adopting a tower reactor and arranging a strengthening unit inside the tower reactor, the full contact between reaction liquids is ensured, the problem of too wide molecular weight distribution caused by uneven local concentration is reduced, and the degree of polymerization of ethylene can be more effectively controlled compared with the reaction liquids in the traditional process. While improving the conversion rate, the problem of excessive floor area in the traditional reactor is overcome; and the arrangement of the strengthening unit enables the reaction liquids to be violently mixed and then broken into extremely small particle gas-liquid mixtures. With the assistance of the strengthening unit, the reaction liquids are fully mixed and the contact area between the two is increased, thereby increasing the reaction rate and the conversion rate; in order to avoid the backmixing of materials during the condensation reaction in the tower reactor, which may lead to the mixing of materials with different residence times, resulting in too long growth time of some polymer chains and premature termination of some other chains, thus affecting the product yield, and the backmixing of materials prolongs the residence time of some materials, leading to excessive condensation of ethylene to produce by-products, affecting the product purity. Moreover, the backmixing is also likely to cause some catalysts to be wrapped by the reacted polymers, making the active sites on the catalysts unable to contact fresh monomers, thus affecting the reaction efficiency. In addition, the backmixing is also likely to lead to uneven distribution of reaction heat, resulting in the mixing of materials in the high-temperature area and the low-temperature area, causing local overheating and catalyst deactivation. Therefore, in order to avoid the above problems that may occur, in the tower reactor, a plurality of arc-shaped baffle plates are fixedly arranged on the inner wall of the tower reactor through buckles and are staggered in the tower reactor to avoid backmixing between materials. Compared with the traditional straight baffle plates, the arc-shaped baffle plates of the present invention can better avoid backmixing between materials and significantly optimize the fluid flow behavior, reduce the dead zone volume, thereby improving the reaction efficiency, product quality and process stability. The arrangement of the arc-shaped baffle plates can destroy the symmetric flow, thereby enhancing the turbulence. The traditional straight baffle plates may cause the fluid to flow along a fixed path, thus forming a symmetric dead zone. While using the arc-shaped baffle plates can change the fluid direction through its curved structure, break the symmetric fluid pattern, increase the fluid disturbance, reduce the stagnant area, and the staggered distribution of the arc-shaped baffle plates can further disrupt the flow field, avoid the formation of regular eddies, make the fluid distribution in the reactor more uniform, and the staggered distribution of the arc-shaped baffle plates can further enhance the contact frequency between the fluid and the heat exchange wall surface, force the fluid to continuously change the path, reduce the residence time of the material in the high-temperature area, increase the heat transfer coefficient, and reduce the risk of overreaction; at the same time, the curved surface of the arc-shaped baffle plate can guide the fluid to generate secondary flow, accelerate the micro mixing, reduce the local concentration gradient, and ensure a narrower molecular weight distribution of the product; and the fluid scouring effect of the arc-shaped baffle plate can reduce the wall adhesion, reduce the blockage risk, and extend the continuous operation cycle.

[0010] The tower reactor of the present invention can be vertically arranged or longitudinally arranged. Each baffle plate in the longitudinally arranged tower reactor is composed of two semi - circles connected together, with a diameter of one - third of the tower diameter of the tower reactor. The distance between two adjacent baffle plates distributed on the same side is four - thirds to twice the tower diameter of the tower reactor. The longitudinal arrangement of the tower reactor and the arc - shaped baffle plates makes the fluid flow path streamline, further greatly increasing the flow path while avoiding the emergence of dead zones.

[0011] Preferably, as a further feasible solution, the included angle between the arc - shaped baffle plate and the tower reactor is 10° - 20°.

