A tower type reaction system for producing PAO or POE from ethylene and a reaction method thereof

Abstract

The application provides a tower type reaction system for ethylene polymerization to produce PAO or POE and a reaction method thereof, wherein the reaction system comprises a tower type reactor; wherein a baffle assembly and a reinforcing unit are sequentially arranged in the tower type reactor, the baffle assembly comprises a plurality of arc baffles and buckles for fixing the arc baffles to the tower type reactor, the arc baffles are staggered in the tower type reactor, and the distance between the arc baffle at the bottom of the plurality of arc baffles and the reinforcing unit is 0.8-1.2 times of the tower diameter of the tower type reactor; a product outlet is further arranged at the top of the tower type reactor, a feeding port and a circulating feeding port are arranged at the bottom of the tower type reactor, a circulating discharge port is further arranged at the bottom of the tower type reactor, and the feeding port and the circulating feeding port are both connected to the reinforcing unit. The application controls the polymerization degree and the reaction time of the polymerization reaction by using the tower type reactor and the arc baffles.

Description

TECHNICAL FIELD

[0001] The present application belongs to the field of chemical engineering and process technology, and specifically to a tower type reaction system for ethylene polymerization to produce PAO or POE and a reaction method thereof. BACKGROUND

[0002] In the field of chemical materials, poly-alpha-olefins (PAO) and polyolefin elastomers (POE) are increasingly widely used due to their unique properties. 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, and 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 plastics 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 a coil type reactor, which is widely used in industry, but has a major drawback of being unable to control the residence time of the reaction liquid and having a large fluid dead zone. If the residence time is short, the flow rate of the reaction liquid in the coil is fast, resulting in insufficient ethylene polymerization and not reaching the desired target product conversion rate. If the residence time is too long, the generated product will continue to polymerize in the coil, resulting in a decrease in product selectivity. Moreover, the coil type reactor is more difficult to clean, occupies a large indoor area, and has a high instrument cost. 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 present application is proposed. SUMMARY

[0006] The first object of the present application is to provide a tower type reaction system for ethylene polymerization to produce PAO or POE. The device combines a strengthening unit and a baffle assembly to increase the mass transfer resistance between the gas-liquid two phases while reducing the dead zone of the fluid in the reaction tower, better avoiding backmixing of the reaction liquid while continuously climbing the reaction liquid, thereby effectively controlling the polymerization degree and reaction time of the polymerization reaction. In addition, the present application 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 the traditional reactor.

[0007] The second object of the present application is to provide a method for reaction of a tower type reaction system for ethylene polymerization to produce PAO or POE, which is simple in operation, mild in operation condition and high in product yield.

[0008] In order to achieve the above object of the present application, the following technical solutions are adopted:

[0009] A tower type reaction system for ethylene polymerization to produce PAO or POE comprises a tower type reactor, wherein a baffle assembly and a reinforcing unit are sequentially arranged in the tower type reactor, the baffle assembly comprises a plurality of arc-shaped baffles and buckles for fixing the arc-shaped baffles to the tower type reactor, the arc-shaped baffles are staggered in the tower type 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 of the tower diameter of the tower type reactor, a product outlet is arranged at the top of the tower type reactor, a feed inlet and a circulating feed inlet are arranged at the bottom of the tower type reactor, a circulating discharge outlet is arranged at the bottom of the tower type reactor, and the feed inlet and the circulating feed inlet are both connected to the reinforcing unit.

