Tower type reaction system for producing PAO or POE through ethylene polymerization
By combining a tower reactor with an arc-shaped baffle, the problems of insufficient ethylene polymerization and large footprint in traditional coil reactors are solved, achieving efficient and precise ethylene polymerization production and improving the conversion rate and selectivity of PAO and POE.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- NANJING YANCHANG REACTION TECH RES INST CO LTD
- Filing Date
- 2025-04-16
- Publication Date
- 2026-04-10
AI Technical Summary
Traditional coil reactors cannot effectively control the residence time and dead zone of the reaction liquid in ethylene polymerization, resulting in incomplete ethylene polymerization, reduced selectivity, large footprint, and difficult cleaning.
A tower reactor combined with an intensifier unit and arc-shaped baffles is used. The staggered arc-shaped baffles reduce the fluid dead zone, increase the gas-liquid two-phase mass transfer resistance, avoid backmixing, control the degree of polymerization and reaction time, and improve the conversion rate.
It enables efficient and precise ethylene polymerization production, improves the conversion rate and selectivity of PAO and POE, reduces floor space, and lowers equipment costs.
Smart Images
Figure CN224100687U_ABST
Abstract
Description
TECHNICAL FIELD
[0001] The utility model belongs to the chemical engineering and process technical field, more particularly belongs to a kind of tower type reaction system of PAO or POE of ethylene polymerization. BACKGROUND
[0002] In the field of chemical materials, poly-alpha-olefin (PAO) and polyolefin elastomer (POE) are increasingly widely used due to their unique performance. PAO, as a synthetic lubricating oil base oil, plays a key role in high-end lubrication fields such as automobile engine oil and industrial lubricating oil. It has excellent viscosity-temperature performance, low-temperature fluidity, oxidation stability and thermal stability. POE is a thermoplastic elastomer with excellent performance, combining the easy processability of plastic and the high elasticity of rubber, and is widely used in the automotive parts, wire and cable, plastic modification and other industries.
[0003] The traditional production process of PAO and POE mainly uses coil type reactors. Although it is widely used in industry, its biggest disadvantage is that it cannot control the residence time of the reaction liquid and has a large fluid dead zone. Short residence time results in fast flow rate of the reaction liquid in the coil, which leads to insufficient ethylene polymerization and does not achieve the desired target product conversion rate. Long residence time leads to continuous polymerization of the generated product in the coil, resulting in decreased product selectivity. Moreover, coil type reactors are more difficult to clean, occupy a large indoor area, and have high instrument costs. The size of the fluid dead zone will affect the residence time of the material in the reaction tower to some extent, leading to excessive local concentration or overheating and causing side reactions.
[0004] With the continuous growth of demand for high-performance, low-cost PAO and POE products in various industries, developing new and efficient ethylene polymerization production technology to overcome the shortcomings of existing technology has become a pressing problem.
[0005] Therefore, the utility model is proposed. SUMMARY
[0006] The first purpose of the utility model is to provide a tower type reaction system for ethylene polymerization production of PAO or POE. The device increases the mass transfer resistance between gas and liquid two phases while reducing the dead zone of the fluid in the reaction tower by combining the intensifier set and the baffling assembly, better avoids backmixing of the reaction liquid while making the reaction liquid continuously climb, thereby effectively controlling the polymerization degree and reaction time of the polymerization reaction. In addition, the utility model also innovatively uses a tower type reactor, which can more effectively control the ethylene polymerization degree compared to the reaction tower in the traditional process, achieve efficient and precise production of PAO or POE with high conversion rate and high selectivity, and overcome the problem of large floor area in traditional reactors.