[0012] In the reaction system of the present invention, the included angle between the arc - shaped baffle plate and the side wall of the tower reactor has a significant impact on the size of the fluid dead zone and the reaction efficiency. If the included angle is small, it will cause the fluid to collide weakly with the side wall when gently turning along the arc surface of the baffle plate, and it is easy to form a large dead zone on the back of the baffle plate and the corner of the side wall; if the included angle is large, it will cause strong turbulence after the fluid impacts the side wall, the dead zone is further reduced but the pressure drop increases significantly, which may trigger the "jet" phenomenon of the fluid, resulting in local excessive shear. Therefore, for the present invention, when the included angle between the arc - shaped baffle plate and the side wall of the tower reactor is 10° - 20°, the turning kinetic energy of the fluid increases, generating secondary flow and further destroying the stability of the dead zone, further compressing the volume of the dead zone, improving the mixing efficiency of the material, making the catalyst dispersion more uniform, and the reaction effect is excellent.

[0013] Preferably, as a further feasible solution, the distance between two arc - shaped baffle plates distributed on the same side is 1.5 - 2.5 times the tower diameter of the tower reactor.

[0014] In the present invention, the distance between the stagger - distributed arc - shaped baffle plates is a key parameter affecting the reaction efficiency and the size of the dead zone. If the distance between two arc - shaped baffle plates distributed on the same side is small, it may cause the formation of a turbulent dead zone on the back of the baffle plate, thus affecting the reaction efficiency; if the distance is large, a low - speed stagnation zone is easily formed between the baffle plates, affecting the product structure. Therefore, for the present invention, when the distance between two arc - shaped baffle plates distributed on the same side is 1.5 - 2.5 times the tower diameter of the tower reactor, the reaction effect is excellent.

[0015] Preferably, as a further feasible solution, the entire arc length of the arc - shaped baffle plate is 0.75 - 1 times the tower diameter of the tower reactor.

[0016] Preferably, as a further feasible solution, it further includes a mixer and a pre-reactor connected in sequence, wherein a strengthening unit is provided at the bottom of the pre-reactor; a mixer feed port is provided at the bottom of the pre-reactor, and an ethylene inlet is further provided below the mixer feed port. The mixer feed port and the ethylene inlet lead into the strengthening unit, and the mixer is connected to the pre-reactor through the mixer feed port. Furthermore, a solvent feed port is provided on one side of the mixer, and a catalyst feed port is provided at the top of the mixer.

[0017] Preferably, as a further feasible solution, an air inlet is further provided below the mixer feed port, and the air inlet leads into the strengthening unit. The ethylene gas cylinder is connected to the pre-reactor through the air inlet.

[0018] Preferably, as a further feasible solution, a discharge port is provided at the top of the pre-reactor, the discharge port is connected to the feed port, and a centrifugal pump is further provided between the discharge port and the feed port.

[0019] Preferably, as a further feasible solution, a circulation pump and a heat exchanger are sequentially provided between the circulation discharge port and the circulation feed port.

[0020] Preferably, as a further feasible solution, it further includes a product tank, and the product tank is connected to the tower reactor through the product outlet.

[0021] In the reaction system of the present invention, after the reactants are fully mixed in the mixer and then enter the pre-reactor, they are broken into microbubbles by the strengthening unit and then enter the pre-reactor. The reactants are violently mixed by the strengthening unit and then broken into a gas-liquid mixture of extremely small particles. By using the assistance of the strengthening unit, the reactants are fully mixed with each other and have a large contact area. After the polymerization reaction is initially initiated, the reaction liquid is pumped into the tower reactor by a centrifugal pump and then broken into smaller particles by the strengthening unit for strengthening reaction to generate the final product. Among them, a plurality of arc-shaped baffle plates are provided in the tower reactor to make the reaction liquid continuously climb and avoid backmixing while increasing the flow path of the reactants in the tower, increasing the residence time, and avoiding insufficient polymerization degree caused by incomplete reaction of the reactants. The arc-shaped baffle plates effectively control the polymerization degree, reaction time, and dead zone size of the polymerization reaction, thereby effectively controlling the ethylene polymerization degree, increasing the residence time of the reactants in the reactor, and improving the product purity; then, the reaction liquid is circulated and pumped into the strengthening unit by the circulation pump provided at the bottom of the tower reactor, and the ethylene is further fully reacted by continuous circulation.