[0010] In the reaction system of the present application, by adopting a tower reactor and arranging a reinforcing unit in the tower reactor, sufficient contact between the reaction liquids is ensured, the problem of excessively 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 conversion rate is improved, and the problem of excessive occupation area in the traditional reactor is overcome; the arrangement of the reinforcing unit enables the reaction liquid to be mixed violently and then broken into extremely small gas-liquid mixture particles, the reaction liquid is fully mixed and the contact area between the two is increased by the assistance of the reinforcing unit, thereby increasing the reaction rate and improving the conversion rate; in order to avoid back mixing of materials during the condensation reaction of the tower reactor, which causes mixing of materials with different residence times, causes some polymer chains to grow for too long a time, and some chains to terminate too early, thereby affecting product yield and back mixing of materials prolonging the residence time of some materials, causing excessive condensation of ethylene to produce byproducts, affecting product purity, and back mixing also easily causes some catalysts to be wrapped by reacted polymers, so that the active sites on the catalyst cannot contact fresh units, thereby affecting reaction efficiency, in addition, back mixing also easily causes uneven distribution of reaction heat, thereby causing mixing of materials in high-temperature and low-temperature regions, causing local overheating and causing the catalyst to be deactivated, therefore, in order to avoid the above problems, a plurality of arc baffles are fixedly arranged in the tower reactor by buckling with the inner wall of the tower reactor, and are staggered distributed in the tower reactor to avoid back mixing between materials, compared with the traditional straight-line baffle, the arc baffle of the present application can better avoid back mixing between materials and also significantly optimize fluid flow behavior, reduce dead volume, thereby improving reaction efficiency, product quality and process stability, the arrangement of the arc baffle can destroy symmetrical flow, thereby enhancing turbulence, the traditional straight-line baffle can cause the fluid to flow along a fixed path, thereby forming a symmetrical dead zone, and the use of the arc baffle can change the direction of the fluid by its curved structure, break the symmetrical fluid pattern, increase the disturbance of the fluid, reduce the residence area, and the staggered distribution of the arc baffle can further disrupt the flow field, avoid the formation of regular vortexes, make the fluid more uniformly distributed in the reactor, and the staggered distribution of the arc baffle can further enhance the contact frequency of the fluid with the heat exchange wall, force the fluid to constantly change the path, reduce the residence time of the material in the high-temperature region, improve the heat transfer coefficient, and reduce the risk of excessive reaction; at the same time, the curved surface of the arc baffle can guide the fluid to produce secondary flow, accelerate micro-mixing, reduce local concentration gradient, and ensure that the molecular weight distribution of the product is narrower; and the fluid scouring action of the arc baffle can reduce wall adhesion, reduce the risk of blockage, and prolong the continuous operation cycle.

[0011] The tower reactor of the present application can be vertically arranged or longitudinally arranged, wherein each baffle plate in the longitudinally arranged tower reactor is composed of two semicircles connected together, the diameter of which is one third of the tower diameter of the tower reactor, and the spacing between two adjacent baffle plates distributed on the same side is four thirds of the tower diameter of the tower reactor to twice the tower diameter, and the arrangement of the longitudinally arranged tower reactor and the arc-shaped baffle plate makes the fluid flow path streamline, further greatly increasing the flow path while avoiding the occurrence of dead zones.

[0012] Preferably, as a further implementable scheme, the included angle between the arc-shaped baffle plate and the tower reactor is 10°-20°.

[0013] In the reaction system of the present application, the included angle between the arc-shaped baffle plate and the side wall of the tower reactor has a significant influence on the fluid dead zone size and reaction efficiency, wherein if the included angle is smaller, it will cause the fluid to collide weakly with the side wall when turning along the arc surface of the baffle plate, and it is easy to form a larger dead zone in the corner of the baffle plate back and the side wall; and if the included angle is larger, it will cause the fluid to form 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 "jetting" phenomenon and thus cause local excessive shear, therefore, for the present application, when the included angle between the arc-shaped baffle plate and the side wall of the tower reactor is 10°-20°, the fluid turning kinetic energy is increased, secondary flow is generated to further destroy the stability of the dead zone, further compress the dead zone volume, so that the mixing efficiency of the material is improved, the catalyst is more uniformly dispersed, and the reaction effect is excellent.