[0007] In order to realize the above-mentioned purpose of the utility model, the following technical scheme is adopted:
[0008] A tower type reaction system for ethylene polymerization production PAO or POE, comprising a tower type reactor; wherein the tower type reactor is sequentially provided with a baffle assembly and a strengthening unit, the baffle assembly comprises a plurality of arc baffle plates and buckles for realizing the fixed connection of the arc baffle plates and the tower type reactor, the arc baffle plates are staggered distributed in the tower type reactor, the distance between the arc baffle plate at the bottom of the plurality of arc baffle plates and the strengthening unit is 0.8-1.2 times of the tower diameter of the tower type reactor; the top of the tower type reactor is further provided with a product outlet, the bottom of the tower type reactor is provided with a feed inlet and a circulating feed inlet, the bottom of the tower type reactor is further provided with a circulating discharge outlet, and the feed inlet and the circulating feed inlet are both communicated into the strengthening unit.
[0009] In the reaction system of the utility model, through the adoption of tower reactor and the mode of setting up the intensifier unit in the tower reactor, the full contact between the reaction liquids is ensured, the problem of too wide molecular weight distribution caused by local concentration unevenness is reduced, the polymerization degree of ethylene can be more effectively controlled compared with the reaction liquid in the traditional process, the problem of too large floor area in the traditional reactor is overcome while the conversion rate is improved; the setting of the intensifier unit makes the reaction liquid be mixed violently and then be broken into extremely small particle gas-liquid mixture, the reaction liquid is fully mixed and the contact area between the two is increased through the assistance of the intensifier unit, and then the reaction rate is increased and the conversion rate is improved; in order to avoid the back mixing of materials when the tower reactor carries out condensation reaction, the mixing of materials with different residence time is caused, part of the polymer chain grows too long, and other chains terminate too early, thereby affecting the product yield and the back mixing of materials prolongs the residence time of part of the materials, thereby causing the over condensation of ethylene to produce by-products, affecting the product purity, and the back mixing also easily makes part of the catalyst be wrapped by the reacted polymer, so that the active sites on the catalyst cannot contact fresh units, thereby affecting the reaction efficiency, in addition, the back mixing also easily causes uneven distribution of reaction heat, thereby causing the mixing of materials in the high temperature area and the low temperature area to cause local overheating to cause the deactivation of the catalyst, therefore, in order to avoid the above problems, a plurality of arc baffle plates are fixedly arranged in the tower reactor through buckles and the inner wall of the tower reactor, and are staggered distributed in the tower reactor, thereby avoiding the back mixing between the materials, compared with the traditional straight line baffle plate, the arc baffle plate of the utility model can better avoid the back mixing between the materials, and can also significantly optimize the fluid flow behavior, reduce the dead volume, thereby improving the reaction efficiency, product quality and process stability, the setting of the arc baffle plate can destroy the symmetrical flow, thereby enhancing the turbulent flow, the traditional straight line baffle plate can cause the fluid to flow along the fixed path, thereby forming a symmetrical dead zone, and the adoption of the arc baffle plate can change the fluid direction through the curved structure, break the symmetrical fluid mode, increase the fluid disturbance, reduce the retention area, and the staggered distribution of the arc baffle plate can further disrupt the flow field, avoid the formation of regular vortex, make the fluid be more uniformly distributed in the reactor, and the staggered distribution of the arc baffle plate can further enhance the contact frequency of the fluid and the heat exchange wall surface, force the fluid to change the path constantly, reduce the residence time of the materials in the high temperature area, improve the heat transfer coefficient, and reduce the risk of overreaction; at the same time, the curved surface of the arc baffle plate can guide the fluid to produce secondary flow, accelerate the micro mixing, reduce the local concentration gradient, and ensure that the product molecular weight distribution is narrower; and the fluid scouring effect of the arc baffle plate can reduce the wall adhesion, reduce the risk of blockage, and prolong the continuous operation cycle.
[0010] The tower reactor of the utility model can be vertically arranged or longitudinally arranged, each baffle plate in the longitudinally arranged tower reactor is composed of two semicircles connected together, the diameter of the baffle plate is one third of the tower diameter of the tower reactor, and the distance between two adjacent baffle plates arranged on the same side is four thirds of the tower diameter of the tower reactor to two times of the tower diameter, the longitudinally arranged tower reactor and the arc baffle plate are arranged so that the fluid flow path is streamlined, and the flow path is greatly increased while avoiding the emergence of dead zones.