[0022] The intensification unit of the present invention belongs to the prior art. Although some are of the pneumatic type, some are of the hydraulic type, and some are of the pneumatic-hydraulic linkage type, the differences between the types are mainly selected according to specific working conditions. In addition, regarding the connection of the intensification reaction tower and the reactor, as well as other equipment, including the connection structure and connection position, it depends on the structure of the intensification reaction tower and is not limited herein.

[0023] The present invention also provides a method for the reaction carried out in a tower reaction system for ethylene polymerization to produce PAO or POE, including the following steps: Introduce a catalyst and a solvent and mix them to obtain a mixed solution. Subsequently, mix the mixed solution with ethylene and then break it into microbubbles for condensation reaction, thus obtaining the product.

[0024] Among them, the reaction temperature for ethylene polymerization to produce PAO is 50°C - 110°C, the reaction pressure is 0.8 Mpa - 5 Mpa, and the residence time is about 4 h - 9 h; The reaction temperature for ethylene polymerization to produce POE is 30°C - 60°C, the reaction pressure is atmospheric pressure, and the reaction time is 1 h - 3 h.

[0025] Moreover, during the reaction process of the present invention, the volume ratio of ethylene to the solvent is 1:2 - 1:3, and the mass ratio of the catalyst to ethylene is 1:50 - 1:100. By adjusting the ratio between the raw materials and combining with a tower reaction system for ethylene polymerization to produce PAO or POE provided by the present invention, the yield of PAO can reach 80% - 90%; the yield of POE is 85% - 95%.

[0026] Compared with the prior art, the beneficial effects of the present invention are as follows: (1) A tower reaction system for ethylene polymerization to produce PAO or POE provided by the present invention. This device combines an intensification unit and a baffle component to increase the mass transfer resistance between the gas-liquid two phases while reducing the dead zone of the fluid in the reaction tower. It can better avoid the backmixing of the reaction liquid while making the reaction liquid continuously rise, thereby effectively controlling the degree of polymerization and reaction time of the polymerization reaction. In addition, the present invention also innovatively uses a tower reactor, which can more effectively control the degree of ethylene polymerization compared with the reaction tower in the traditional process, realizing efficient and precise production of high-conversion and high-selectivity PAO or POE, and overcoming the problem of large floor area in the traditional reactor.

[0027] (2) A method for the reaction carried out in a tower reaction system for ethylene polymerization to produce PAO or POE provided by the present invention. This method is simple to operate, has mild operating conditions, and a high product yield. Description of the Drawings

[0028] Upon reading the following detailed description of the preferred embodiments, various other advantages and benefits will become apparent to those of ordinary skill in the art. The drawings are only for the purpose of illustrating the preferred embodiments and are not considered to be a limitation of the present invention. Moreover, throughout the drawings, the same reference numerals are used to denote the same components.

[0029] Figure 1 It is a structural diagram of a tower reaction system for producing PAO or POE by ethylene polymerization according to the present invention; In the drawings: 1. Solvent feed inlet; 2. Mixer; 3. Catalyst feed inlet; 4. Pre-reactor; 5. Centrifugal pump; 6. Tower reactor; 7. Product tank; 8. Arc baffle; 9. Circulation pump; 10. Strengthening unit; 11. Ethylene gas cylinder; 12. Heat exchanger. Detailed embodiments

[0030] The technical solutions of the present invention will be clearly and completely described below in conjunction with the drawings and specific embodiments. However, those skilled in the art will understand that the following described embodiments are some embodiments of the present invention, rather than all embodiments, and are only used to illustrate the present invention and should not be construed as limiting the scope of the present invention. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative efforts fall within the scope of protection of the present invention. Those not specified in the embodiments are carried out under conventional conditions or conditions recommended by the manufacturer. Those reagents or instruments not specified by the manufacturer can be obtained as conventional products through commercial purchase.

[0031] In the description of the present invention, it should be noted that the orientation or positional relationship indicated by the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. is based on the orientation or positional relationship shown in the drawings, and is only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of the present invention. In addition, the terms "first", "second", "third" are only used for descriptive purposes and cannot be construed as indicating or implying relative importance.