[0014] Preferably, as a further implementable scheme, the spacing between two arc-shaped baffle plates distributed on the same side is 1.5-2.5 times the tower diameter of the tower reactor.

[0015] In the present application, the spacing between the staggered arc-shaped baffle plates is a key parameter affecting the reaction efficiency and dead zone size, wherein if the spacing between two arc-shaped baffle plates distributed on the same side is smaller, it may cause the fluid to form a turbulent dead zone on the back of the baffle plate, thereby affecting the reaction efficiency; and if the spacing is larger, a low-speed stagnant zone is easily formed between the baffle plates, thereby affecting the product structure, therefore, for the present application, when the spacing 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.

[0016] Preferably, as a further implementable scheme, the entire arc length of the arc-shaped baffle plate is 0.75-1 times the tower diameter of the tower reactor.

[0017] 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 provided 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.

[0018] 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.

[0019] Preferably, as a further implementable scheme, an inlet is further provided 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.

[0020] 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 provided between the discharge port and the feed port.

[0021] Preferably, as a further implementable scheme, a circulation pump and a heat exchanger are further sequentially provided between the circulation discharge port and the circulation feed port.

[0022] Preferably, as a further implementable scheme, a product tank is further connected to the column reactor through the product outlet.

[0023] In the reaction system of the present application, after the reactants are fully mixed in 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 intensively mixed by the reinforced unit and then broken into extremely small gas-liquid mixture particles, the auxiliary of the reinforced unit is used 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 reactants are broken into smaller particles by the reinforced unit for intensive reaction to produce the final product, wherein 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 leading to 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 polymerization degree of ethylene, 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 circulation pump arranged at the bottom of the column reactor, and the ethylene is further fully reacted by continuous circulation.

[0024] The intensifier unit of the application belongs to the prior art, although some are of the pneumatic type, some are of the hydraulic type, and some are of the gas-liquid linkage type, but the difference between the types is mainly to select according to the different specific working conditions, and in addition, the connection of the intensifying reaction tower and the reactor and other equipment, including the connection structure and the connection position, is determined according to the structure of the intensifying reaction tower, which is not limited.

[0025] The application also provides a reaction method of the tower type reaction system for producing PAO or POE by ethylene polymerization, comprising the following steps:

[0026] The catalyst and the solvent are mixed to obtain a mixed solution, and then the mixed solution and ethylene are mixed and broken into micro-bubbles to perform condensation reaction.

[0027] The reaction temperature for producing PAO by ethylene polymerization is 50-110°C, the reaction pressure is 0.8-5 MPa, and the residence time is about 4-9 h;

[0028] The reaction temperature for producing POE by ethylene polymerization is 30-60°C, the reaction pressure is normal pressure, and the reaction time is 1-3 h.

[0029] In the reaction process of the application, the volume ratio of ethylene to solvent is 1:2-1:3, and the mass ratio of catalyst to ethylene is 1:50-1:100. By adjusting the ratio of raw materials and using the tower type reaction system for producing PAO or POE by ethylene polymerization provided by the application, the PAO yield can reach 80-90%, and the POE yield can reach 85-95%.

[0030] Compared with the prior art, the application has the following advantages:

[0031] (1) The tower type reaction system for producing PAO or POE by ethylene polymerization provided by the application increases the mass transfer resistance between gas-liquid two phases while reducing the dead zone of the fluid in the reaction tower by combining the intensifier unit and the baffle assembly, better avoids the back mixing of the reaction liquid, and continuously climbs the reaction liquid, so as to effectively control the polymerization degree and the reaction time of the polymerization reaction. In addition, the application also innovatively uses a tower type reactor, which can more effectively control the ethylene polymerization degree compared with the reaction tower in the traditional process, realize efficient and accurate production of PAO or POE with high conversion rate and high selectivity, and overcome the problem of large occupied area in the traditional reactor.