[0011] Preferably, as a further implementable scheme, the included angle between the arc baffle plate and the tower reactor is 10-20 degrees.
[0012] In the reaction system of the utility model, the included angle between the arc baffle plate and the side wall of the tower reactor has a significant influence on the fluid dead zone size and the reaction efficiency, wherein if the included angle is small, the collision of the fluid with the side wall when the fluid is gently turned along the arc surface of the baffle plate is weak, and a large dead zone is easily formed at the back of the baffle plate and the corner of the side wall; if the included angle is large, the fluid forms strong turbulence after colliding with the side wall, the dead zone is further reduced but the pressure drop is significantly increased, which may cause the fluid to be "ejected" and thus cause local excessive shearing, therefore, for the utility model, when the included angle between the arc baffle plate and the side wall of the tower reactor is 10-20 degrees, the fluid turning kinetic energy is increased, secondary flow is generated to further destroy the stability of the dead zone, the dead zone volume is further compressed, the mixing efficiency of the material is improved, the catalyst is more uniformly dispersed, and the reaction effect is excellent.
[0013] Preferably, as a further implementable scheme, the distance between two arc baffle plates arranged on the same side is 1.5-2.5 times of the tower diameter of the tower reactor.
[0014] In the utility model, the distance between the staggered arc baffle plates is a key parameter affecting the reaction efficiency and the dead zone size, wherein if the distance between two arc baffle plates arranged on the same side is small, the fluid may form a turbulent dead zone at the back of the baffle plate, thereby affecting the reaction efficiency; if the distance is large, a low-speed stagnant zone is easily formed between the baffle plates, thereby affecting the product structure, therefore, for the utility model, when the distance between two arc baffle plates arranged on the same side is 1.5-2.5 times of the tower diameter of the tower reactor, the reaction effect is excellent.
[0015] Preferably, as a further implementable scheme, the entire arc length of the arc baffle plate is 0.75-1 times of the tower diameter of the tower reactor.
[0016] Preferably, as a further implementable scheme, a mixer and a pre-reactor are sequentially connected, wherein the bottom of the pre-reactor is provided with a reinforced unit; the bottom of the pre-reactor is provided with a mixer feed port, and an ethylene gas inlet is further arranged below the mixer feed port, the mixer feed port and the ethylene gas inlet are connected to the reinforced unit, and the mixer is connected to the pre-reactor through the mixer feed port.
[0017] Further, one side of the mixer is provided with a solvent feed port, and the top of the mixer is provided with a catalyst feed port.
[0018] Preferably, as a further implementable scheme, an inlet is further arranged below the mixer feed port, the inlet is connected to the pre-reactor through the reinforced unit, and an ethylene gas cylinder is connected to the pre-reactor through the inlet.
[0019] Preferably, as a further implementable scheme, the top of the pre-reactor is provided with a discharge port connected to the feed port, and a centrifugal pump is further arranged between the discharge port and the feed port.
[0020] Preferably, as a further implementable scheme, a circulating pump and a heat exchanger are sequentially arranged between the circulating discharge port and the circulating feed port.
[0021] Preferably, as a further implementable scheme, a product tank is further connected to the column reactor through the product outlet.
[0022] In the reaction system of the utility model, after the reactants are fully mixed by the mixer and then enter the pre-reactor, the reactants are broken into micro-bubbles by the reinforced unit and then enter the pre-reactor, the reactants are mixed violently by the reinforced unit and then broken into extremely small particle gas-liquid mixture, the auxiliary of the reinforced unit is adopted to make the reactants fully mixed and have a large contact area, the preliminary polymerization reaction is initiated, the reaction liquid is pumped into the column reactor by the centrifugal pump, the reinforced unit is broken into smaller particles for reinforced reaction to produce the final product, a plurality of arc baffles are arranged in the column reactor to make the reaction liquid continuously climb and avoid back mixing, increase the flow path of the reactants in the column, increase the residence time, avoid incomplete reaction of the reactants to cause insufficient polymerization degree, effectively control the polymerization degree, reaction time and dead zone size of the polymerization reaction through the arc baffles, thereby effectively control the ethylene polymerization degree, increase the residence time of the reactants in the reactor, and improve the product purity; then the reaction liquid is pumped into the reinforced unit by the circulating pump arranged at the bottom of the column reactor, and the ethylene is fully reacted by continuous circulation.