[0032] In the description of the present invention, it should be noted that unless otherwise clearly specified and defined, the terms "installed", "connected", "connected" should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be directly connected or indirectly connected through an intermediate medium, and it can be the communication inside two elements. For those of ordinary skill in the art, the specific meanings of the above terms in the present invention can be understood in specific situations.

[0033] In order to more clearly illustrate the technical solutions in the present invention, the following will be described in the form of specific embodiments.

[0034] Embodiment 1 Refer to the attached drawings of the specification Figure 1 As Figure 1 shown, the present invention is a tower reaction system for ethylene polymerization to produce PAO or POE, including a tower reactor 6; wherein a baffle component and a strengthening unit 10 are sequentially arranged in the tower reactor 6; The baffle component includes a plurality of arc-shaped baffle plates 8 and fasteners for fixedly connecting the arc-shaped baffle plates 8 to the tower reactor 6. The arc-shaped baffle plates 8 are staggeredly distributed in the tower reactor 6. The distance between the arc-shaped baffle plate 8 at the bottom among the plurality of arc-shaped baffle plates 8 and the strengthening unit 10 is 0.8 times the tower diameter of the tower reactor 6; a product outlet is further arranged at the top of the tower reactor 6, a feed inlet and a circulating feed inlet are arranged at the bottom of the tower reactor 6, and a circulating discharge outlet is further arranged at the bottom of the tower reactor 6. Both the feed inlet and the circulating feed inlet lead into the strengthening unit 10; Wherein the included angle between the arc-shaped baffle plate and the side wall of the tower reactor 6 is 10°, and the distance between two arc-shaped baffle plates distributed on the same side is 1.5 times the tower diameter of the tower reactor 6. The entire arc length of the arc-shaped baffle plate is 0.75 times the tower diameter of the tower reactor; Furthermore, the reaction system of the present invention further includes a mixer 2 and a pre-reactor 4 connected in sequence. A strengthening unit 10 is further arranged at the bottom of the pre-reactor 4. A mixer feed inlet is arranged at the bottom of the pre-reactor. The mixer feed inlet leads into the strengthening unit 10. The mixer 2 is connected to the pre-reactor 4 through the mixer feed inlet; Furthermore, an air inlet is further arranged below the mixer feed inlet. The air inlet also leads into the strengthening unit 10. The ethylene gas cylinder 11 is connected to the pre-reactor 4 through this air inlet; A discharge outlet is arranged at the top of the pre-reactor 4. The discharge outlet is connected to the feed inlet arranged at the bottom of the tower reactor 6. A centrifugal pump 5 is further arranged between the discharge outlet and the feed inlet; Wherein a circulating pump 9 and a heat exchanger 12 are sequentially arranged between the circulating discharge outlet and the circulating feed inlet; The reaction system of the present invention further includes a product tank 7. The product tank is connected to the tower reactor through the product outlet.

[0035] Wherein, the specific reaction process of the tower reaction system for ethylene polymerization to produce PAO or POE of the present invention is as follows: The catalyst enters the mixer 2 through the catalyst feed port 3 provided on one side of the mixer 2, and is fully stirred and mixed with the solvent introduced from the solvent feed port 1 provided at the top of the mixer 2 in the mixer 2; After the catalyst and the solvent are evenly mixed in the mixer 2, they enter the interior of the mixer 2 through the mixer feed port provided at the bottom of the mixer 2, and at the same time, ethylene introduced at a flux of 1 t / h through the ethylene inlet provided at the bottom of the pre-reactor 4 is jointly introduced into the intensifying unit 10 provided at the bottom of the pre-reactor 4. The reactants are broken into extremely small micro-particles and then undergo a preliminary reaction in the pre-reactor 4; Subsequently, after the preliminary reaction is completed, the centrifugal pump 5 pumps the reaction liquid in the pre-reactor 4 into the intensifying unit 10 provided at the bottom of the tower reactor 6 through the feed port provided at the bottom of the tower reactor 6. In this intensifying unit 10, the reaction liquid is broken into small particles again to further carry out an intensifying reaction. At the same time, the reaction liquid is circulated and intensively reacted through the circulation outlet and the circulation inlet provided by the circulation pump 9 provided at the bottom of the tower reactor 6. Through continuous intensifying reaction, ethylene is rapidly polymerized. Then, due to the multiple baffle components provided in the tower reactor 6, a plug flow is formed in the reactor, and the reaction liquid continuously climbs along the arc-shaped baffle 8 to avoid backmixing. The baffle components include multiple arc-shaped baffles 8 and buckles for fixedly connecting the arc-shaped baffle 8 to the tower reactor 6; when the indicators such as the conversion rate of the product reach the standard stably, the product is taken out from the product outlet provided at the top of the tower reactor 6 and stored in the product tank 7.