[0032] (2) The reaction method of the tower type reaction system for producing PAO or POE by ethylene polymerization provided by the application is simple in operation, mild in operation condition, and high in product yield. BRIEF DESCRIPTION OF DRAWINGS

[0033] 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. The accompanying drawings are included to provide a description of the preferred embodiments and are not intended to limit the scope of the application. Furthermore, the drawings are not necessarily drawn to scale and like reference numerals designate like parts throughout the several views.

[0034] Figure 1 Structure diagram of a tower reactor system for producing PAO or POE by ethylene polymerization according to the present application;

[0035] In the drawings:

[0036] 1. solvent feed port; 2. mixer; 3. catalyst feed port; 4. pre-reactor; 5. centrifugal pump; 6. tower reactor; 7. product tank; 8. arc baffle; 9. circulation pump; 10. intensifier unit; 11. ethylene cylinder; 12. heat exchanger. DETAILED DESCRIPTION

[0037] The technical solutions of the present application will be described clearly and completely in combination with 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, not all the embodiments, and are only used to illustrate the present application, and should not be considered 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 fall 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 used are not marked with the manufacturer, which are conventional products that can be purchased on the market.

[0038] In the description of the present application, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer" and the like indicate the orientation or positional relationship based on the orientation or positional relationship 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 indicating or implying that the devices or elements referred to must have a particular orientation, be constructed and operated in a particular 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.

[0039] In the description of the present application, it should be noted that unless otherwise explicitly specified and limited, the terms "mounting", "connection", "linking" should be understood in a broad sense, for example, it can be fixed connection, or detachable connection, or integrally connected; it can be mechanical connection, or electrical connection; it can be directly connected, or indirectly connected through intermediate medium, or the internal communication of 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.

[0040] In order to more clearly illustrate the technical solutions in the present application, the following will be described in the form of specific examples.

[0041] Example 1

[0042] Referring to the drawings accompanying the specification Figure 1

[0043] As Figure 1 shown, the present application is a tower type reaction system for producing PAO or POE by ethylene polymerization, which comprises a tower type reactor 6; wherein a baffle assembly and a reinforcing unit 10 are sequentially arranged in the tower type reactor 6;

[0044] The baffle assembly comprises a plurality of arc-shaped baffles 8 and buckles for realizing the fixed connection of the arc-shaped baffles 8 with the tower type reactor 6, the arc-shaped baffles 8 are staggered distributed in the tower type reactor 6, the distance between the arc-shaped baffle 8 at the bottom of the plurality of arc-shaped baffles 8 and the reinforcing unit 10 is 0.8 times of the tower diameter of the tower type reactor 6; the top of the tower type reactor 6 is further provided with a product outlet, the bottom of the tower type reactor 6 is provided with a feed inlet and a circulating feed inlet, and the bottom of the tower type reactor 6 is further provided with a circulating discharge outlet, and the feed inlet and the circulating feed inlet are both communicated into the reinforcing unit 10;

[0045] The included angle between the arc-shaped baffle and the side wall of the tower type reactor 6 is 10°, the spacing between two arc-shaped baffles distributed on the same side is 1.5 times of the tower diameter of the tower type reactor 6, and the entire arc length of the arc-shaped baffle is 0.75 times of the tower diameter of the tower type reactor;

[0046] Further, the reaction system of the present application further comprises a mixer 2 and a pre-reactor 4 connected in sequence, wherein the bottom of the pre-reactor 4 is further provided with a reinforcing unit 10, the bottom of the pre-reactor is provided with a mixer feed inlet, and the mixer feed inlet is communicated into the reinforcing unit 10, and the mixer 2 is connected with the pre-reactor 4 through the mixer feed inlet;

[0047] Further, a gas inlet is further arranged below the mixer feed inlet, wherein the gas inlet is also communicated into the reinforcing unit 10, and an ethylene gas cylinder 11 is connected with the pre-reactor 4 through the gas inlet;

[0048] The top of the pre-reactor 4 is provided with a discharge port connected with an inlet port provided at the bottom of the column reactor 6, and a centrifugal pump 5 is further provided between the discharge port and the inlet port;

[0049] The circulation pump 9 and the heat exchanger 12 are further provided between the circulation discharge port and the circulation inlet port in sequence;

[0050] The reaction system further comprises a product tank 7 connected with the column reactor through a product outlet.