[0023] The intensifier unit of the utility model belongs to prior art, although some are pneumatic type, some are hydraulic type, and some are gas-liquid linkage type, but the difference between the types is mainly selected according to the different specific working conditions, in addition, the connection of the intensification reaction tower and the reactor and other equipment, including the connecting structure and the connecting position, is determined according to the structure of the intensification reaction tower, which is not limited.
[0024] The tower type reaction system for the ethylene polymerization production PAO or POE provided by the utility model can make the PAO yield reach 80-90%, and the POE yield is 85-95%.
[0025] Compared with the prior art, the utility model has the beneficial effects that:
[0026] (1) the tower type reaction system for the ethylene polymerization production PAO or POE provided by the utility model, the device is combined with the intensifier unit and the baffle assembly to increase the mass transfer resistance between the gas-liquid two phases and reduce the dead zone of the fluid in the reaction tower, better avoid the back mixing of the reaction liquid, and make the reaction liquid continuously climb, so that the polymerization degree and the reaction time of the polymerization reaction can be effectively controlled, in addition, the utility model also innovatively uses the tower type reactor, compared with the reaction tower in the traditional process, the ethylene polymerization degree can be more effectively controlled, the high conversion rate memory high selectivity PAO or POE is realized, and the problem of large floor area in the traditional reactor is overcome. BRIEF DESCRIPTION OF DRAWINGS
[0027] Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments with reference made to the accompanying drawings. The drawings are for purposes of illustration only and are not intended to be limiting in any respect. Furthermore, the use of the same reference symbols in different drawings indicates similar or identical items.
[0028] Figure 1 It is a structure diagram of the tower type reaction system for the ethylene polymerization production PAO or POE of the utility model;
[0029] In the drawings:
[0030] 1. solvent feed inlet; 2. mixer; 3. catalyst feed inlet; 4. pre-reactor; 5. centrifugal pump; 6. tower type reactor; 7. product tank; 8. arc baffle; 9. circulating pump; 10. intensifier unit; 11. ethylene gas cylinder; 12. heat exchanger. DETAILED DESCRIPTION
[0031] The technical solutions of the present application will be described clearly and completely in the following with reference to the drawings and specific embodiments, but those skilled in the art will understand that the following described embodiments are part of the embodiments of the present application, rather than all the embodiments, and are only used to illustrate the present application, and should not be regarded as limiting the scope of the present application. Based on the embodiments in the present application, all other embodiments obtained by those skilled in the art without creative labor are within the scope of protection of the present application. The specific conditions not mentioned in the embodiments are carried out according to the conventional conditions or the conditions recommended by the manufacturer. The reagents or instruments not mentioned by the manufacturer are all conventional products that can be purchased in the market.
[0032] In the description of the present application, it should be pointed out that the orientations or positional relationships indicated by the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer" and the like are based on the orientations or positional relationships shown in the drawings, and are only for the convenience of describing the present application and simplifying the description, and therefore cannot be understood as limiting the devices or elements indicated to have a specific orientation, to be constructed and operated in a specific orientation, and therefore cannot be understood as limiting the present application. In addition, the terms "first", "second", "third" are only for the purpose of description, and cannot be understood as indicating or implying relative importance.
[0033] In the description of the present application, it should be pointed out that unless otherwise explicitly specified and limited, the terms "mounting", "connection", "connection" should be understood broadly, for example, it can be fixedly connected, or it can be detachably connected, or integrally connected; it can be mechanically connected, or it can be electrically connected; it can be directly connected, or it can be indirectly connected through an intermediate medium; it can be the communication inside two elements. For those skilled in the art, the specific meaning of the above terms in the present application can be understood according to the specific circumstances.