[0036] Example 2 The present invention is a tower reaction system for ethylene polymerization to produce PAO or POE, including a tower reactor 6; wherein a baffle component and an intensifying unit 10 are sequentially arranged in the tower reactor 6; The baffle component includes multiple arc-shaped baffles 8 and buckles for fixedly connecting the arc-shaped baffle 8 to the tower reactor 6. The arc-shaped baffles 8 are staggered in the tower reactor 6. The distance between the arc-shaped baffle 8 at the bottom among the multiple arc-shaped baffles 8 and the intensifying unit 10 is 1.2 times the tower diameter of the tower reactor 6; a product outlet is further provided at the top of the tower reactor 6, a feed port and a circulation feed port are provided at the bottom of the tower reactor 6, and a circulation outlet is further provided at the bottom of the tower reactor 6. The feed port and the circulation feed port both lead into the intensifying unit 10; Wherein the included angle between the arc-shaped baffle and the side wall of the tower reactor 6 is 20°, and the distance between two arc-shaped baffles distributed on the same side is 2.5 times the tower diameter of the tower reactor 6. The entire arc length of the arc-shaped baffle is 1 times the tower diameter of the tower reactor; Furthermore, the reaction system of the present invention further includes a mixer 2 and a pre-reactor 4 connected in sequence. A strengthening unit 10 is provided at the bottom of the pre-reactor 4. A mixer feed port is provided at the bottom of the pre-reactor, and the mixer feed port leads into the strengthening unit 10. The mixer 2 is connected to the pre-reactor 4 through the mixer feed port. Furthermore, an air inlet is provided below the mixer feed port, and the air inlet also leads into the strengthening unit 10. The ethylene gas cylinder 11 is connected to the pre-reactor 4 through this air inlet. A discharge port is provided at the top of the pre-reactor 4, and the discharge port is connected to a feed port provided at the bottom of the tower reactor 6. A centrifugal pump 5 is also provided between the discharge port and the feed port. A circulation pump 9 and a heat exchanger 12 are sequentially provided between the circulation discharge port and the circulation feed port. The reaction system of the present invention further includes a product tank 7, and the product tank is connected to the tower reactor through a product outlet.

[0037] Among them, the specific process of the reaction carried out by a tower reaction system for ethylene polymerization to produce PAO or POE of the present invention is as follows: The catalyst enters the mixer 2 from the catalyst feed port 3 provided on one side of the mixer 2, and is fully stirred and mixed with the solvent introduced from the solvent feed port 1 provided at the top of the mixer 2 in the mixer 2. After the catalyst and the solvent are evenly mixed in the mixer 2, they enter the interior of the mixer 2 through the mixer feed port provided at the bottom of the mixer 2, and at the same time, ethylene introduced at a flux of 1 t / h through the ethylene inlet provided at the bottom of the pre-reactor 4 is jointly introduced into the strengthening unit 10 provided at the bottom of the pre-reactor 4. The reactants are broken into extremely small micro-particles and then undergo a preliminary reaction in the pre-reactor 4. Subsequently, after the preliminary reaction is completed, the centrifugal pump 5 pumps the reaction liquid in the pre-reactor 4 from the feed port provided at the bottom of the tower reactor 6 into the strengthening unit 10 provided at the bottom of the tower reactor 6. In this strengthening unit 10, the reaction liquid is fully broken into small particles again to further carry out a strengthening reaction. At the same time, through the circulation pump 9 provided at the bottom of the tower reactor 6, a circulation strengthening reaction is carried out through the circulation discharge port and the circulation feed port. Through continuous strengthening reactions, ethylene is rapidly polymerized. Then, due to the multiple baffle components provided in the tower reactor 6, a plug flow is formed in the reactor, and the reaction liquid continuously climbs along the arc-shaped baffle 8 to avoid backmixing. The baffle components include a plurality of arc-shaped baffles 8 and buckles for fixedly connecting the arc-shaped baffle 8 to the tower reactor 6. When the indicators such as the conversion rate of the product reach the standard stably, the product is taken out from the product outlet provided at the top of the tower reactor 6 and stored in the product tank 7.