[0051] The reaction process of the column reactor system for producing PAO or POE from ethylene polymerization is as follows:

[0052] The catalyst is introduced into the mixer 2 from a catalyst inlet port 3 provided at one side of the mixer 2, and is fully stirred and mixed with the solvent introduced from a solvent inlet port 1 provided at the top of the mixer 2;

[0053] After the catalyst and the solvent are uniformly mixed in the mixer 2, the mixture is introduced into the mixer 2 through a mixer inlet port provided at the bottom of the mixer 2, and is introduced into the intensifier set 10 provided at the bottom of the pre-reactor 4 together with the ethylene introduced into the ethylene inlet port provided at the bottom of the pre-reactor 4 at a flux of 1 t / h, so that the reactants are broken into extremely small micro-particles and then preliminarily react in the pre-reactor 4;

[0054] After the preliminary reaction is completed, the centrifugal pump 5 pumps the reaction liquid in the pre-reactor 4 into the intensifier set 10 provided at the bottom of the column reactor 6, so that the reaction liquid is again broken into small particles in the intensifier set 10, thereby further strengthening the reaction, and the reaction liquid is circulated and strengthened through the circulation pump 9, the circulation discharge port and the circulation inlet port provided at the bottom of the column reactor 6, so that the ethylene is rapidly polymerized through continuous strengthening reaction, and then the reaction liquid forms a plug flow in the column reactor 6 due to the multiple baffle assemblies provided in the column reactor 6, and continuously climbs along the arc-shaped baffle plates 8 to avoid back mixing, wherein the baffle assembly comprises multiple arc-shaped baffle plates 8 and buckles for fixing the arc-shaped baffle plates 8 to the column reactor 6; when the conversion rate and other indicators of the product reach the standard, the product is taken out from the product outlet provided at the top of the column reactor 6 and stored in the product tank 7.

[0055] Example 2

[0056] The column reactor system for producing PAO or POE from ethylene polymerization comprises a column reactor 6, wherein the column reactor 6 is provided with a baffle assembly and an intensifier set 10 in sequence;

[0057] 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 baffles 8 at the bottom of the plurality of arc-shaped baffles 8 and the intensifier set 10 is 1.2 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 to the intensifier set 10;

[0058] The included angle between the arc-shaped baffle and the side wall of the tower reactor 6 is 20°, and the spacing between the two arc-shaped baffles distributed on the same side is 2.5 times the tower diameter of the tower reactor 6, and the entire arc length of the arc-shaped baffle is 1 times the tower diameter of the tower reactor;

[0059] Further, the reaction system of the present application further comprises a mixer 2 and a pre-reactor 4 connected in sequence, wherein the bottom of the pre-reactor 4 is further provided with an intensifier set 10, the bottom of the pre-reactor is provided with a mixer feed inlet, and the mixer feed inlet is connected to the intensifier set 10, and the mixer 2 is connected to the pre-reactor 4 through the mixer feed inlet;

[0060] Further, the bottom of the mixer feed inlet is further provided with an air inlet, wherein the air inlet is connected to the intensifier set 10, and the ethylene gas cylinder 11 is connected to the pre-reactor 4 through the air inlet;

[0061] The top of the pre-reactor 4 is provided with a discharge outlet, the discharge outlet is connected to the feed inlet provided at the bottom of the tower reactor 6, and a centrifugal pump 5 is further provided between the discharge outlet and the feed inlet;

[0062] Wherein, a circulating pump 9 and a heat exchanger 12 are further provided between the circulating discharge outlet and the circulating feed inlet in sequence;

[0063] The reaction system of the present application further comprises a product tank 7 connected to the tower reactor through the product outlet.