[0034] In order to more clearly describe the technical solutions in the present application, the following will be described in the form of specific embodiments.
[0035] Embodiment 1
[0036] Referring to the drawings Figure 1
[0037] As Figure 1 shown, the present application is a tower type reaction system for producing PAO or POE by ethylene polymerization, comprising a tower type reactor 6; wherein the tower type reactor 6 is sequentially provided with a baffle assembly and a strengthening unit 10;
[0038] The baffle assembly comprises a plurality of arc-shaped baffles 8 and buckles for fixing the arc-shaped baffles 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 of the plurality of arc-shaped baffles 8 and the intensifier set 10 is 0.8 times the tower diameter of the tower reactor 6; the top of the tower reactor 6 is further provided with a product outlet, the bottom of the tower reactor 6 is provided with a feed inlet and a circulating feed inlet, and the bottom of the tower reactor 6 is further provided with a circulating discharge outlet, and the feed inlet and the circulating feed inlet are both connected into the intensifier set 10;
[0039] The included angle between the arc-shaped baffle and the side wall of the tower reactor 6 is 10°, the spacing between two arc-shaped baffles distributed on the same side is 1.5 times the tower diameter of the tower reactor 6, and the entire arc length of the arc-shaped baffle is 0.75 times the tower diameter of the tower reactor;
[0040] Further, the reaction system of the utility model further comprises a mixer 2 and a pre-reaction device 4 connected in sequence, wherein the bottom of the pre-reaction device 4 is further provided with an intensifier set 10, the bottom of the pre-reaction device is provided with a mixer feed inlet, and the mixer feed inlet is connected into the intensifier set 10, and the mixer 2 is connected with the pre-reaction device 4 through the mixer feed inlet;
[0041] Further, the bottom of the mixer feed inlet is further provided with an air inlet, wherein the air inlet is also connected into the intensifier set 10, and an ethylene gas cylinder 11 is connected with the pre-reaction device 4 through the air inlet;
[0042] The top of the pre-reaction device 4 is provided with a discharge outlet, the discharge outlet is connected with the feed inlet provided at the bottom of the tower reactor 6, and a centrifugal pump 5 is further arranged between the discharge outlet and the feed inlet;
[0043] Wherein, a circulating pump 9 and a heat exchanger 12 are further arranged in sequence between the circulating discharge outlet and the circulating feed inlet;
[0044] The reaction system of the utility model further comprises a product tank 7, and the product tank is connected with the tower reactor through the product outlet.
[0045] The reaction process of the tower reaction system for producing PAO or POE of the utility model is as follows:
[0046] The catalyst is introduced into the mixer 2 through the catalyst feed inlet 3 arranged on one side of the mixer 2, and is fully stirred and mixed with the solvent introduced through the solvent feed inlet 1 arranged at the top of the mixer 2;
[0047] After the catalyst is mixed with the solvent uniformly in the mixer 2, the mixture is introduced into the inside of the mixer 2 through a mixer feed port arranged at the bottom of the mixer 2, and is introduced into the intensifier set 10 arranged at the bottom of the pre-reactor 4 together with ethylene introduced into the ethylene inlet arranged at the bottom of the pre-reactor 4 at a flux of 1 t / h, and the reactants are broken into extremely small micro-particles and then preliminarily reacted in the pre-reactor 4;
[0048] After the preliminary reaction is completed, the centrifugal pump 5 pumps the reaction liquid in the pre-reactor 4 into the intensifier set 10 arranged at the bottom of the tower reactor 6 through the feed port arranged at the bottom of the tower reactor 6, the reaction liquid is broken into small particles again in the intensifier set 10, and further intensified reaction is carried out, and the reaction liquid is circulated and intensified through the circulating pump 9, the circulating outlet and the circulating inlet arranged at the bottom of the tower reactor 6, and the ethylene is rapidly polymerized through continuous intensified reaction, and then the reaction liquid forms a plug flow in the tower reactor 6 due to the multiple baffle assemblies arranged in the tower reactor 6, and continuously climbs along the arc baffle plate 8 to avoid back mixing, wherein the baffle assembly comprises multiple arc baffle plates 8 and buckles for fixing the arc baffle plates 8 to the tower reactor 6, and the product is taken out from the product outlet arranged at the top of the tower reactor 6 when the conversion rate and other indicators of the product reach the standard, and is stored in the product tank 7.