[0038] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit them; although the present invention has been described in detail with reference to the foregoing embodiments, those of ordinary skill in the art should understand that they can still modify the technical solutions described in the foregoing embodiments, or perform equivalent replacements on some or all of the technical features; and these modifications or replacements do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. A tower reaction system for ethylene polymerization to produce PAO or POE, characterized in that, It includes a tower reactor; wherein a baffle component and a strengthening unit are sequentially arranged in the tower reactor, the baffle component includes a plurality of arc-shaped baffle plates and buckles for fixedly connecting the arc-shaped baffle plates to the tower reactor, the arc-shaped baffle plates are staggered and distributed in the tower reactor, and the distance between the arc-shaped baffle plate at the bottom among the plurality of arc-shaped baffle plates and the strengthening unit is 0.8 - 1.2 times the tower diameter of the tower reactor; a product outlet is further arranged at the top of the tower reactor, a feed inlet and a circulating feed inlet are arranged at the bottom of the tower reactor, a circulating discharge outlet is further arranged at the bottom of the tower reactor, and both the feed inlet and the circulating feed inlet lead into the strengthening unit.

2. The tower reaction system for producing PAO or POE by ethylene polymerization according to claim 1, characterized in that, The included angle between the arc-shaped baffle plate and the tower reactor is 10° - 20°.

3. The tower reaction system for ethylene polymerization to produce PAO or POE according to claim 1, characterized in that, The distance between two arc-shaped baffle plates distributed on the same side is 1.5 - 2.5 times the tower diameter of the tower reactor.

4. The tower reaction system for ethylene polymerization to produce PAO or POE according to claim 1, characterized in that, The entire arc length of the arc-shaped baffle plate is 0.75 - 1 times the tower diameter of the tower reactor.

5. The tower reaction system for ethylene polymerization to produce PAO or POE according to claim 1, wherein, It further includes a mixer and a pre-reactor connected in sequence, wherein a strengthening unit is arranged at the bottom of the pre-reactor; a mixer feed inlet is arranged at the bottom of the pre-reactor, and an ethylene inlet is further arranged below the mixer feed inlet, both the mixer feed inlet and the ethylene inlet lead into the strengthening unit, and the mixer is connected to the pre-reactor through the mixer feed inlet.

6. The tower reaction system for ethylene polymerization to produce PAO or POE according to claim 5, wherein, An inlet is further arranged below the mixer feed inlet, the inlet leads into the strengthening unit, and an ethylene gas cylinder is connected to the pre-reactor through the inlet.

7. The tower reaction system for ethylene polymerization to produce PAO or POE according to claim 5, characterized in that, A discharge outlet is arranged at the top of the pre-reactor, the discharge outlet is connected to the feed inlet, and a centrifugal pump is further arranged between the discharge outlet and the feed inlet.

8. The tower reaction system for ethylene polymerization to produce PAO or POE according to claim 1, wherein, A circulation pump and a heat exchanger are sequentially arranged between the circulating discharge outlet and the circulating feed inlet.

9. The tower reaction system for ethylene polymerization to produce PAO or POE according to claim 1, wherein It further includes a product tank, and the product tank is connected to the tower reactor through the product outlet.

10. A reaction method carried out by a tower reaction system for ethylene polymerization to produce PAO or POE according to any one of claims 1-9, characterized in that, It includes the following steps: A catalyst and a solvent are introduced and mixed to obtain a mixed solution, and then the mixed solution and ethylene are mixed and broken into microbubbles for a condensation reaction to obtain the product.

Images