[0064] The reaction process of the tower reactor system for producing PAO or POE of ethylene polymerization of the present application is as follows:

[0065] The catalyst enters the mixer 2 from the catalyst feed inlet 3 provided on one side of the mixer 2, and is fully stirred and mixed with the solvent introduced from the solvent feed inlet 1 provided at the top of the mixer 2;

[0066] 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 the mixer feeding 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 the ethylene introduced into the ethylene feeding port 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 are preliminarily reacted in the pre-reactor 4;

[0067] 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 feeding port arranged at the bottom of the tower reactor 6, the reaction liquid is broken into small particles again in the intensifier set 10, so that the intensified reaction is further carried out, and the intensified reaction is carried out through the circulation of the reaction liquid by the circulation pump 9 through the circulation feeding port and the circulation feeding port arranged at the bottom of the tower reactor 6, the ethylene is rapidly polymerized through the continuous intensified reaction, and then the reaction liquid is formed into a plug flow in the tower reactor 6 due to the multiple baffle components arranged in the tower reactor 6, and is continuously climbed along the arc baffle plate 8, so that the back mixing is avoided, wherein the baffle components include the arc baffle plate 8 and the buckle for fixing the arc baffle plate 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 indexes of the product reach the standard, and is stored in the product tank 7.

[0068] Finally, it should be noted 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-type reaction system for the polymerization of ethylene to produce PAO or POE, characterized in that, The reactor includes a tower reactor; wherein a baffle assembly and an intensifier unit are sequentially arranged within the tower reactor. The baffle assembly includes multiple arc-shaped baffles and clips for fixing the arc-shaped baffles to the tower reactor. The arc-shaped baffles are staggered within the tower reactor. The distance between the bottom arc-shaped baffle and the intensifier unit is 0.8-1.2 times the diameter of the tower reactor. The top of the tower reactor also has a product outlet, and the bottom of the tower reactor has a feed inlet and a circulating feed inlet. The bottom of the tower reactor also has a circulating discharge outlet. Both the feed inlet and the circulating feed inlet lead into the intensifier unit.

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

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

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

5. The tower reaction system for producing PAO or POE by ethylene polymerization according to claim 1, characterized in that, It also includes a mixer and a pre-reactor connected in sequence, wherein an intensifier unit is provided at the bottom of the pre-reactor; a mixer inlet is provided at the bottom of the pre-reactor, and an ethylene gas inlet is provided below the mixer inlet. The mixer inlet and the ethylene gas inlet are connected to the intensifier unit, and the mixer is connected to the pre-reactor through the mixer inlet.

6. The tower reaction system for ethylene polymerization to produce PAO or POE according to claim 5, characterized in that, An air inlet is also provided below the feed inlet of the mixer, and the air inlet leads into the intensification unit. The ethylene cylinder is connected to the pre-reactor through the air inlet.

7. The tower reaction system for ethylene polymerization to produce PAO or POE according to claim 5, characterized in that, The pre-reactor is provided with a discharge port at the top, which is connected to the inlet. A centrifugal pump is also provided between the discharge port and the inlet.

8. The tower reaction system for producing PAO or POE by ethylene polymerization according to claim 1, characterized in that, A circulating pump and a heat exchanger are also sequentially installed between the circulating discharge port and the circulating inlet.

9. The tower reaction system for producing PAO or POE by ethylene polymerization according to claim 1, characterized in that, It also includes a product tank, which is connected to the tower reactor via the product outlet.

10. A reaction method for a tower-type reaction system for the polymerization of ethylene to produce PAO or POE as described in any one of claims 1-9, characterized in that, Includes the following steps: A catalyst and solvent are introduced and mixed to obtain a mixture. The mixture is then mixed with ethylene and broken into microbubbles for condensation reaction to obtain the final product.

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