[0049] Embodiment 2
[0050] The utility model discloses a kind of tower reactor systems of ethylene polymerization production PAO or POE, including tower reactor 6;Wherein tower reactor 6 is sequentially provided with baffle assembly and intensifier set 10 in sequence;
[0051] Baffle assembly includes multiple arc baffle plates 8 and buckle for realizing the arc baffle plate 8 with the tower reactor 6 fixedly connected, arc baffle plate 8 is staggered distribution in the tower reactor 6, the distance between the arc baffle plate 8 in the multiple arc baffle plates 8 and the intensifier set 10 between bottom is 1.2 times of the tower diameter of the tower reactor 6;The top of the tower reactor 6 is also provided with product outlet, the bottom of the tower reactor 6 is provided with feed port and circulating feed port, the bottom of the tower reactor 6 is also provided with circulating outlet, and the feed port and circulating feed port are all introduced into the intensifier set 10;
[0052] Wherein the included angle between arc baffle and the side wall of tower reactor 6 is 20 °, and the spacing between two arc baffles distributed on the same side is 2.5 times of the tower diameter of the tower reactor 6, and the whole arc length of arc baffle is 1 times of the tower diameter of the tower reactor;
[0053] Further, the reaction system of the utility model further includes the mixer 2 and the pre-reactor 4 that are connected in sequence, wherein the bottom of the pre-reactor 4 is further provided with the intensifier set 10, the bottom of the pre-reactor is provided with the mixer feed inlet, and the mixer feed inlet leads into the intensifier set 10, and the mixer 2 is connected with the pre-reactor 4 through the mixer feed inlet;
[0054] Further, the lower portion of the mixer feed inlet is further provided with the gas inlet, wherein the gas inlet also leads into the intensifier set 10, and the ethylene gas cylinder 11 is connected with the pre-reactor 4 through the gas inlet;
[0055] The top of the pre-reactor 4 is provided with the discharge port, the discharge port is connected with the feed inlet arranged at the bottom of the tower reactor 6, and the centrifugal pump 5 is further arranged between the discharge port and the feed inlet;
[0056] The circulation pump 9 and the heat exchanger 12 are further arranged between the circulation discharge port and the circulation feed inlet in sequence;
[0057] The reaction system of the utility model further includes the product tank 7, and the product tank is connected with the tower reactor through the product outlet.
[0058] The reaction process of the tower reactor system for the production of PAO or POE of the utility model is as follows:
[0059] The catalyst is introduced into the mixer 2 through the catalyst feed inlet 3 arranged at one side of the mixer 2, and is fully stirred and mixed with the solvent introduced through the solvent feed inlet 1 arranged at the top of the mixer 2;
[0060] After the catalyst and the solvent are uniformly mixed in the mixer 2, the catalyst and the solvent are introduced into the mixer 2 through the mixer feed inlet arranged at the bottom of the mixer 2, and the ethylene introduced through the ethylene gas inlet arranged at the bottom of the pre-reactor 4 is introduced into the intensifier set 10 arranged at the bottom of the pre-reactor 4 together with the ethylene, and the reactants are broken into tiny particles and then preliminarily react in the pre-reactor 4;
[0061] After the initial reaction is completed, the centrifugal pump 5 pumps the reaction liquid in the pre-reactor 4 from the feed inlet arranged at the bottom of the tower reactor 6 into the intensifier set 10 arranged at the bottom of the tower reactor 6, and the reaction liquid is fully broken into small particles in the intensifier set 10, so as to further perform the intensification reaction, and the circulation pump 9 arranged at the bottom of the tower reactor 6 is used to perform the circulation intensification reaction through the circulation outlet and the circulation inlet, so that the ethylene is rapidly polymerized through continuous intensification reaction, and then the reaction liquid forms a plug flow in the tower reactor 6 due to the multiple baffle components arranged in the tower reactor 6, continuously climbs along the arc baffle plate 8, and thus the back mixing is avoided, wherein the baffle components include multiple arc baffle plates 8 and buckles for fixing the arc baffle plates 8 to the tower reactor 6; when the conversion rate and other indicators of the product reach the standard, the product is taken out from the product outlet arranged at the top of the tower reactor 6 and stored in the product tank 7.
[0062] Finally, it should be pointed out that: the above embodiments are only used to illustrate the technical solutions of the present application, and not to limit them; although the present application has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that: it can still modify the technical solutions recorded in the foregoing embodiments, or make equivalent replacement for part or all of the technical features; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the scope of the technical solutions of the embodiments of the present application.
Claims
1. A tower reactor system for the polymerization of PAO or POE from ethylene, characterized in that, The tower reactor comprises a baffle assembly and a reinforcing unit arranged in sequence; the baffle assembly comprises a plurality of arc-shaped baffles and buckles for fixing the arc-shaped baffles to the tower reactor; the arc-shaped baffles are staggered in the tower reactor; the distance between the arc-shaped baffle at the bottom of the plurality of arc-shaped baffles and the reinforcing unit is 0.8-1.2 times the diameter of the tower reactor; the top of the tower reactor is provided with a product outlet; the bottom of the tower reactor is provided with a feed inlet and a circulating feed inlet; the bottom of the tower reactor is also provided with a circulating discharge outlet; the feed inlet and the circulating feed inlet are connected to the reinforcing unit.
2. The column reactor system for the production of PAO or POE from ethylene according to claim 1, characterized in that The included angle between the arc-shaped baffle and the tower reactor is 10-20°.
3. The column reactor system for the production of PAO or POE from ethylene according to claim 1, characterized in that The distance between two arc-shaped baffles distributed on the same side is 1.5-2.5 times the diameter of the tower reactor.
4. The column reactor system for the polymerization of PAO or POE from ethylene according to claim 1, characterized in that The entire arc length of the arc-shaped baffle is 0.75-1 times the diameter of the tower reactor.
5. The columnar reaction system for the production of PAO or POE from ethylene according to claim 1, characterized in that, The tower reactor is further provided with a mixer and a pre-reactor connected in sequence; the bottom of the pre-reactor is provided with a reinforcing unit; the bottom of the pre-reactor is provided with a mixer feed inlet; the bottom of the mixer feed inlet is further provided with an ethylene gas inlet; the mixer feed inlet and the ethylene gas inlet are connected to the reinforcing unit; the mixer is connected to the pre-reactor through the mixer feed inlet.
6. The column reactor system for the polymerization of PAO or POE from ethylene according to claim 5, characterized in that The bottom of the mixer feed inlet is further provided with a gas inlet connected to the reinforcing unit; an ethylene gas cylinder is connected to the pre-reactor through the gas inlet.
7. The column reactor system for the polymerization of PAO or POE from ethylene according to claim 5, characterized in that The top of the pre-reactor is provided with a discharge outlet connected to the feed inlet; a centrifugal pump is arranged between the discharge outlet and the feed inlet.
8. The columnar reaction system for the production of PAO or POE from ethylene according to claim 1, characterized in that, A circulating pump and a heat exchanger are arranged in sequence between the circulating discharge outlet and the circulating feed inlet.
9. The columnar reaction system for the production of PAO or POE from ethylene according to claim 1, characterized in that, The tower reactor is further provided with a product tank connected to the tower reactor through the product outlet.